Cameron Hydraulic Data

CAMERON HYDRAULIC DATA A handy reference on the subject of hydraulics, and steam Edited by C. R. Westaway and A. W. L...

Author: Ingersoll-Rand

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CAMERON HYDRAULIC DATA A handy reference on the subject of hydraulics, and steam

Edited by

C. R. Westaway and

A. W. Loomis

Sixteenth Edition Third Printing

Price $10.00

&INGERSOLLRANR Woodcliff Lake, N.J. 07675

Pump Manufacturing Plants Phillipsburg, N.J., U.S.A. Allentown, Pa., U.S.A. Gateshead, Co. Durham, England Sherbrooke, Que., Canada KitchnerICambridge, Ontario, Canada Naucalpan de Juarez, Mexico Alberton, Transvaal, So. Africa Coslada, Madrid, Spain

Preface to the Sixteenth Edition (2nd Printing) The Cameron Hydraulic Data Book is an Ingersoll-Rand publication and, as in the previous fifteen editions, is published as an aid to engineers involved with the selection and application of pumping equipment. The information in the sixteenth edition, has been updated and brought in line with current practice, primarily the data dealing with the flow of liquids through pipes, valves and fittings. Other information which has been expanded on in considerable detail includes: "Weight-Volume Relationships for Cellulose FiberWater Suspensions" and the section on conversion factor (metric) data. Also, minor rearrangements of certain material has been made for more convenient reference; in addition, some additional data on density, specific gravity, specific weight, vapor pressure and viscosity of various liquids that may be of help and interest has been included.

Copyright 1926, 1930, 1934, 1939, 1942, 1951, 1958, 1961, 1965, 1970, 1977, 1979, 1981, 1984 b y Ingersoll-Rand Company All rights reserved PRINTED IN U.S.A.

To facilitate locating the desired data, a detailed index has been provided in the rear of this book (Section IX). It should be noted that for convenient reference this index is arranged in two (2) parts; first a General Index with items listed alphabetically, page 9-2 through page 9-10, and secondly, an Index of Liquids arranged alphabetically, page 9-11 through page 9-14. Frequent reference to this index is suggested for quickly locating the information desired.

Form 931

11

iii

INGERSOLLRAND CAMERON Contents Hydraulic principles

..........................

Selected formulas and equivalents ..............

Friction data. ................................ Water Paper stock Viscous liquids Fittings WARNING The misuse or misapplication of data in this book could result in machinery or system failures, severe damage to other property and/or serious injury to persons. Ingersoll-Rand Company does not assume any liability for any losses or damages resulting from the use or application of the materials and data set forth in this book.

Liquids-miscellaneous data .................. Density-specific gravity-vapor pressure Viscosity etc Steam data

..................................

Electrical data

...............................

Miscellaneous data. ........................... Data for cast iron & steel pipe-Arithmetrical formulas Metric (SI) Conversions-General

data..

.......

Index-Two Sections: . . . . . . . . . . . . . . . . . . . . . . . . Section No. 1-General Index (A to Z) Section No. 2-Index of Liquids (A to Z)

SECTION I

HYDRAULICS

CAMERON HYDRAULIC DATA CONTENTS OF SECTION 1 Hydraulics Page Introduction . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-3 Liquids . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-3 Liquid Flow . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-4 Viscosity . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-5 Pumping . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-6 Volume- System Head Calculations- Suction Head . . . . . . 1-6, 1-7 Suction Lift -Total Discharge Head -Velocity Head . . . . . . 1-7, 1-8 Total Sys. Head -Pump Head-- Pressure- Spec. Gravity . . . 1-9, 1-10 Net Positive Suction Head . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-11 NPSH -Suction Head-Lift ; Examples: . . . . . . . . . . . . 1-11,to 1-16 NPSH -Hydro-Carbon Corrections . . . . . . . . . . . . . . . . . . . . 1-16 NPSH -Reciprocating Pumps . . . . . . . . . . . . . . . . . . . . . . . . 1-17 Acceleration Head - Reciprocating Pumps . . . . . . . . . . . . . . . 1-18 Entrance Losses -Specific Speed . . . . . . . . . . . . . . . . . . . . . . 1-19 Specific Speed - Impeller . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-19 Specific Speed -Suction . . . . . . . . . . . . . . . . . . . . . . . . . . 1-20, 1-21 Submergence . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-21, 1-22 Intake Design-Vertical Wet Pit Pumps . . . . . . . . . . . . . 1-22 to 1-27 Work Performed in Pumping . . . . . . . . . . . . . . . . . . . . . . . . . . 1-27 Temperature Rise . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-28 Characteristic Curves . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-29 Affinity Laws -Stepping Curves . . . . . . . . . . . . . . . . . . . . . . . 1-30 System Curves . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-31 Parallel and Series Operation . . . . . . . . . . . . . . . . . . . . . . 1-32, 1-33 Water Hammer . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . , . . 1-34 Reciprocating Pumps -Performance . . . . . . . . . . . . . . . . . . . . 1-35 Recip . Pumps-Pulsation Analysis & System Piping . . . 1-36 to 11-45 Pump Drivers- Speed Torque Curves . . . . . . . . . . . . . . . . 1-45, 1-46 Engine Drivers - Impeller Profiles . . . . . . . . . . . . . . . . . . . . . 1-47 Hydraulic Institute Charts . . . . . . . . . . . . . . . . . . . . . . 1-48to 1-52 Bibliography . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1-53

HYDRAULICS Introduction The following outline is offered for those who have a basic understanding and knowledge of hydraulic and fluid dynamic principles, but who would like a convenient reference to various items that must be taken into consideration in the commercial selection and application of pumping equipment. If more detailed information is desired, or to investigate the subject in greater depth, reference is suggested to the many Textbooks, Technical Papers, Engineering Handbooks, Standards and Manuals that are available, some of which are listed in the Bibliography a t the conclusion of this section. (Page 1-53)

Liquids Hydraulics is concerned with the behavior of liquids a t rest and in motion. A liquid has a definite volume a s contrasted to a gas which will expand or contract depending on changes in temperature and pressure. Liquids are said to be "practically" incompressible. This is true for most considerations a t low pressures but a t higher pressures and as temperatures vary, there will be changes in density which must be taken into account. The pressure existing a t any point in a liquid a t rest is caused by the atmospheric pressure exerted on the surface, plus the weight of liquid above the point in question. Such pressure is equal in all directions and acts perpendicularly to any surfaces in contact with the liquid. All liquid pressures can be visualized as being caused by a column of liquid which due to its weight would produce a pressure equivalent to the pressure at the point in question. Such a column of liquid, real or imaginary, is called the "pressure head," or the "static head" and is usually expressed in feet of liquid.

The flow of liquids may be caused by gravity or by mechanical means using one of the many types of pumps that may be available depending on the characteristics of the liquid and the nature of the service conditions.

I

INGERSOLLRAND

CAMERON HYDRAULIC DATA

Fig. No. 1

Volute C a s ~ n g

Reference is made to Figure 1 illustrating diagrammatically a simple centrifugal pump; here it will be observed that in its simplest form a centrifugal pump consists of an impeller rotating within a casing. Liquid directed into the center of the rotating impeller is picked up by the impeller vanes and accelerated to a high velocity by the rotation of the impeller and discharged by centrifugal force into the casing and out the discharge. When the liquid in the impeller is forced away from the center of the impeller a reduced pressure is produced and consequently more liquid flows forward. Therefore a steady flow through the impeller is produced unless something happens to break the vacuum a t the inlet or disrupt the flow to the center of the impeller or unless the flow a t the discharge is restricted by a pressure greater than the pressure head developed by the rotating impeller. Reciprocating Positive Displacement Pumps, on the other hand, do not generate head. Instead, these pumps convert rotating motion and torque into linear motion and force, generating variable flow a t the discharge connection. Head is generated by the system's resistance to flow. Hence, this pump will draw upon available power and energy until it overcomes all flow resistances downstream. If excessive flow restrictions exist, the pump can be over pressurized and the driver may stall or the weakest link in the system can fail. Therefore, it is imperative that a safety relief valve is installed a s close to the pump as possible.

Liquid flow During passage through a pipe the flow of a liquid is said to be laminar (viscous) or turbulent depending on the liquid velocity, pipe size and liquid viscosity. For any given liquid and pipe size these

HYDRAULICS factors can be expressed in terms of a dimensionless number called the Reynolds number R where:

V = Average velocity -f t/sec D = Average internal diameter -ft v = Kinematic viscosity of the fluid-ft2/sec (For pure fresh water a t 60°F v = 0.000 012 16 ft2/sec) For values of R less than approximately 2000 the flow is laminar (viscous); i.e., particles of the liquid follow separate non-intersecting paths with little or no eddying or turbulence. When R is above 4000 turbulent flow is considered to exist. Values of R between 2000 and 4000 are in the critical zone where the flow is generally considered to be turbulent for the purpose of friction loss or pressure drop calculations; this gives safe results because the friction loss is higher for turbulent flow than for laminar (viscous) flow.

Viscosity In flowing liquids the existence of internal friction or the internal resistance to relative motion of the fluid'particles with respect to each other must be considered; this resistance is called viscosity. The viscosities of most liquids vary appreciably with changes in temperature whereas the influence of pressure change is usually negligible. The viscosities of certain liquids can change depending on the extent to which the liquid may be agitated.

A liquid is said to be a "Newtonian" or "true" fluid if its viscosity is unaffected by the kind and magnitude of motion or agitation to which it may be subjected a s long as the temperature remains constant; an example of a "Newtonian" liquid would be water or mineral oil. A liquid is said to be "thixotropic" if its viscosity decreases as agitation is increased a t constant temperature; examples of "thixotropic" liquids would be asphalts, cellulose compounds, glues, greases, molasses, paints and soaps.

t

A liquid is said to be "dilatant" if the viscosity increases as agitation is increased at constant temperature; examples of "dilatant" liquids are clay slurries and candy compounds. Pumping

To move a liquid against gravity or to force it into a pressure vessel, or to provide enough head, or pressure head, to overcome pipe friction and other resistance, work must be expended. The type of pump to be considered for any application is normally a financial decision. Technically, centrifugal and reciprocating pumps can both perform nearly any service function. But large flow applications require such a large reciprocating pump that it is cost prohibitive. Normally such applications are better handled by centrifugal pumps. As a general rule, reciprocating pumps are best suited for low flows and high pressures.

No matter what type of pump is used, nor what service is required of a pump, all forms of energy imparted to the liquid both on the suction and discharge sides in performing this service must be accounted for in establishing the duty to be performed. In centrifugal pump applications in order that all these forms of energy may be algebraically added it is customary to express them all in terms of head expressed in feet of liquid. In reciprocating, rotary, or positive displacement types of pumps it is customary to express the heads in terms of pressure (psi). The various items that must be taken into account in establishing the total head (based on feet of liquid) including design capacity (volume)are discussed below. Volume

In this discussion the standard unit of volume will be the U.S. gallon. The rate of flow shall be expressed in gallons per minute (gpm1. The specific weight of water a t a temperature of 65OF shall be taken as 62.34 lbs per cubic foot. For other temperatures proper specific weight corrections should be made in calculating the rate of flow particularly if the required delivery is given in pounds per hour; for example : lb per hour gpm = '500 X specific gravity

HYDRAULICS System head calculations The total head (H)-formerly called "total dynamic headv-for a specific system is equal to the total discharge head (h,) minus the total suction head (h,) or plus the total suction lift.

It is recommended that total head calculations for the suction side be listed separately from those for the discharge side to help avoid the possibility of overlooking a troublesome suction condition. In this discussion the terms suction head and suction life (or the equivalent of a lift) are discussed separately to help visualize the suction condition that may exist.

Suction head AL k .LA Suction head (h,) exists when the liquid supply level is above the pump centerline or impeller eye. The total suction head is equal to the static height or static submergence in feet that the liquid supply level is above the pump centerline less all suction line losses including entrance loss plus any pressure ( a vacuum as in a condenser hotwell being a negative pressure) existing a t the suction supply source. Caution-even when the liquid supply level is above the pump centerline the equivalent of a lift will exist if the total suction line losses (and vacuum effect) exceed the positive static suction head: This condition can cause problems particularly when handling volatile or viscous liquids. On a'n existing installation total suction head would be the reading of a gage a t the suction flange converted to feet of liquid and corrected to the pump centerline elevation plus the velocity head in feet of liquid at point of gage attachment.

Suction lift Suction lift (h,) exists when the liquid supply level or suction source is below the pump centerline or impeller eye. Total suction lift 5\: :-

* Note: One gallon of water weighs 8.333 pounds a t 65OF; therefore 60 X 8.333 equals 500. For practical applications the * * specific gravity of water is considered to be equal t o 1.00 a t normal temperatures (60°F t o 70°F); for some purposes it is taken a s 1.00 a t 39.Z°F ( 4 O C ) which is its point of maximum density; for most applications which base is selected makes little difference. See pages 2-3 and 4-3. * * Basis specific gravity of 1.00, one psi equals 2.31 f t of water a t normal temperatures.

HYDRAULICS System head calculations The total head (H)-formerly called "total dynamic headv-for a specific system is equal to the total discharge head (h,) minus the total suction head (h,) or plus the total suction lift.

It is recommended that total head calculations for the suction side be listed separately from those for the discharge side to help avoid the possibility of overlooking a troublesome suction condition. In this discussion the terms suction head and suction life (or the equivalent of a lift) are discussed separately to help visualize the suction condition that may exist.

Suction head AL k .LA Suction head (h,) exists when the liquid supply level is above the pump centerline or impeller eye. The total suction head is equal to the static height or static submergence in feet that the liquid supply level is above the pump centerline less all suction line losses including entrance loss plus any pressure ( a vacuum as in a condenser hotwell being a negative pressure) existing a t the suction supply source. Caution-even when the liquid supply level is above the pump centerline the equivalent of a lift will exist if the total suction line losses (and vacuum effect) exceed the positive static suction head: This condition can cause problems particularly when handling volatile or viscous liquids. On a'n existing installation total suction head would be the reading of a gage a t the suction flange converted to feet of liquid and corrected to the pump centerline elevation plus the velocity head in feet of liquid at point of gage attachment.

Suction lift Suction lift (h,) exists when the liquid supply level or suction source is below the pump centerline or impeller eye. Total suction lift 5\: :-

* Note: One gallon of water weighs 8.333 pounds a t 65OF; therefore 60 X 8.333 equals 500. For practical applications the * * specific gravity of water is considered to be equal t o 1.00 a t normal temperatures (60°F t o 70°F); for some purposes it is taken a s 1.00 a t 39.Z°F ( 4 O C ) which is its point of maximum density; for most applications which base is selected makes little difference. See pages 2-3 and 4-3. * * Basis specific gravity of 1.00, one psi equals 2.31 f t of water a t normal temperatures.

INGERSOLL-RAND CAMERON HYDRAULIC DATA is equal to the static lift in feet plus all friction losses in the suction line including entrance loss. When the liquid supply level or suction source is above the pump centerline or impeller eye and under a vacuum, as in a condenser hotwell, the equivalent of a suction lift will exist which will be equal to the vacuum effect in feet less the net submergence. On an existing installation the total suction lift is the reading of a mercury column or vacuum gage a t the suction flange converted to feet of liquid and corrected to the pump centerline elevation minus the velocity head in feet of liquid a t point of gage attachment.

Total discharge head (h,)-is the sum of: (1)Static discharge head. ( 2 )All piping and friction losses on discharge side including straight runs of pipe, losses at all valves, fittings, strainers, control valves, etc. ( 3 ) Pressure in discharge chamber (if a closed vessel). ( 4 ) Losses a t sudden enlargements (as in a condenser water box). ( 5 )Exit loss at liquid discharge (usually assumed to be equal to one velocity head at discharge velocity) ( 6 ) Plus any loss factors that experience .indicates may be desirable.

On an existing installation total discharge head would be the reading of a pressure gage a t the discharge flange converted to feet of liquid and corrected to the pump centerline plus the velocity head (in feet of liquid) at the point of gage attachment.

Velocity head (hv)-in a pumping system is an energy component that represents the kinetic or "velocity" energy in a moving liquid at the point being considered in the system. It is equivalent to the vertical distance the mass of liquid would have to fall (in a perfect vacuum) to acquire the velocity V and is expressed as:

where: h, V d g gpm bph

= velocity head in feet of liquid = velocity of liquid -ft/sec = inside diameter of pipe in inches = gravitational constant -32.174 ft/sec2 = gallons (U.S.)per minute = barrels (42 gallons -U.S. ) per hour

HYDRAULICS -

-

The velocity head energy component is used in system head calculations as a basis for establishing entrance losses, losses in valves and fittings, losses at other sudden enlargements and exit losses by applying the appropriate resistance coefficient K to the VV2g term (see page 3-110). In system head calculations for high head pumps the velocity head will be but a small percentage of the total head and is not significant. However, in low head pumps it can be a substantial percentage and must be considered. When total heads on an existing installation are being determined from gage readings then the velocity head values as calculated must be included; i.e. the total suction lift will be the reading of a vacuum gage or mercury column a t the suction flange, corrected to the pump centerline elevation minus the velocity head a t point of gage attachment. The total suction head and total discharge head will be the readings of gages at the flanges corrected to the pump centerline elevation plus the velocity heads a t the points of gage attachments. Total system head (H)-formerly total dynamic head-is the total discharge head (h,) minus the total suction head (h,) if positive or plus if a suction lift: H = h, - h, (head) or H = h, h, (lift).(Note: For typical suction head calculation, see examples 1, 2, 3, 4 and 5 under NPSH pages 1-13to 1-15. For total head calculation see example on pages 3-9 and 3-10.

+

Pump head -Pressure -Specific gravity

In a centrifugal pump the head developed (in feet)is dependent on the velocity of the liquid as it enters the impeller eye and as it leaves the impeller periphery and therefore is independent of the specific gravity of the liquid. The pressure head developed (in psi) will be directly proportional to the specific gravity. Head and Pressure are interchangeable terms provided that they are expressed in their correct units. In English Units to convert from one to the other use:

Liquid Head in feet = psi x 2.31 SP gr Liquid Head in feet = psi x 144 W

INGERSOLLflAND


Pressure in psi = Head in feet x sp gr 2.31 Pressure in psi = Head in feet x W 144 Where W=*Specific weight in pounds per cubic foot of liquid being pumped under pumping conditions; For Water W = 62.32 lb per cu ft a t 68 degrees F (20°C).

A column of water 2.31 ft high will exert a pressure of one ( I )psi based on water a t approximately 65 F. * Figures 2 and 3 are included to help visualize the head-pressure relationships of centrifugal pumps when handling liquids of varying specific gravities. Fig. 2 illustrates three identical pumps, each pump designed to develop 115.5 f t . of head ; when pumping water with a specific gravity of 1.0 ( a t 6B°F) the pressure head will be 50 psi ( 115.5 f t divided by 2.31); when pumping liquids of other gravities, the head (in feet)will be the same, but the pressure head (psi) will be proportional to the specific gravities as shown; to avoid errors, it is advisable to check one's calculations by using the above formulas.

Fig. 2. Pressure-head ing specific gravities.

relationship of identical pumps handling liquids of differ-

*For other water temperatures see tables on pages 4-4 and 4-5.

HYDRAULKS

Fig. 3 Pressure-head relationship of pumps delivering same pressure handling liquids of differing specific gravity.

Figure 3 illustrates three pumps, each designed to develop the same pressure head (in psi); consequently the head (in feet of liquid) will be inversely proportional to the specific gravity as shown. In these illustrations friction losses, etc., have been disregarded.

Net Positive Suction Head The Net Positive Suction Head (NPSH)is the total suction head in feet of liquid (absolute a t the pump centerline or impeller eye) less the absolute vapor pressure (in feet) of the liquid being pumped. I t must always have a positive value and can be calculated by the following equations: To help in visualizing the conditions that exist, two ( 2 ) expressions will be used; the first expression is basis a suction lift-liquid supply level is below the pump centerline or impeller eye; the second expression is basis a positive suction, (flooded),where the liquid supply level is above the pump centerline or impeller eye. For Suction Lift:

NPSH = ha - h,,, - h,, - hf, For Positive (Flooded)Suction:

NPSH = ha - h,,,

+ h,,

- hf,

I

where: ha = absolute pressure (in feet of liquid) on the surface of the liquid supply level (this will be barometric pressure if suction is from an open tank or sump; or the absolute pressure existing in a closed tank such as a condenser hotwell or deareator ). h,,, = The head in feet corresponding to the vapor pressure of the liquid a t the temperature being pumped. hSt= Static height in feet that the liquid supply level is above or below the pump centerline or impeller eye. h,, = All suction line losses (in feet)including entrance losses and friction losses through pipe, valves and fittings, etc. Two values of net positive suction head must be considered; i.e. Net Positive Suction Head Required (NPSHR) and Net Positive Suction Head Available (NPSHA). The NPSHR is determined by the pump manufacturer and will depend on many factors including type of impeller inlet, impeller design, pump flow, rotational speed, nature of liquid, etc. NPSHR is usually plotted on the characteristic pump performance curve supplied by the pump manufacturer. The Net Positive Suction Head Available (NPSHA)depends on the system layout and must always be equal to or greater than the NPSHR. The vapor pressure of the liquid a t the pumping temperature must always be known to calculate the NPSHA. On an existing installation the NPSH available would be the reading of a gage a t the suction flange converted to feet of liquid absolute and corrected to the pump centerline elevation less the vapor pressure of the liquid in feet absolute plus the velocity head in feet of liquid at point of gage attachment. The following examples show the importance and influence of vapor pressure. In all cases, for simplicity, the same capacity will be used; also the following suction line losses will be assumed in all cases: Friction loss through suction pipe and fittings *Entranceloss (assumeequal to one half velocity head) Total losses ' N o t e : For more exact entrance losses, refer t o pages 3-116 thru 3-118.

2.51 f t 0.41 2.92 f t

HYDRAULICS

IOf

Fig. 4. (Example No 1 )

Example No 1 ( Fig 4 ) Open system, source below pump; 68OF water a t sea level. Atmospheric pressures 14.696 psia, 33.96 f t abs. Vapor pressure of liquid 0.339 psia = 0.783 f t abs.

NPSHA = 33.96 - 0.783 - 10.00 - 2.92 = 20.26 ft Suction Lift = 10.00 + 2.92 = 12.92 ft-this charge head to obtain total head.

is to be added to dis-

Note: No pump can actually lift water on the suction side. In this case, water is forced in by an excess of atmospheric pressure over the vapor pressure less 12.92 f t net static lift. Example No 2 (Fig 5 ) Open system, source above pump; 68OF water at sea level.

NPSHA = 33.96 - 0.783 + 10.00 - 2.92 = 40.26 f t .

Atmospheric Pressure

+-

- - ---- -- -

68OF Water

Fig. 5 (Example 2)

~-~EFT'

-- .-- -

loft.

INGERSOLL-RAND CAMERON HYDRAULIC DATA Suction Head- 10.00 - 2.92 = 7.08 ft-this is to be subtracted from discharge head to obtain total head.

Atmospheric Pressure

2 1 2 0 F --:-.---Water 5 : 10 ft.

Fig. 6 (Example 3)

Example No. 3 (Fig. 6 ) Open system, source above pump; 212OF water a t sea level; vapor pressure same as atmospheric since liquid a t boiling point.

+

NPSHA = 33.96 - 33.96 10.00 - 2.92 = 7.08 f t . In this case, atmospheric pressure does not add to NPSHA since it is required to keep the water in liquid phase. Suction Head = 10.00 - 2.92 = 7.08 ft-this is to be subtracted from discharge head to obtain total head. Note: In this example it was assumed that pipe friction losses for 21z°F water were the same as for 68OF water whereas actually they would be somewhat less, as will also be the case in Example 4.

7

'"

Water

.,,I

Fig. 7 (Example 4)

HYDRAULICS -

Example No 4 (Fig 7 )

Closed system (under pressure as a feed water deareator) source above pump. 350°F water V.P. = 134.60 psia = 348.76 ft abs (at 350°F sp gr = NPSHA = 348.76 - 348.76 + 10.00 - 2.92 = 7.08 ft. Suction Head- (Figure basis gage pressures; i.e., 119.91psig = 310.69 f t ) = 310.69 + 10.00 - 2.92 = 317.77 ft-This is to be subtracted from the discharge head to obtain total system head. I t is important to note that while the suction head is 317.77 f t (122.64 psig) the NPSHA is still only 7.08 ft.

Example No 5 (Fig 8)-Closed system (under vacuum as a condenser hotwell) liquid source above pump. Absolute pressure (ha)= 1.50" Hg X 1.139 = 1.71 ft. Water a t saturation point 91.7Z°F; therefore vapor pressure (h,,) = 1.50" Hg X 1.139 = 1.71 ft. NPSHA = 1.71 - 1.71

+ 10.00 - 2.92 = 7.08ft.

Suction Condition-In this example the suction condition (head or lift) for the pump can best be visualized by the calculations listed below where it can be seen that we have a suction lift equal to the vacuum effect a t the suction source less the net static submergence.

I

CONDENSER

I

Abs = 1-50" Hg Vacuum = 28-42" Hg

[--'It Condensate

d

Fin. 8 (Example 5 )

INGERSOLL-AAND CAMERON HYDRAULIC DATA 28.42"Hg Vacuum = 28.42 x 1.139 = Static submergence Friction and entrance loss Net static submergence = Equivalent suction lift = vacuum effect less net submergence

32.37 f t 10.00 f t 2.92 ft 7.08 ft

7.08 f t 25.29 ft

In this example it is noted that the NPSHA is equal to the static suction head less the friction and entrance losses. Also the equivalent suction lift must be added to the total discharge head to obtain the total system head.

In the foregoing examples standard sea level atmospheric conditions were assumed; for other locations where altitude is a factor proper corrections must be made. These examples (3, 4 and 5) illustrate that if the liquid is in equilibrium (vapor pressure corresponds to saturation temperature) then the NPSH is equal to the difference in elevation between the liquid supply level and the pump centerline elevation (or impeller eye) less the sum of the entrance loss and the friction losses in the suction line. NPSH reductions- hydrocarbon liquids and hot water The NPSH requirements of centrifugal pumps are normally determined on the basis of handling water a t or near normal room temperatures. However, field experience and laboratory tests have confirmed that pumps handling certain gas free hydrocarbon fluids and water a t elevated temperatures will operate satisfactorily with harmless cavitation and less NPSH available than would be required for cold water. The figure on page 1-52 shows NPSH reductions that may be considered for hot water &d certain gas free pure hydrocarbon liquids. The use and application of this chart is subject to certain limitations some of which are summarized below: 1. The NPSH reductions shown are based on laboratory test data

a t steady state suction conditions and on the gas free pure hydrocarbon liquids shown; its application to other liquids must be considered experimental and is not recommended. 2. No NPSH reduction should exceed 50% of the NPSH required for cold water or ten feet whichever is smaller.

HYDRAULICS 3. In the absence of test data demonstrating NPSH reductions

greater than ten feet the chart has been limited to that extent and extrapolation beyond that point is not recommended. 4. Vapor pressure for the liquid should be determined by the bubble point method-do not use the Reid vapor pressure. 5. Do not use the chart for liquids having entrained air or other non-condensible gases which may be released as the absolute pressure is lowered at the entrance to the impeller, in which case additional NPSH may be required for satisfactory operation. 6. In the use of the chart for high temperature liquids, particularly with water, due consideration must be given to the susceptibility of the suction system to transient changes in temperature and absolute pressure which might require additional NPSH to provide a margin of safety, far exceeding the reduction otherwise permitted for steady state operation. Subject to the above limitations, which should be reviewed with the Manufacturer, the procedure in using the chart is as follows: Assume a pump requires 16 feet NPSH on cold water at the design capacity is to handle pure propane at 55 Deg F which has a vapor pressure of approximately 100 psia; the chart shows a reduction of 9.5 feet which is greater than one half the cold water NPSHR. The corrected value of the NPSHR is one half the cold water NPSHR or 8 feet. Assume this same pump has another application to handle propane a t 14 Deg F where its vapor pressure is 50 psia. In this case the chart shows a reduction of 6 feet which is less than one half of the cold water NPSH. The corrected value of NPSH is therefore 16 feet less 6 feet or 10 feet. Note in reading the chart follow the sloping lines from left to right. For a more detailed discussion on the use of this chart and its limitations reference is suggested to the Hydraulic Institute Standards.

NPSH -Reciprocating pumps The foregoing discussion on NPSH and accompanying calculations was primarily for the benefit of centrifugal pump selections and applications. NPSH available for a reciprocating pump application is calculated in the same manner as for a centrifugal pump, except in the NPSH required for a reciprocating pump some additional allowance must be made for the reciprocating action of the pump; this additional re-

INGERSOLL-RAND CAMERON HYDRAULIC DATA -

-

-

quirement is termed "acceleration head." This is the head required to accelerate the liquid column on each suction stroke so that there will be no separation of this column in the pump or suction line. If this minimum condition is not met the pump will experience a fluid knock caused when the liquid column, which has a vapor space between it and the plunger, overtakes the receding plunger. This knock occurs approximately two-thirds of the way through the suction stroke. If sufficient acceleration is provided for the liquid to completely follow the motion of the receding face of the plunger, this knock will disappear. If there is insufficient head to meet minimum acceleration requirements of NPSH, the pump will experience cavitation resulting in loss of volumetric efficiency; also, serious damage can occur to the plungers, pistons, valves and packing due to the forces released in collapsing the gas or vapor bubbles. Acceleration head -reciprocating pumps

For indepth information on NPSH and Acceleration Head, see the section entitled "Pulsation Analysis and System Piping."

Fig. 9

HYDRAULICS Entrance losses

Special mention is made of entrance loss considerations because failure to appreciate and provide for this problem is one of the major causes of faulty pump performance, particularly when handling liquids that are in equilibrium such as light hydrocarbons from a vacuum tower or condensate from a condenser hotwell. Reference to Figure 9 illustrates that when taking suction from the bottom of a tower, or a side outlet from a condenser hotwell, sufficient static height ( h ) must be provided to account for the entrance loss and velocity head a t point "A" plus any additional submergence that may be required to prevent vortices from entering the suction line. The submergence required to control vortices may be reduced by using suitable baffles or other anti-swirl devices. Specific speed

In the intelligent consideration of centrifugal pumps it is helpful to have an understanding of specific speed to determine if the pump design being proposed is within certain established limits for the service conditions under which it will operate. In Specific Speed terminology there are two considerations: ( 1) First-Impeller specific speed and ( 2 ) Secondly-suction specific speed ; Impeller specific speed will be discussed first. Impeller specific speed (N,)

This is an index of hydraulic design; it is defined as the speed at which an impeller, geometrically similar to the one under consideration, would run if it were reduced in size to deliver one gpm a t one foot head. Mathematically it is expressed as:

where: rpm = Pump speed. gpm = Design capacity a t best efficiency point. H = Total head per stage in feet a t best efficiency point.

INGERSOLL-RAND


Impeller specific speed is an index as to the type of impeller when the factors in the above formula correspond to its performance a t optimum (or best) efficiency point. I t is a useful tool for the Hydraulic Designer in the designing of impellers to meet varying conditions of head, capacity (and shape of curve), suction conditions and speed. Impellers for high heads and low net positive suction head required usually have low specific speeds, whereas, impellers for low heads and high NPSHR usually have high specific speeds. Depending on the type of impeller specific speeds can range between 400 to 20,000 for commercial designs. According to specific speed values impellers and pumps can be classified roughly as follows: Below 4200-Centrifugal or Radial type; Between 4200 and 9000-Mixed Flow; Above 900-Axial Flow. The charts and illustrations included herewith-pages 1-47 to 1-48 show typical impeller types for various specific speed ranges; also the variations in head-capacity performance characteristics for various specific speed are illustrated. Specific speed is also a very valuable criterion in determining the permissible safe maximum suction lift or the minimum net positive suction head required for various conditions of capacity, head and speed. The Hydraulic Institute has established suggested specific speed limitations with respect to suction conditions for various types of pumps. These suggested limitations are expressed graphically on charts ,(pages1-49 to 1-52) reproduced herein with permission of the Hydraulic Institute. For a more detailed discussion of these charts and their application reference should be made to the Hydraulic Institute Standards. Suction specific speed ( S )

Suction specific speed (S)like Impeller specific speed (N,) is a parameter, or index of hydraulic design except here it is essentially an index descriptive of the suction capabilities and characteristics of a given first stage impeller. I t is expressed as:

S = rpm Vgpm (NPSHR)3/4

CAMERON HYDRAULIC DATA submergence is a term used to relate liquid level to the setting of a vertical immersed wet pit type pump with a free air surface a t the liquid supply level.

In the case of a conventional horizontal pump operating with a suction lift, or a large dry pit type pump, with a flooded suction, some submergence or liquid level, in addition to the NPSHR, may be necessary to prevent vortex formation on the liquid supply surface and thus preclude or retard the possibility of air being drawn in the pump suction intake. The amount of submergence will depend to some extent on the design of the suction intake; i.e. a bell or cone shaped entrance should require less than a straight pipe intake. Intake design In addition to providing sufficient submergence for vertical wet pit immersed pumps it is imperative that the sump and intake structure be of proper proportions-and that pump arrangements be such as to preclude uneven velocity distributions in the approach to the pump or around the suction bell. Uneven velocity distributions particularly when accompanied by insufficient submergence can result in the formation of vortices which will introduce air in the pump suction causing a reduction in capacity, unbalance and rough operation resulting in rapid deterioration of equipment and costly outages. Also, underwater vortices can form, causing uneven flow into the impeller resulting in rough operation. Providing additional submergence will not compensate for an improperly designed intake and therefore careful consideration must be given to pump arrangement and location of intake and sump dimensions. WARNING Intake design, pump arrangements, location and setting are, among other things, the complete responsibility of the user, and improper use of the following data could result in severe damage to property and/or injury to person. Accordingly, Ingersoll-Rand Company does not assume any liability for any losses or damages to property or injury to persons that may result from the utilization of the following suggested design data. Such design data do not cover all technical considerations for proper operation. They have been developed as a result of extensive model testing and field experience over many years, and are offered herein a s a general guide for preliminary layout work.

HYDRAULICS Vertical wet pit pumps

Referring to Figure 10 and using the pump suction bell diameter* ( D )as a reference: 1. Back wall distance to centerline of pump is 0.75D.

2. Side wall distance to centerline of pump is 1.00D. 3. Bottom clearance (approximate) is 0.30D. 4. Location of the intake screen can vary depending on the particular design, but usually should be in the range of 3D to 4D minimum from inside face of screen to centerline of pump. 5. Intake tunnel velocity should be less than 2 to 3 ft/sec. 6. No restrictions or sharp turns should occur less than 6D or 3 times the channel width in front of the pump, whichever is greater. 7. Provide water depth (submergence)over the pump suction bell in accordance with the "Capacity vs. Submergence" chart -Fig. No. 14. *Check Manufacturer for dimensions.

Tra

Fig. 10 Standard Vertical Wet Pit Pump

Fig. 11 Turning Vane Assembly

Multiple pump arrangements

The preferred arrangement is to have the pump suction bells located in individual pump bays by means of separator walls or parti-

tions so one pump will not interfere hydraulically with the operation of another. However, if this is not practical, as may be the case with small pumps, a number of units can be installed in a single large sump provided that: 1. They are located in a line running perpendicular to the ap-

2. 3.

4. 5.

6.

proaching flow. Minimum spacing of 2D is provided between pump centerlines. Back wall clearance, bottom clearance and submergence same as for single pumps. All pumps are running. The up-stream conditions should provide uniform flow to the suction bells (avoid turns). Each pump capacity is less than 15,000 gpm.

When individual pump bays are provided use dimensions for a single pump in accordance with Fig. 10, page 1-23. nrning vane intake assemblies

Structural costs can sometimes be reduced by employing a turning vane assembly below the suction bell entrance to achieve a suitable flow pattern as illustrated in Fig. 11. This arrangement normally requires a deeper sump but the width ( W ) may be reduced to 1.50D or less resulting in reduced screen and construction costs. The following guidelines are offered with a turning vane assembly: 1. Dimensions A and A' should be equal.

2. Pump bell should be as close as possible to the level of the support beam bottom. 3. Dimension B should be as short as clearance permits. 4. Dimension W should be equal to the bell diameter plus the necessary clearance to allow for variations in structural and casting dimensions. 5. In order to prevent excessive velocity a t pump entrance, the suction bell should be 1D or greater above the sump bottom depending on pump size. 6. The turning vanes should slightly accelerate the flow to the pump (i.e. the inlet area of each passage should be greater than the corresponding exit ). 7. Intake tunnel velocity should be limited to 1to 2 ft/sec maximum. 8. Submergence "S" should be per submergence vs capacity chart Fig. 14, page 1-26.

HYDRAULICS Side intake -dry pit pumps

The following guidelines are offered for typical dry pit type pump arrangements as illustrated in Fig. 12 for a horizontal pump and Fig. 13 for a vertical centrifugal or scroll case type of pump. In these illustrations dimension "D" is the diameter, or effective diameter, of the suction intake fitting. 1. Submergence "S" should be approximately one foot for each foot per second a t "D." Velocity a t "D" should be less than 6 ft/sec. 2. Radius "R" should be as large as possible within structure

limitations. 3. Submergence can be reduced to half the values indicated in (1) with either a roof or vertical baffle. A vertical baffle should have ample depth to be effective and centrally located. At location D alternate shapes can be used to further reduce depth; i.e. rectangular or elliptical areas. Effective "D" then becomes the average diameter of the two axes. Always check NPSHR.

6D

SEPARATOR WALL FOR MULTIPLE PUMP INSTALLATIONS

-1

Fig. 12

SEPARATOR WALL

Fig. 13

1-25

INGERSOLL43AND


4. Suction bays should be symmetrical with no turn in the approach. With two or more pumps, separator walls extending for a length of 6D and a height "S" should be provided between the intakes of each pump. 5. Minimum water level must always be above the impeller eye. When the level is below the top of the volute priming is preferable. 6. Stop logs in the bay are preferred to a suction valve. If a butterfly valve is used, stem should be horizontal for horizontal double suction pumps and fully open when running. 7. Intake screens should be placed a minimum of 6D from the pump inlet ( D = diameter of suction intake fitting).

The above suggestions for alternative pump arrangements are offered as general guidelines and should not be considered as optimum. Analysis and design of intake structures and arrangement of pumps should only be made on the basis of experience together with model and field testing. If new or questionable arrangements are being proposed, model tests should be conducted. In most cases it is desirable to have the Manufacturer's comments before finalizing a design.

CAPACITY

( X 1000)

GPM

Fig. 14 Capacity Vs Submergence over suction bell for Vertical Wet Pit Pumps.

HYDRAULICS Work performed in pumping -horsepower

The work performed in pumping or moving a liquid depends on the weight of the liquid being handled in a given time against the total head (in feet of liquid) or differential pressure (in psi) being developed. Since one horsepower equals 33000 f t lb per minute the useful or theoretical horsepower (usually called the hydraulic horsepower -hyd hp ) will equal : Hyd hp = lb of liquid per minute X H (in feet) 33,000 The actual or brake horsepower (bhp) of a pump will be greater than the hyd hp by the amount of losses incurred within the pump through friction, leakage, etc. The pump efficiency will therefore be equal to: Pump efficiency = hyd hp bhp hyd hp Brake hp = pump efficiency Since the above expressions apply to both centrifugal and reciprocating types of pumps, horsepower calculations can be simplified if the weight of liquid being handled (capacity)is expressed in terms of gpm and/or bph-and the differential pressure ( H) in terms of head in feet of liquid for centrifugal pumps, and psi (pounds per sq in. ) for receiprocating pumps as follows :

(in feet) sp gr (common centrifugal terms) Brake hp = gpm 3960 x efficiency - bph

(in feet)xsp gr (common centrifugal terms ) 5657 x efficiency

-

gpm x psi (common reciprocating terms) 1714 x eff

-

bph psi (common reciprocating terms) 2450 x eff

Note: t o obtain the hyd hp from the above expressions use a pump efficiency of 100%.

INGERSOLLRAND CAMERON HYDRAULIC DATA In the above expressions: gpm = U S gallons per minute delivered (one gallon = 8.33 lb a t 68 Deg F. ) bph = barrels (42 gallons) per hour -delivered H = total head in feet of liquid-differential psi =lbs per sq in -differential Electrical hp input to motor =

Pump bhp motor efficiency

KW input to motor = pump bhp X 0.7457 mot or efficiency If a variable speed device is used between pump and driver then overall efficiency will equal Pump eff X Motor eff X eff of variable speed drive. From the above formulas it should be noted that it is important to correct the (gpm) and ( H ) for the temperature being pumped; it should also be noted that more power is required to pump a given weight of liquid hot against a given pressure than will be required to pump the same weight of liquid cold. When handling some liquids and for water a t very high pressures, the compressibility of the liquid may need to be considered as its density may change within the pump. Temperature rise -Minimum Flow :

Except for a small amount of power lost in the pump bearings and stuffing boxes the difference between the brake horsepower and hydraulic horsepower developed represents the power losses within the pump itself, most of which are transferred to the liquid passing through the pump causing a temperature rise in the liquid. It is sometimes desirable to have a curve showing temperature rise versus pump capacity -which can be calculated from this formula: The allowable minimum flow through a Centrifugal Pump may depend to some extent on the allowable temperature rise permitted. Since items other than thermal (such as hydraulic radial thrust) may have to be considered, the manufacturer should be consulted on the safe minimum flow permitted. where TR = Temperature rise in Deg F H = Total head in feet E = Efficiency expressed as a decimal

HYDRAULICS Characteristic curves

Since the head (in feet of liquid) developed by a centrifugal pump is independent of the specific gravity, water at normal temperatures with a specific gravity of 1.000 is the liquid almost universally used in establishing centrifugal pump performance characteristics. If the head for a specific application is determined in feet, then the desired head and capacity can be read without correction as long as the viscosity of the liquid is similar to that of water. The horsepower curve, which is basis specific gravity of 1.0, can be used for liquids of other gravity (if viscosity is similar to water) by multiplying the horsepower for water by the specific gravity of the liquid being handled. The hydraulic characteristics of centrifugal pumps usually permit considerable latitude in the range of operating conditions. Ideally, the design point and operating point should be maintained close to the best efficiency point ( B E P ) ;however, substantial variations in flow either to the right (increasing)or to the left (decreasing) of the BEP are usually permissible. However, operating back on the curve a t reduced flow, or at excessive run out may result in radial thrust, or cavitation causing damage and therefore the manufacturer should be consulted when such conditions may exist. Since a centrifugal pump is a machine which imparts velocity and converts velocity to pressure, the flow and head developed may be changed by varying the pump speed or changing the impeller diameter. These modifications will change the tip speed or velocity of the impeller vanes and therefore the velocity a t which the liquid leaves the impeller. Note that changing impeller diameters may result in a loss in efficiency as the diameter is reduced. For reasonable speed variations the efficiency should not change appreciably. For pumps in the centrifugal range of specific speeds (radial flow impellers) the relationships between capacity, head and horsepower with changes in impeller diameter and speed are approximately as follows : For small variations in impeller diameter (constant speed)

BHP,

Dl3

INGERSOLLRAND CAMERON HYDRAULIC DATA For variations in speed: (constant impeller diameter)

BHP, = S13 BHP,

S,3

where

D= Impeller diameters in inches H=Heads in feet QzCapacities in gpm S =Speeds in rpm BHP = Brake horsepowers Note: Subscript 1 is for original design conditions.

The above relationships are known as the Affinity Laws and are offered in this text with the understanding their application will be limited to centrifugal (radical flow) type pumps only. When other types such as axial, mixed flow or propeller type are involved consult the manufacturer for instructions. These laws can be summarized as follows: With variable speeds the capacity varies directly and the head varies as the square of the speed; efficiencies will not change for reasonable variations in speed. The break horsepower (BHP) varies as the cube of the speeds. With variable impeller diameters the capacity varies directly and the head varies as the square of the impeller diameter-efficiency will be reduced as the diameter is reduced-check manufacturer for limitations. The brake horsepower (BHP)varies as the cube of impeller diameters. Note: These relations hold only for small changes in impeller diameter. Stepping curves-Using the above relationships the head-capacity (HI-Q,) curves can be stepped up or down within reasonable limits making the necessary efficiency corrections for changes in impeller diameter. Solving for S, and D, to meet a specified H,-Q, is a cut and try operation if exact values are desired; in all cases the manufacturer should be consulted before making final modifications to the original design conditions.

I

HYDRAULICS System curves

A centrifugal pump always operates a t the intersection of its headcapacity curve and the system curve which shows the head required to make the liquid flow through the system of piping, valves, etc. The head in a typical system is made up of three components: 1.Static head 2. Pressure head 3. All losses; i.e. friction, entrance and exit losses

To illustrate, take a typical system shown in Fig. 15 where the total static head is 70 ft, the pressure head is 60 f t (2.31 X 26) and the friction head through all pipe, valves, fittings, entrance and exit losses in 18.9 f t a t the design flow of 1500 gpm, total system head a t design flow is 70 + 60 + 18.9 = 148.9 ft. In drawing the system curve (see Fig. 16, page 1-32) the static head will not change with flow so it is represented by the line AB, the pressure head will not change with flow so it is added to the static head and shown by the horizontal line'^^. The friction head through a piping system, however, varies approximately as the square of the flow so the friction a t 500 gpm will be X 18.9 = 2.1 f t (Point E); likewise the friction a t 1000 gpm will be 8.4 f t (Point F),

-

PRESSURE HEAD

26 PSlG

THROTTLE VALVE

J

H f =FRICTION HEAD

u

Fig. 15

INGERSOLL-RAND


HYDRAULICS

---

Water hammer

In fluid flow, water hammer can cause rupture and serious damage t o the entire piping system unless essential precautions are taken; in the case of condenser circulating water systems it can cause rupture and serious damage t o the tube sheets and water boxes. I t is the result of a rapid increase in pressure which occurs in a closed piping system when the liquid velocity is suddenly changed by sudden starting, stopping or change in speed of a pump; or sudden opening or closing of a valve which may change the liquid velocity in the system.

Elements of Graphical Solution of Water Hammer Problems in Centrifugal Pump Systems-A. J. Stepanoff 'Ikansactions of A.S.M.E. 71:515 (1949) Water Hammer Analysis- J. Parmakian Prentice Hall Publication, New York (1955) Reciprocating Pumps -Performance

The pressure on a reciprocating pump is determined by the maximum allowable plunger load and the area of the plunger: M

This increase, or dynamic change in pressure, is the result of the kinetic energy of the moving mass of liquid being transformed into pressure energy, resulting in an excessive pressure rise which can cause damage on either the suction or discharge side of the pump. Water hammer may be controlled by regulating valve closure time, surge chambers, relief valves or other means. Water hammer calculations are quite involved, and it is recommended that specialized engineering services be employed in cases where i t may be a problem. For information on this subject the following further references are suggested: Symposium on Water Hammer American Society of Mechanical Engineers 1933 (Reprinted 1949) Symposium on Water Hammer-Tkansactions A.S.M.E. 59:651(1937)

~psig ~ =. Max. Plunger Load Plunger area

The flow rate is determined by the area of the plunger, stroke length, the number of plungers, the pump speed, and Volumetric Efficiency: GPM = Plunger Area x Stroke Length x Number of Plungers x RPM x Volumetric Efficiency For a given pump size with stroke length, number of plungers, maximum RPM and maximum plunger load are constant; the maximum BHP is fixed. If the suction pressure is less than 10% of discharge pressure, the horsepower required is equal to the hydraulic horsepower divided by mechanical efficiency (M.E. ), as shown previously in the section titled Work Performed in Pumping Horsepower.

Water Hammer Control- S. L. Kerr Journal of American Water Works Assoc. 43:985 (December 1951)

When dealing with high suction pressure conditions (greater than 10% of discharge pressure), non-reversal of power end loading exists. Therefore, special pump selections are necessary. Generally the plunger rating is decreased reducing available rod load. In addition, the required input horsepower becomes the sum of the hydraulic and frictional horsepowers or:

Practical Aspects of Water Hammer-S. L. Kerr Journal of American Water Works Assoc. 40:599 (June 1948)

BHP = H.P.

+ F.H.P.

HYD H P = ( GPM ) ( Disch. Press.-Suction Press. ) 1714

INGERSOLLffAND

HYDRAULICS

CAMERON HYDRAULIC DATA FIGURE 1

FLOW VARIATION

F.H.P. =

(

, G P M ) . Press.) (

-

1

)

(I+

E:k",:IS

>1

DUPLEX DOUBLE ACTING VARIATION ABOVE MEAN - 24 1% VARIATION BELOW MEAN 21.50/b TOTALVARIATION-456%W

-

NOTE:

I I

Pump mechanical efficiency decreases with a decrease in rod load. Consult manufacturer for values.

Reciprocating Pumps Pulsation Analysis and System Piping hciprocating pumps produce flow variations which are converted into fluid pressure pulsations by the piping system. Dependent upon the design of the piping system this conversion can result in excessive pressure pulsations leading to piping vibration and fatigue failures, loss of fluid flow due to cavitation, or damage to pump components. However, the majority of these problems can be avoided if the piping system design incorporates pulsation analysis or evaluates the acoustic characteristics of the piping system. Typically, reciprocating pump systems are designed and built following standard industry practices. However, the interaction between the flow variation of the pump and the acoustic natural frequency of the piping is not addressed. Past experience has indicated excessive pulsation problems could occur if this interaction is ignored. As illustrated in Figure 1 flow variations can range from 23% for a triplex to only 2.2% for a nonuplex unit, three ( 3 )to nine ( 9 )plungers, respectively. Subsequently, these flow variations are converted into pressure pulsations by the piping system because the system pressure is generated by flow restrictions within the piping (i.e. friction effects, velocity head, flow through valves or orifice, etc.). Therefore, a varying flow will result in pressure variations or pulsations. However, whereas the flow variation for the pump can be easily predicted, the resultant pressure variations or pulsations are more difficult to determine due to the acoustic characteristics of the piping system. Figure 2 indicates how the flow variations are converted into pulsations a t distinct frequencies. These frequencies are directly related t o the number of plungers and pump speed. (f=NP/GO). In addition, test data confirms the peak amplitudes will occur at multiples of the primary or first order frequency. If the acoustic natural frequency of

u

DIAGRAMS FOR VARIOUS MULTIPLEX RECIPROCATING PUMPS SHOW VARIATION AT ALL POINTS FOR ONE REVOLUTION

1 1 1 I N/I I

I

.\hY

i

I I

TRIPLEX VARIATION ABOVE MEAN - 6.1% 16.9% VARIATION BELOW MEAN TOTAL VARIATION - 23.00/0

-

OUADRUPLEX VARIATION ABOVE MEAN - 11.OOh VARIATION BELOW MEAN - al.ssa TOTALVARIATION-32.5%W

1

,

1IY.M 1 I I

h W /I I I IY\.VI 1 I I N

QUINTUPLO( VARIATION ABOVE MEAN - 1.8% VARIATION BELOW MEAN 5.3C TOTAL VARIATION - 7 1%

-

SEXTUPLEX VARIATION ABOVE MEAN - 4.8% VARIATION BELOW MEAN TOTAL VARIATION - 14.0%

-

SEPTUPLEX VARIATION ABOVE MEAN 1.Z0h VARlAllON BELOW MEAN - 2.8% TOTAL VARIATION 4.0%

-

NONUPLEX .7% VARIATION ABOVE MEAN VARIATION BELOW MEAN - 1 5% TOTAL VARIATION

-

0"

24"

48'

72"

96" 120" 144" 168" 192" 216' 240' 264" 288" 312' 336' 360"

Fig. 1 Flow Variation

INGERSOLLRAND

CAMERON HYDRAULIC DATA TABLE 1

HYDRAULICS

A

Properties of Common Liquids At 68 F and 14.7 psia

HELMHOLTZ RESONATOR f

Density, lb/ft3

Liquid Pure Water Seawater Benzene Methanol E than01 Turpentine

62.3 63.9 54.8 49.3 49.3 54.2

Bulk Modulus 10"b/in2 318 (s) 344 ( s ) 222 ( s ) 144 ( s ) 155 ( s ) 223 ( s )

Acoustic Velocity ft/sec 4865 4993 4324 3678 3812 4363

-2

'-

2n

attenuate

1 fI

QUARTER WAVE STUB I*n f,

1) c

4L

A t 68' F and 200 psia

attenuate

Propane Isobutane N-butane

30.8 35.0 35.8

25 ( t ) 41 ( t )

53 ( t )

2000-2500 2200-2800 3100-3700

Note: The values listed are average. For higher temperatures or pressures obtain specific values.

t = isothermal bulk modulus s = isentropic bulk modulus

f2

fl

C SURGE VOLUME f

-5

' --

m

=

u

2L ~

~

/

d

attenuate

~

fI

From Engineering Dynamics Incorporated technical report, ED1 85305, Oct. 85.

f3

f2

attenuation Increases as m increases

D

Once determined, the acoustic frequency of the piping system has to be separated or removed from the excitation frequency generated by the pump's normal flow variation. vpically, pulsation dampeners or stabilizers are installed t o generate this separation. Pulsation suppression devices change the acoustic characteristics of the system.

HELMHOLTZ FILTER

I m

P

Unfortunately, one cannot indiscriminately install pulsation dampeners and expect reliable results. If the proper selection techniques are not followed, the addition of a dampener could increase system problems instead of reducing or eliminating them. Basically, there are four ( 4 )different types of styles of pulsation dampeners a s shown in Figure 4. Examining the attenuation characteristics of each type indicates the problems that can occur if the dampener is not married to the system properly.

=

~

~

"C . 2L, '

/

d -

p

"C 2L,

attenuate

~

passband frequency

attenuation increases as rn Increases

Fig. 4 Attenuation Characteristics of Acoustic Components

f3


HYDRAULICS

Low frequency pulsations ( 1-20 hz) are the most damaging, easily discovered and can be attenuated by gas-filled bladder type dampeners or gas-charged volume devices (Helmholtz Resonators Figure 4a). Higher frequency pulsations (20-300 hz) on the other hand are harder to discover and attenuate. Reduction of high frequency pulsations usually require a sophisticated pulsation device, Helmholtz Filter (figure 4d). In addition, an acoustic analysis using either analog or digital methods is required to identify the problem frequencies and determine the effectiveness of the selected dampener.

hvpa = vapor pressure of the fluid a t pumping temperature (psi)

INGERSOLLRAND

Net Positive Suction Head (NPSH) NPSH available for reciprocating pumps applications is calculated in the same manner as for centrifugal pumps, except an additional allowance must be made for the reciprocating action of the pump and the acoustic characteristics of the piping system. Qpically, this additional requirement is termed "acceleration head", or the pressure required to accelerate the liquid column on each stroke to prevent separation of this column in the pump or suction piping. If there is insufficient suction pressure t o meet the NPSH requirements of the pump, cavitation resulting in loss of volumetric efficiency may occur. In addition serious damage may occur t o plungers, valves, packing, and other pump components due to the force released during the collapse of the gas or vapor bubbles during cavitation. Approximation Method The following equation is beneficial for approximating the NPSH available within a system. However, this method of analysis begins t o lose validity if the length of the suction line exceeds 50 feet, simultaneous operation of more than two pumps, more than three ( 3 ) bends in suction line, or complex mixtures of fluids. In addition this simplified method of analysis doesn't address the acoustic interaction discussed previously. NPSH = hp

-

hvpa

hst - hfs

-

ha

where: hp = absolute pressure (psi) on the surface of the Liquid supply level. (Barometric pressure for open tanks or sump; Absolute pressure existing in closed tanks or systems.)

hst = static pressure developed by column of fluid above ( + ) or below ( - ) the centerline of the suction manifold (psi). hfs = suction line loss (psi) including entrance loss, friction loss, pressure drop across valves, filters, system components, etc. ha = LVnCSG 2.31Kg L = length of suction line (feet) V = Fluid Velocity in suction line (fps) n = Pump Speed (rpm) c = Constant for pump type = 200 for duplex single acting = .I15 duplex double acting = .066 triplex single or double acting = .040 Quintuplex single or double acting = .028 septuplex single or double acting = .022 nonuplex single or double acting K = Theoretical Fluid Factor representing the reciprocal of the fraction of theoretical acceleration head. (K=2.5 for hot oil; 2.0 most hydrocarbons; 1.5 amine, glycol, water; 1.4 deareated water, 1.0 urea and liquids with minimal entrained air. SG = specific gravity of fluid g = gravitational constant (32.2ft/sec2) Fkgarding cavitation, Figure 5 illustrates how pulsating pressure waves can result in cavitation if the amplitude of the negative pressure spike falls below the vapor pressure of the fluid. Figure 6 illustrates the magnitude of pressure spikes that may occur due to cavitation. I t is easy to see why cavitation results in damage to pump components after reviewing Figure 6. Therefore, the best method of insuring cavitation will not occur and system NPSH is accurately predicted is to perform an acoustic analysis. In summation, reciprocating pump piping systems built following standard design practices can develop pulsation related problems if

HYDRAULICS


INGERSOLLRAND

TRAVELING PULSATION WAVE

I

i

/-

POSITIVE PRESSURE

jw

LINE PRESSURE

L L

a

I

pi--

l li Pd Ps - P then cavltatlon w ~ loccur P, = ~ t a t l g ~ ~ r e s s u r e Pd - Dynam~cPulsal~ons,0 p PVp Vapo~Pressure

- ---\--L'-- - - LIQUID VAPOR PRESSURE \

I

I

VAPOR BUBBLES FORM AS NEGATIVE PULSE PASSES

**A-

*4

I

d,"ZOi

BUBBLES COLLAPSE AFTER NEGATIVE PRESSURE PULSE PASSES

DISTANCE ALONG PIPE

PS PD

=

80 PSIG P 1800 PSIG

WHEN NEGATIVE PRESSURE PULSATIONS EXCEED STATIC PRESSURE, CAVITATION OCCURS AND POSITIVE PRESSURE SPIKES RESULT.

Fig. 5 Acoustic Pulse Producing Local Cavitation in Liquid Filled Pipe

acoustics are ignored. These problems are normally the result of interaction between the flow variation characteristics of the pumps and the acoustic natural frequency of the piping system. The coincidence of the flow variation and acoustic frequency can result in extremely high pressure pulsations. If unattenuated, the pulsations can lead to cavitation, piping vibration, fatique failure of pipe elements, and possibly damage t o pump components. An acoustic analysis is required t o avoid these problems. Typically, acoustic analyses of piping systems are conducted via either electro-analog techniques or digital computer simulation. In either instance, this analysis is extremely complex, requiring the assistance of consultants or individuals experienced in this field. Previous experience has shown that systems built or modified to correct pulsation related problems utilizing the benefits of acoustic analysis operate reliably.

PLUNGER b2

262 RPM 400 PSliDlV 0 0 250 SEC F S 11 50 AM

12 10.83 PS PD

-

=

84 PSIG 1350 PSIG

Fig. 6 Cavitation of Liquids

Pump Drivers -speed torque curves

The driver must be capable of supplying more torque a t each successive speed from zero to full load than required by the pump in order to reach rated speed. This condition seldom presents any prob-

HYDRAULICS lem with the average centrifugal pump driven by standard induction or synchronous motors, but with certain applications such as with high specific speed pumps having high shut-off horsepower, or with reduced voltage starting, motors with high pull-in torque may be required.

wards. This complicates the speed torque cal~ul,~tion which should be referred to the pump manufacturer. Although torque is a function of the square of the speed in the case of centrifugal pumps, in the case of positive displacement pumps the torque is constant regardless of the speed, as long as the differential discharge pressure remains unchanged. Therefore, a general rule is the starting torque required for reciprocating pumps is approximately 125% of full load running - torque when starting under load, and approximately 25% full load running torque when starting without load.

Where centrifugal pumps in the low to medium specific speed range (under 3500) are started with the discharge valve closed the minimum torque requirements at various speeds for this condition are calculated as follows: Determine the maximum horsepower required a t rated speed under shut off conditions. Convert this horsepower to torque in (Ib. ft.) by using the formula: Tin(1b. f t . ) = 5250xhp rpm Torquevariesasthe squareof thespeed; therefore,toobtaintorqueat:

3/4 speed-multiply % speed-multiply 54 speed-multiply % speed-multiply

full speed torque by 0.563 full speed torque by 0.250 full speed torque by 0.063 full speed torque by 0.016

At zero speed the torque would theoretically be zero, but the driver must overcome stuffing box friction, rotating element inertia and bearing friction in order to start the shaft turning. This requires a torque a t zero speed of from 2%percent to 15 percent of the maximum. Speed torque requirements for starting conditions other than with closed discharge will vary depending on the horsepower requirements a t each successive speed. This can be determined by superimposing the pump H-Q curve on the system curve; selecting several speeds and calculating the horsepower a t each of the speeds selected; then calculating the torque for each speed selected. On vertical axial flow and propeller pumps with high specific speeds (and high shut off horsepower) it is standard practice to start the pumps with discharge valves partially open to reduce starting horsepower and thrust. In the case of the second of two pumps starting with the first already pumping, it is possible that the water may be flowing back through the discharge of the idle pump turning it back-

Engine drivers f; +

If reciprocating engine drivers are being considered the speedtorque requirements of the pump must be checked against the speed torque capabilities of the engine to assure their compatibility. Caution must be used in the selection of reciprocating engine drivers because excessive cyclic stresses may be superimposed on the pump shaft due to the periodic power impulses produced by each engine cylinder. These cyclic pulses produce a torsional vibration whose magnitude depends on the state of resonance of the entire system; this results in an increase in the cyclic tensile loading of the pump shaft. For these reasons the allowable pump shaft horsepower per 100 rpm (hp/100 rpm) limits must be reduced substantially. Due to the torsional vibration problems that may develop, the pump manufacturers should be checked to determine the suitability of the engine drive being considered. Impeller Profiles Values of Spec~fic Speeds.

,

-

7-7 r l 8

\

--.

-

Irnpellar

;__ , n u b Y,

Radial-Vane Arab

Franc,. V a n e Are.

Maxed F l o w Araa

Arnal F l o w Area

AX,s oq

Rotatton

Fig. 18 showing profiles of impeller designs ranging from the low specific speed radial flow design on the left to a high specific axial flow design on the right. (Courtesy of Hydraulic Institute.) 1-47

INGERSOLLUAND


I NS

HYDRAULICS

= 9 0 0 DOUBLE SUCT.

5 7 0 0 SINGLE SUCT.

CAPACITY

PER CENT

OF

NORMAL

Fig. 19 showing shape of typical head-capacity curves for various specific speeds.

-I

u

I

Q:

0 Z

SINOLE SUCT

Fig. 21 Values of IFJ' 0

25

50

CAPACITY

75

100

125

150

P E R CENT OF NORMAL

Fig. 20 showing shape of typical brake horsepower curves for various specific speeds.

INGERSOLLRAND


Fig. 22 Recommended maximum operating speeds for single suction pumps.

1-50

HYDRAULICS

Fig. 23 Recommended maximum operating speeds for double suction pumps.

1-51

INGERSOLLRAND

HYDRAULICS

CAMERON HYDRAULIC DATA BIBLIOGRAPHY

The following references are among those available if it is desired to investigate the subjects discussed herein in further detail: Crane Technical Paper No 410-Flow of Fluids through Valves, Fittings and Pipe. Crane Company. Advertising Division. 300 Park Avenue, New York, N.Y. 10022 Crane Technical Paper No. 41OM-Metric Edition-SI Units is now available; order from above address. (orders for Crane Papers must be prepaid) Hydraulic Institute Standards and Engineering Data Book- Address: Hydraulic Institute, 712 Lakewood Center North, Cleveland, Ohlo 43107.

The following are published by McGraw-Hill Inc.: Baumeister ant1 Marks-Standard Handbook for Mechanical Engineers. Chow-Handbook of Applied Hydrology. Hicks-Standard Handbook of Engineering Calculations. Kallen-Handhook of Inslrumerltation and Controls. King and Rrater-Handbook of Hydraulics. Merritt-Standard Handbook for Civil Engineers. Perry- Engineering Manual. Streeter-Handbook of Fluid Dynamics. Streeter and Wylie-Fluid Mechanics. TTrguhart - Civil Engineering Handhook. Karassik, Krutzsch, Fraser and Messina-Pump Handhook. Shames-Mechanics of Fluids.

The following a r e published by the Macmillan Publishing Company: Sahersky, Acosra and Hauptmann-Fluid

Flow.

The following a r e published by John Wiley & Sons: Stepanoff-Centrifugal and Axial E'low Pumps. Rouse-Engineering. Hydraulics. Vennard & Street-E:lementary Fluid L)ynamics

The following a r e published by Prentice Hall: NOTE: This chart has been constructed from test data obtained using the llqulds shown For applicability to other llqulds refer to the text

Fig. 24 NPSH reduction for pumps handling hydrocarbon liquids a n d high t e m p e r a t u r e water.

Binder-Fluid Mechanics. Albertson, Barton and Simons-Fluid Mechanics for Engineers Butterworth Publishers. 10 Tower Office Park Woburn, Ma. 01801 Telephone 1-617-933-8260

FORMULAS

2- 1

FORMULAS AND EQUIVALENTS


General-Information on Liquids i

\

!

:

1

In this section the more commonly used Formulas and Equivalents are included for the convenience of the user. With references to Volume and Weight Equivalents, the following mavitv. and ssecific weieht comments on t e m ~ e r a t u r e .ssecific " " should be of interest. J

CONTENTS OF SECTION 2

P

Page

Volume and weight equivalents

Flow equivalents

............................. 2-4 ............................ 2-5

...................................2-6 and 2-7

Flow through orifices and nozzles Flow data -nozzles Flow data-weirs

The Specific Gravity of a solid or liquid is the ratio of the mass of the body to the mass of an equal volume of water a t some selected base or standard temperature. Specific Gravity of Water is usually given a s 1.000 a t 60°F (15.6"C). However, in some cases, for convenience, it may be given as 1.000 at 68°F (20°C); and in other cases a s 1.000 a t 39.Z°F (4°C) which is its point of maximum density. Based on using water having a specific gravity of 1.000 a t 39.Z°F (4°C) a s a reference point, water a t 60°F (15.6"C) will have a specific gravity of 0.9991, and 0.9983 a t 68°F (20°C)- therefore, for practical applications which temperature (39.Z°F-60°F or 68°F) is selected a s a base for reference makes little difference. At the present time the base of 39.2"F (4°C) is commonly used by physicists, but the engineer usually uses 60°F (15.6"C) or 68°F (20°C) as a base. For actual specific gravities and specific weights of water for other temperatures to 705.47"F (374.15"C) see page 4-4.

. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2-3

Head and pressure equivalents..

. . . . . . . . . . . . . . . . . . . . . . . . . . .2-8

........................................ 2-9

Specific Gravities of Other Liquids is given relative to waterusually a t 60°F (15.6"C). Numerically, specific gravity is about the same a s the density in grams per cubic centimeter in the cgs system. Other systems of measuring specific gravity or density are related; conversion tables are shown on pages 4-6 to 4-19.

................................. 2-10 and 2-11

Irrigation table . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2-12 Frequently used formulas, constants and conversions . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .2-13 through 2-16

I.

I

(For metric formulas see page 8-28)

U '

Temperature affects the characteristics of a liquid. For most liquids an increase in temperature decreases viscosity, decreases specific gravity and increases volume (see page 1-6).

Selected Formulas and Equivalents General information on liquids

A

Specific Weight a s used in this discussion, is the weight in lb per cu ft. The specific weight of water a t 39.Z°F is 62.4258 lb per cu ft., a t 60°F is 62.3714 lb per cu ft; a t 68°F is 62.3208 lb per cu ft. For other temperatures proper specific weight values should be used (see page 4-4).

0

Density is the mass per unit volume. I t is usually stated in lb/ft", or g/cm3 or kg/m" For a detailed discussion see page 4-3.

';3

Volume & Weight Equivalents Example: 20 U S gallons x 3.7854 = 75.708 liters

6

Weight equivalent basis water at 60°F (15.6"C)

Volume and weight equivalents US gallons

Imperial gallons

Cubic inches

1

0.8327

231

0.13368

3.7854

0.0037854

8.338

0.00417

3.782

Imperial gallons . . . . . . . . . . . .

1.20094

1

277.39

0.16054

4.546

0.004546

10.0134

0.005

4.542

Cubic inches . . . . . . . . . . . . . . .

0.004329

0.003605

1

0.0005787

0.016387

0.000016387

0.036095

55409

0.016372

Cubic feet . . . . . . . . . . . . . . . . . .

7.48052

6.229

1728

1

28.31 7

0.02832

62.3714

0.031 19

28.291

Liters . . . . . . . . . . . . . . . . . . . . . .

0.2642

0.2200

61.024

0.035315

I

0.001

2.2029

0.001 1

0.1000

Cubic meters . . . . . . . . . . . . . . .

264.2

220.0

61024

35.315

1000

1

2202.65

1.10133

1000.0

Pounds* . . . . . . . . . . . . . . . . . . .

0.1 199

0.09987

27.71

0.016033

0.4539

,000454

1

0.0005

0.45359

U S gallons . . . . . . . . . . . . . . . .

Cubic feet

Cubic meters

Liters

p p p p

US tons

Pounds

Kilograms

'0.

ce,

,S rn

impeller diameter)

INGERSOLLUAND CAMERON HYDRAULIC DATA Miscellaneous Temperature equivalents:

Kelvin

0 Absolute zero .......... Water freezing point: (14.696psia 101.325 KPa) . . . . . . . . . . . . . . . . 273.15 Water boiling point: (14.696psia 101.325 KPa) . . . . . . . . . . . . . . . . 373.15

Degrees Celsius

Degrees Fahrenheit

273.15

- 459.67

491.67

0

32

671.67

100

212

Degrees Rankine

0

-

Celsius/Fahrenheit conversions:

Deg C Deg F

= =

5/9 (OF - 32) 9/5 OC + 32

Reynolds Number ( R ) : (see page 1-4)

V = Average velocity-ft/sec D = Average internal diameter-ft u = Kinematic viscosity of the fluid-ft2/sec (For pure fresh water a t 60°F v = 0.000 0 012 16 ft2/sec.) Dare y - Weisbach (see page 3-3)

Haxen and Williams (see page 3-7)

NOTE: For selected arithmetrical and geometrical formulas refer to page 7-3

--

I

I

-

\

I

SECTION Ill

-

FRICTION

A

1

LLRAND-

1

INGERSOLL-RAND CAMERON HYDRAULIC DATA Friction Losses in Pipe CONTENTS OF SECTION 3 Friction Data: Friction loss principles . . . . . . . . . . . . . . . . .

Page . . . . . . 3-3

Darcy-Weisbach Formula . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3-3 Hazen and Williams Formula . . . . . . . . . . . . . . . . . . . . . . . . . 3-7 Example-Head loss Calculation . . . . . . . . . . . . . . . . . 3-9 to 3-10 Moody diagram-Reynolds Nos. Versus Friction Factor Chart . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3-11 Friction of water in cast iron and steel pipe . . . . . . . . 3-12 to 3-34 Friction of water in copper tubing and brass pipe . . . 3-34 to 3-48 Friction of viscous liquids in pipes . . . . . . . . . . . . . . . 3-48 to 3-88

where

and fittings . . . . . . . . . . . . 3-122

h, = friction loss- ft of liquid L = pipe length -feet D = average inside diameter of pipe-feet V = average pipe velocity in ftisec g = gravitational constant (32.174 ft/sec2) f = friction factor-a dimensionless number which has been determined experimentally and for turbulent flow depends on the roughness of the pipe's interior surface and the Reynolds number (see page 3-5). For laminar (viscous) flow (Reynolds number below 2000) the roughness or condition of the pipe's interior surface has no effect (except a s i t affects the cross sectional area) and the friction factor (0 becomes:

Pages 3-103 through 3-109 are located in this section (following Paper Stock Friction Data) for convenience and ready reference.

For turbulent flow (Reynolds number above 4000) the friction factor is affected by both the roughness of the pipe's interior surface

Friction of paper stock in pipes . . . . . . . . . . . . . . . . .3-88 to 3-101 Friction of paper stock in fittings . . . . . . . . . .3-101 to 3-102 *General Information-Pulp and Paper Industry . . .3-103 to 3-110 Friction of water-valves and fittings . . . . . . . . . . .3-110 to 3-122 Friction of water-valves and fittings in terms equivalent length straight pipe . . . . . . . . . . . . . . . . . . . . . . .3-120 to 3-121 Friction-viscous liquids-valves

* NOTE:

The resistance to flow as a liquid is moved through a pipe results in a loss of head or pressure and is called friction (measured in feet of liquid). This resistance to flow is due to viscous shear stresses within the liquid and turbulence that occurs along the pipe walls due to roughness. The amount of head loss for a given system depends on the characteristics of the liquid being handled; i.e. viscosity, size of pipe, condition (roughness) of pipe's interior surface and length of travel; also loss through various valves, fittings, etc. (see page 3-110). A vast amount of research has been conducted to determine the amount of friction loss for different conditions, and various expressions based on experimental data have been developed for calculating friction loss. The expression most commonly used in present day practice and the one on which the tables in this book are based is the *Darcy-Weisbach equation. This formula recognizes that pipe friction is dependent on condition (roughness of pipe's interior surface), internal diameter of pipe, velocity of liquid and its viscosity. It is expressed as: - L V'

'

Also known as t h e Fanning Formula

INGERSOLLRAND


and the Reynolds Number and can be determined from an equation developed by C. F. Colebrook (1939); i.e. 1

--

-

-2 log,,

&j

+ .51j RVT

where

R

=

f

=

Reynold's Number

VD

=2'

Friction Factor E = Absolute Roughness-in feet-(See following table) D = Inside diameter of pipe-ft V = Average pipe velocity -ft/sec v = Kinematic Viscosity -ftz/sec Since the Colebrook equation is non-factorable in f, awkward and difficult to solve, the value of f may be obtained from a graph or chart developed by L. F. Moody (ASME 1944) and included herein on page 3-11. This graph shows the relation between the friction factor f, the Reynolds Number R, and the relative roughness clD, where is the absolute roughness in feet and D is the pipe diameter in feet; Note that for convenience the relative roughness is used in developing the graph on page 3-11. However, to avoid possible errors in reading the friction factor f from the Moody graph the friction loss data presented in the tables on pages 3-12 to 3-88 were calculated mathematically (programmed on a digital computer) basis the following assumptions: (a) Turbulent Flow -Reynolds Numbers above 2000 except as noted (see pages 1-4 and 1-5). (b) Absolute Roughness Parameters (€)-of 0.00015 for new clean steel pipe (schedules as listed) and 0.0004 for new asphalt dipped cast iron pipe; and 0.000005 for smooth copper tubing and brass pipe. (c) Water Friction-Pages 3-12 to 3-48 based on pure fresh water a t a temperature of 60°F (15.6 "C); Kinematic viscosity (v) = 0.000 012 16 ft2/sec (1.130 Centistokes.) It should be noted that since the viscosity of water can vary appreciably from 32°F to 212°F the friction can increase or decrease as much as 40% between the two temperature extremes. (d) Viscous Liquids-Friction -Pages 3-48 to 3-88, absolute roughness parameter of 0.00015 for new clean steel pipe-schedules as listed (see viscosity discussion page 4-23). For pipes with other absolute roughness parameters see the following table.

FRICTION

Type of pipe (new, clean, condition) Drawn tubing-glass, brass, plastic Commercial steel or wrought iron Cast iron -asphalt dipped Galvanized iron Cast iron -uncoated Wood stave Concrete Riveted steel

Absolute roughness" E (in feet) 0.000005 0.00015 0.0004 0.0005 0.00085 0.0006-0.0003 0.001-0.01 0.003-0.03

' Basis data from Hydraulic Institute Engineering Data Book.

To obtain friction loss in pipes having other roughness parameters, the applicable friction factor can be obtained from the Moody chart on page 3-11 and then, if desired, checked for accuracy with the Colebrook formula. In using the Moody chart on page 3-11 the relative roughness (€ID) is used where "E" is the absolute roughness in feet and "D" is the pipe diameter in feet. Friction losses for pipe sizes between those listed in the tables may be found with reasonable accuracy using a ratio of the fifth power of the diameters; thus Desired friction loss in pipe B dia A = Known friction loss in pipe A dia I3

(

Use of a general multiplier to correct the head loss shown in these tables to head loss for pipes of other roughness characteristics is not recommended, or safe; multipliers can be developed, but they would apply accurately to only one flow or capacity. Instead the best procedures to follow is to: Calculate the applicable Reynolds Number, select the applicable friction factor from the Moody Chart and use it in the Darcy formula to determine the head loss desired. The effect of aging and the allowances that should be made in estimating friction loss is beyond the scope of this discussion. I t will depend on the particular properties of the fluid being handled and its effect on the interior pipe surface; any safety factors to allow for this effect must be estimated for local conditions and the requirements of each particular installation. CAUTION-Since the friction loss data in the tables in this book are calculated on the basis of the roughness parameters for clean new pipe with no allowances for aging, manufacturing tolerances and other conditions which may cause variations of the interior pipe 3-5

FRICTION

INGERSOLL-RAND CAMERON HYDRAULIC DATA surfaces, it is suggested that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables. For a more detailed discussion of friction loss calculations and the various items that should be considered, reference is suggested to the Engineering Data Book of the Hydraulic Institute; also to Crane Technical Paper No. 410. See page 1-47 for bibliography. For convenient reference formulas used in connection with the Darcy-WeisbacWColebrook method are: Head Loss L V2

hf= f - - = D 2g

f

0.03112 L(gpmI2 d5

=

f

0.0153 L(bphjP d5

Friction Factor (f): (also see graph page 3-11.)

64 F o r R less than 2000 (laminar flow): f = R Reynolds Number:

R (water a t 60°F) =

2799.5(gpm) d

Velocity:

=

f- LV" 4m2g

g

acceleration of gravity, ft/sec2(taken as 32.174 ft/sec2 in making conversionsj. hf = head loss due to friction, ft of liquid r = absolute roughness in feet -see page 3-5 h, = Velocity head-ft of liquid =

k = kinematic viscosity, centistokes

z

=S

v = kinematic viscosity, -ft2/sec L = length of pipe including equivalent length for loss through fittings- ft flow area m = hydraulic radius = = ft wetted perimeter (use in calculating flow in open channels or unfilled pipes) p = density a t temp. and press. a t which liquid is flowing, lb/ft3 gpm = flow of liquid, gallons per minute. p = absolute or dynamic viscosity, lb-sec/ft2 V = velocity of flow, ft/sec s = density, glcm" (water at 4°C or 39.2"F = 1.000) z = absolute or dynamic viscosity-centipoises HAZEN AND WILLIAMS Although the Darcy-Weisbach/Colebrook method (on which the tables in this book are based) offers a rational mathematical solution to friction loss calculations (since it can be applied to any liquid except plastics and those carrying suspended solids) some engineers prefer to use one of the many empirical formulas that have been developed for water flowing under turbulent conditions. Of these, the most widely used and accepted is the Hazen and Williarn,~empirical formula since it is convenient to use and experience has shown that it produces reliable results. In a convenient form it reads:

Velocity Head:

SYMBOLS USED IN FORMULAS, PAGES 3-6 and 3-7 bph = flow of liquid, barrels (42 gal) per hour. d = inside diameter of circular pipe-inches C = Friction Factor for Hazen & Williams D = inside diameter of circular pipe-feet f = Darcy-Weisbach friction factor, dimensionless. 3- 6

This formula is basis a fluid having a kinematic viscosity, v = 0.000 012 16 ft2/sec(1.130 centistokes) or 31.5 SSU which is the case for water a t 60°F. But since the viscosity of water can vary appreciably from 32°F to 212OF t h e friction can decrease or increase a s much a s 40% between the two temperature extremes. However, this formula can be used for any liquid having a viscosity i n the range of 1.130 centistokes. Values of C for various types of pipe with suggested design values are given in the following table with corresponding multipliers that can be applied, when appropriate, to obtain approximate results. 3- 7

Hazen and Williams-Friction

Friction-head

Factor C** Values of C

Type of

I

pipe

RangeHlgh = best.

$ 7 Low poor =

1

Cement-Asbestos Flbre B~tumastlc-enamellined Iron or steel centrifugally applied Cement lined Iran or steel centrifugally applied

1

Average value . 8 , new PIP^

or corroded

Commonly

vA70r

deslgn purposes

160-140 -

150 150

140 140

160 130

148

140

-

150

140

Copper brass lead tln or glass pope and tublng

150-120

140

130

Wood-stave

145-110

120

110

Welded and seamless steel.. . . . . . . . Interior rlveted steel (no projecting rlvets). . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Wrought-1.0.. Cast-1.0. . . . . . . . . . . . . . . . . Tar-coated cast-lron . . . . . . . . . . . . . . . . . . . . . .

150-80

1

Glrth-r~vetedsteel (projecting rivets in girth .......................... seams only) ......................... Concrete. Full-riveted steel (projecting rivets in g ~ r t h and horizontal seams1 . . . . . . . . . . . V~trlf~ed. Splral-rlveted iteel (flow wlth lap)

I

Spiral-riveted steel (flow agalnst lap)

......

1

& ;&

:ii

1

152-85

-

I

130

11s

I

Problem-referring to the accompanying figure, page 3-10, a pump takes water (68°F) &om a sump and delivers it through 1250 feet of 4" diameter schedule 40 steel pipe. The suction pipe is 4" vertical 5 feet long and includes a foot valve and a long-radius elbow. The discharge line includes two standard 90 degree flanged elbows, a swing check valve and an open wedge-disc gate valve. I t is required to find the suction lift (hs) and the discharge head (h,) when the rate of flow is 200 gpm.

from table on page 3-20.

Velocity head

I

116

calculation:

To illustrate the application of the friction and head loss data in calculating the total system head for a specific system the following example is offered:

(a) SUCTION LIFT-Data

1

130 120

loss-sample

Solution

v2

= - = 0.395

ft

2g

100

90

60

60

Corrugated steel

................

ValuesofC..

.........

150

140

130

120

110

100

90

80

70

60

...

47

.54

.62

.71

.84

10

1 22

1.50

1 93

2.57

'Multiplier (Basis C = 100)

FRICTION


INGERSOLLRAND

' Multiplier to correct lrict~onloss tables (in prevlous ed~t~ons-14thEd~t~on and earlier), cannot be used with tables In thls book whlch are based on the Darcy-Weisbach-Colebrookformula. Note: the Hazen Willlams fr~ct~on factor "C" must not be confused wlth the Darcy-Weisbach-Colebrook frlction factor "f": these two frlctlon factors are not In any way related to each other.

Pipe friction loss h, = 2.25 ft per 100 f t of pipe. The resistance coefficient for the foot valve (page 3-115) is K = 1.3 and for the long-radius elbow (page 3-112) is K = 0.27.

The head loss due to pipe friction will be:

"

The head loss in the foot valve and long-radius elbow will be:

Total suction lift

(b)= (28.62 - 24.00) + 0.62 + 0.11 = 5.35 ft

(b) DISCHARGE HEAD-The 4" discharge line will be:

head loss due to pipe friction in the

INGERSOLLRAND

FRICTION


Friction Factors for Commercial Pipe

1-1

(for Darcy-Weisbach formula, page 3-3)

ELEV 2 8 9 0 0

Reldtive Roudllness

,, ,

O

D

O

N

O

Y

0

0

-

B

- 8 "

"

-

0"

O

=

1) . r

0 0 - -

688s

8

0 0 0 -

O

- -8 8 L

-

+

a cz D

0 .

A L L P I P E 1s NEW I-INCH

7'

\FOOT

STD.

STEEL-SCHEDULE

a0

VALVE

The resistance coefficient for the various fittings as obtained from the tables will be: Standard 90 degree flanged elbow (pg. 3-112) Swing check valve (pg. 3-115) Wedge-disc gate valve (pg. 8-111) Sudden enlargement (pg. 3-116 to 3-118) The total resistance coefficient for the fittings on the discharge side and sudden enlargement at exit will be: K = 2 x 0.51 + 1.70 + 0.14 + 1.0 = 3.86 Therefore the head loss due to the fittings on the discharge side and sudden enlargement will be:

-

The total discharge head (h,) will be:

cz

-

Total system head (H) = h, + h, = 290 + 5.35 = 295 ft Add a reasonable safety factor to allow for any abnormal condition of pipe's interior or surface (see page 3-5).

d

m

9

-

"

-

9

C

I , q

-

r

i lfoorly (liagrarn

cz

rn F .

,

Y

-

a

"7 4

c3

--

s

0

'=2

g

g

F r ~ c t ~ o nFactor

5th i.il C o p y n ~ h t 1971 by Mctiraa-H111 Book C i # m p a n > . N e r Yark) Sote: Chart shows relation of 1,elatlvr t.ooghnra.i~-dl) whi.t.r r i s a t w ~ l u t rrlnighnr,~in f ~ r am1 l 1) ~-;,liarnrtet.in feet.

(V 1. Strretrr "1.'1,11il.lIerhantrc

"


INGERSOLLRAND

Friction of Water

FRICTION

New Steel Pipe

Friction of Water

(Based on Darcy's Formula)

New Steel Pipe (Continued)

(Based on Darcy's Formula) '/a lnch

1/4 lnch Standard wt steel-sch

40

Extra strong steel-sch

.622"inside d ~ a Flow US gal per mln

Veloc~ty fl per sec

Veloclty head ft

Head loss ll per 100 n

Veloclty I t per sec .96 1.37 2.06 2.74 3.43

.01 .03 .07 12 18

1.39 2.58 5.34 9.02 13.6

1 90 2 85 3 80 4.74

056 126 224 349

3.0 3.5 4.0 45 5.0

3 17 3.70 4 22 475 5.28

,156 ,212 ,277 351 433

9.94 13.2 17.0 21.1 25.8

4.11 4.80 5.48 6.1 7 6.86

.26 .36 .47 .59 .73

19.1 25.5 32.7 40.9 50.0

5.69 6.64 7.59 8.54 9.49

503 ,684 ,894 1.13 1 40

5.5 6.0 6.5 7.0 7.5

5.81 6.34 6.86 7.39 7.92

,524 ,624 ,732 849 975

30.9 36.4 42.4 48.8 55.6

7.54 8 23 8 91 9.60 10.3

.88 1.05 1.23 1.43 1.6

59.9 70.7 82.4 95.0 109

10.44 11.38 12.33 13 28 1423

8.0 8.5 9.0 9.5 10

8.45 8.98 9.50 10.03 10 56

1 109 1 25 1 40 1.56 1 73

63.0 70.7 78.9 87.6 96.6

11.0 11.6 12.3 13.0 13.7

1.9 21 24 2.6 2.9

123 138 154 171 189

.

Flow

US gal per mln

0.423 inside dia

0.493" inside dia Velocity ft per sec

Velocity hkad-ft

Head loss ft per 100 ft

Velocity ft per sec

Velocity head-ft

Head loss ft per l 0 O A

Calculations on pages 3-12 to 3-34 are by Ingersoll-Rand Co Note No allowance has been made for age, dlfference In dlarneter, or any abnormal c o n d ~ t ~ oofn Interlor surface Any factor of safety must be est~matedfrom the local condltlons and the requirements of each particular lnstallat~on It 1s recommended that for most cornmerclal des~gnpurposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5

Flow US gal per m~n

Velocity ft per sec

Velocity head ft

Veloc~ty ft per sec 1.11 1.48 1.86 2.23 2.60

1.68 5.73 12.0 20.3 30.8 43.5 58.2 75.0 94.0 115 138 163 190 220

1.69 2.01 2.36 2.74 314

lnch


80

Steel-schedule

Veloc~ty head ft

160

,612'inslde dla

,742"inslde d ~ a

Head loss n per 100 R

Head loss ft per 100 n

Velocity head ft

0.74 1.86 2.82 4.73 7.10

,824"inslde d ~ a

80

Veloclty ft per sec

,008 017 ,039 069 108

Standard wt steel-s~h 40


Veloc~ty head ft

0.739 1.056 1.58 2.11 2.64

% lnch 40

464"lnside dia

Head loss f l per 100 n

0.7 1.0 1.5 2.0 2.5

Y4

Standard wt steel-sch

Schedule 160

80

546"lnslde d ~ a

Head loss flper 100 n

Veloclty ft per sec

Velocity head fl

Head loss n per

loon

1.19 1.99 2.97 4.14 5.48

1.64 2.18 2.73 3 27 3.82

042 074 115 166 226

3.05 5.12 7.70 10.8 14.3

295 374 462 .665 ,905

18.4 22.9 28.0 39.5 53.0

1.5 2.0 2.5 3.0 3.5

0.90 1.20 1.50 1.81 2.11

013 023 .035 ,051 ,069

0.72 1.19 1.78 2.47 3.26

4.0 4.5 5.0 6

7

2 41 271 3.01 3 61 4.21

,090 ,114 ,141 ,203 ,276

4.16 5.17 6.28 8.80 11.7

2.97 3 34 3.71 4 45 5 20

.I4 .17 ' 2 1 .31 .42

7.01 6.72 10.6 14.9 19.9

4.36 4.91 5.45 6.54 7.64

8 9 10 11 12

4.81 5.42 6.02 6 62 7 22

360 456 563 681 722

15.1 18.8 23.0 27.6 32.5

5.94 6 68 7 42 8 17 8 91

55 69 86 1 04 1.23

25.6 32.1 39.2 47.0 55.5

8 73 9.82 10.91 12.00 13.09

1 18 1 50 185 2 23 2.66

68.4 85.8 105 126 149

13 14 16 18 20

7.82 8.42 9.63 10.8 12.0

,951 1 103 1.44 1.82 2.25

37.9 43.7 56.4 70.8 86.8

9.63 10.4 11.9 13.4 14.8

1.44 17 22 2.8 3.4

64.8 74.7 96.7 121 149

14 18 15.27 17.45

3.13 3.62 473

175 202 261

02 03 .05 .08 .ll

Note- No allowance has been made for age, dlfference In d~ameter,or any abnormal cond~tionof interior surface. Any factor of safety must be est~matedfrom the local conditions and the requirements of each part~cularinstallation It Is recommended that for most commercial des~gnpurposes a Safety factor of 15 to 20% be added to the values In the tables-see page 3-5.


INGERSOLLRAND

Friction of Water


Friction of Water

1YZ lnch

1 lnch Standard wt steel-sch

40


1 049"lnslde dla Flow US gal per mln

Veloclty ft per sec

Velocity head ft

2 3 4 5 6

0 74 111 1 48 1 86 2 23

009 019 034 ,054 077

8 10 12 14 16

2 97 371 4 45 5.20 594

,137 ,214 ,308 ,420 548

18 20 22 24 26

668 7 42 8 17 891 9.65

694 857 1 036 1.23 1.45

28 30 35 40 45

10 39 111 13 0 14.8 16 7

1 68 193 2 62 3 43 4.33

80

,385 ,787 1.270 1.90 2.65

Veloclty flper sec

.O1 03 05 .08 .ll

3 57 4 46 5 36 6 25 7 14

.20 31 45 .61 .79

20.6 25.2 30.3 35.8 41.7

8.03 8.92 9.82 10.7 11.6

1 00 124 1 50 1.8 2.1

48.1 55.0 74.1 96.1 121 ;

12.5 13.4 15.6 17.9 20 1

2.4 2.8 3.8 50 6.3

4.50 6.81 9.58 12.8 16.5

Head loss fl per 100 fl ,599 1.19 1.99 2.99 4.17

Veloc~ty 11 per sec

Head loss tt per 10011

Velocity head ft

1 23 185 2 46 3 08 3 69

023 053 094 147 211

7.11 10.8 15.2 20.4 26.3

4.92 6.15 7.38 8.61 9.84

376 ,587 845 1 15 1 50

32.9 40.3 48.4 57.2 66.8

11 07 12 30 13.53 14 76 1599

1.26 2.60 4.40 6.63 9.30 15.9 24.3 34.4 46.2 59.7

1.90 2.35 2.84 3.38 3.97

74.9 91.8 110 131 153

77.1 88.2 119 154 194

1% lnch Standard wt steel-sch Flow US gal per mln

40


1.380'1nsdedla

80

Schedule 160-steel

1 278" i n s ~ d ed ~ a

1 160"inslde dia

Veloc~ty head ft

Head loss tt per 100R

.858 1073 1 29 1 50 1 72

.Oil 018 .026 .035 ,046

.35 .52 .72 / .95 1.20

1.00 1 25 1 50 1 75 2 00

015 024 034 048 062

.51 .75 1.04 1.33 1.69

1.21 1 52 1 82 213 2 43

023 .036 .051 070 092

10 12 14 16 18

215 257 300 3.43 386

072 103 140 183 232

1.74 2.45 3.24 4.15 5.17

2 50 3.00 3.50 4.00 4.50

097 140 190 249 315

2.55 3.57 4.75 6.10 7.61

3 04 3 64 4.25 4 86 5 46

143 ,206 280 366 463

20 25 30 35 40

4 29 5 36 6.44 7.51 8 58

286 431 644 876 1 14

6.31 9.61 13.6 18.2 23.5

5 00 6 25 7 50 8 75 10.0

388 607 874 1 19 1 55

9.28 14.2 20.1 27.0 34.9

6 07 7 59 9.11 10.63 12.14

572 894 1 29 1 75 2 29

125 150 17.5 20 0 22 5

243 350 4 76 6.21 786

4 5 6 7 8

50 60 70 80 90

Veloclty ft per sec

107 129 15.0 17.2 193

179 257 3.50 453 5.79

36.2 51.5 69.5 90.2 114

Veloclty ft per sec

Veloc~ty head It

Head loss R per 100 ll

53.7 76.5 103 134 168

Veloc~ty ft per sec

15.18 1822 2125 24 29 27.32

Veloclty head ft

358 515 701 9 16 11 59

Head loss ll per 100

n

,806 1.20 1.61 2.1 4 2.73 4.12 5.78 7.72 9.92 12.4 15.1 23.2 32.9 44.2 57.3 88.3 126 170 221 279

Note No allowance has been made for age dlfference ~n d~ameter,or any abnormal c o n d ~ t ~ oofn Interlor surface Any factor of safety must be estlmated from the local cond~tlonsand the requlrements of each particular lnstallatlon It IS recommended that for most commercial desdgn purposes a safety factor of 15 to 20% be added to the values In the tables-see page 3-5

3-14

40


Flow US gal per rn~n

Velocity tt per sec

Veloclty head ft

80

Schedule 160-steel 1.338" lnside dla

1.500"1ns1dedla

1.610"lnslde dla

,815"lnslde dla

Veloc~ty head ft

89 1 34 1 79 2 23 2 68


Schedule 160 steel

957"lnslde dla Head loss ll per 100 fl




Head loss ll per 100

n

Veloclty flper sec

Velocity head ft

Head loes I t per roo

n

Velocity I t per sec

Velocity head tt

Heed Ions ti per 100 1

4 5 6 7 8

63 .79 .95 1.10 1.26

006 010 ,014 019 025

,166 ,246 .340 ,447 ,567

33 .91 1.09 1 27 1.45

.01 01 02 03 03

,233 ,346 ,478 .630 .800

,913 1.14 1.37 1.60 1.83

.013 ,020 ,029 ,040 ,052

.404 ,601 ,832 1.10 1.35

9 10 12 14 16

1 42 1.58 1.89 2.21 2.52

,031 ,039 ,056 076 ,099

,701 ,848 1.18 1.51 1.93

1.63 1.82 2.18 2.54 2.90

.04 .05 .07 .I0 .13

,990 1.20 1.61 2.14 2.74

2 05 2 28 2.74 3.20 3 65

065 081 116 .I58 207

1.67 2.03 2.84 3.78 4.85

18 20 22 24 26

2.84 3.15 3.47 3.78 4.10

,125 ,154 .I87 .222 ,261

2.40 2.92 3.48 4.10 4.76

3 27 3.63 3.99 4.36 4.72

17 20 25 .30 .35

3.41 4.15 4.96 5.84 6.80

4.1 1 4.56 5.02 5.48 5.93

,262 ,323 391 ,465 ,546

6.04 7.36 8.81 10.4 12.1

26 30 32 34 36

4.41 4.73 5.04 5.36 5.67

,303 ,347 ,395 ,446 .500

5.47 6.23 7.04 7.90 8.80

5.08 5.45 5.81 6.17 6.54

.40 .46 .52 .59 66

7.82 8.91 10.1 11.3 12.6

6.39 6.85 7.30 7.76 8.22

,634 727 ,828 ,934 1.05

13.9 15.9 18.0 20.2 22.5

38 40 42 44 46

5.99 6.30 6.62 6.93 7.25

577 .618 681 ,747 ,817

9.76 10.8 11.8 12.9 14.0

6 90 7 26 7.99 63 8.35

74 82 .SO .99 1.08

14.0 15.4 16.9 18.5 20.1

8.67 9.13 9.58 10.04 10.50

1 17 1.29 1.43 1.57 1.71

25.0 27.6 30.3 33.1 36.1

48 50 55 60 65

7.56 7.88 8.67 9.46 10.24

,889 965 1.17 1.39 1.63

15.2 16.5 19.8 23.4 27.3

8.72 9.08 9.99 10.9 11.8

1.18 1.28 1.55 1.8 2.2

21.8 23.6 28.4 33.6 39.2

10.95 11.41 12.55 13.69 14.83

1.86 2.02 2.45 2.91 3.41

39.2 42.4 51.0 60.4 70.6

70 75 80 85 90

11.03 11.8 12.6 13.4 14.2

1.89 217 2.47 2 79 3.13

31.5 36.0 40.8 45.9 51.3

12.7 136 14.5 15.4 16.3

2.5 29 3.3 3.7 4.1

45.3 51.8 58.7 66.0 73.8

15.97 17.11 18.25 19.40 20.54

3 96 4 55 5.17 5 84 6.55

81.5 93.2 106 119 133

95 1M) 110 120 130

15.0 15.8 17.3 18.9 20 5

3 48 3.86 4 67 5 56 6.52

57.0 63.0 75.8 89.9 105

17.2 18 2 20.0 21.8 23.6

46 5.1 6.2 74 87

82.0 90.7 109.3 129.6 151.6

21.68 22.82 25.10 27.38 2966

7.29 8.08 9.78 11.6 13.7

148 164 197 234 274

140 150 160 170 180

22.1 23.6 25.2 268 284

7.56 8.68 9.88 11.15 1250

122 139 158 178 199

25.4 27.2 29.0 309 327

10.0 11.5 13.1 148 16.6

175 201 228 257 288

Note No allowance has been made for age dlfference In d~ameter or any abnorrnal c o n d ~ t ~ oOfn lnterlor surface Any factor of safety must be estlmated from the local condlt~onsand the requlrements of each parllcular lnstallat~on It IS recommended that for most commerc~ald e s ~ g npurposes a safety factor of 15 to 2090 be added to the values In the tables-see page 3-5

INGERS0LLQ;IAND CAMERON HYDRAULIC DATA Friction of Water

1



2 lnch Standard wt Steel-sch

40

Veloclty head ft

80

Schedule 160-steel

1.939'1nsldedla

Head loss R per

Veloc~ty 11 per sec

loon

Veloclty head

ft

1.687 lns~ded ~ a Head loss fi per 100 ft

Veloc~ty ft per sec

Veloc~ty head ft

Head loss fiper

100 ft

5 6 7 8 9

478 574 .669 765 .860

004 005 007 009 012

,074 ,102 ,134 -170 ,209

54 65 76 87 98

00 01 01 01 01

.I01 .I39 .I82 .231 .285

718 861 101 1 15 1 29

006 01 2 016 020 026

,197 ,271 ,357 ,452 ,559

10 12 14 16 18

.956 115 134 1.53 172

014 021 028 036 046

.252 ,349 461 ,586 ,725

1.09 1.30 1.52 1.74 1.96

02 03 .04 05 06

343 .476 .629 .800 ,991

1 44 1.72 2 01 2.30 2.58

032 .046 ,063 .062 .I04

,675 ,938 1.20 1.53 1.90

20 22 24 28 28

1.91 210 2.29 2.49 2.68

,057 069 082 096 111

,878 1.05 1.18 1.37 1.57

2 17 2 39 2 61 2 83 3.04

07 .09 .I1 .12 14

1.16 1.38 1.62 1.88 2.16

2 87 3 16 3.45 3.73 4.02

128 ,155 ,184 216 ,251

2.31 2.76 3.25 3.77 4.33

30 35 40 45 50

2 87 3 35 3.82 4 30 4.78

128 174 227 288 355

1.82 2.38 3.06 3.82 4.66

3.26 3.80 4 35 4 89 5 43

.17 .22 29 37 48

2.46 3.28 4.21 5.26 6.42

4.31 5.02 5.74 6.46 7.18

288 392 512 648 799

4.93 6.59 8.49 10.6 13.0

55 60 65 70 75

5 26 5 74 6.21 6.69 7.17

430 511 800 696 799

5.58 6.58 7.66 8.82 10.1

598 6 52 7.06 7 61 8 15

56 .66 77 90 1 03

7.70 9.09 10.59 12.2 13.9

7.89 8.61 9.33 10.05 10 77

.967 1.15 135 1.57 180

15.6 18.4 21.5 24.8 28.3

80 85 90' 95 100

7 65 8.13 8.60 9.08 9.56

909 1 03 1 15 1 28 1.42

11.4 12.8 14.3 15.9 17.5

8.69 9.03 9 78 10 3 10 9

1.17 1.27 1.49 16 1 8

15.8 17.7 19.8 22.0 24.3

11.48 12 20 12.92 13.64 14.35

2 05 2 31 2 59 2 89 3.20

32.1 36.1 40.3 44.8 49.5

110 120 130 140 150

10.52 11.5 12.4 13.4 143

172 2.05 2 40 2 78 3.20

21.0 24.9 29.1 33.6 38.4

12.0 13.0 14.1 15.2 16.3

2.2 2.6 3.1 36 4.1

29.2 34.5 40.3 46.6 53.3

15.79 17.22 18 66 20.10 21 53

3.87 4.61 5 40 6.27 7.20

59.6 70.6 82.6 95.5 109

160 170 180 190 200

153 16.3 172 182 19.1

364 411 4 60 5 13 5.68

43.5 49.0 54.8 60.9 67.3

17 4 18 5 19 6 20 6 21 7

47 53 60 6.6 73

60.5 68.1 76.1 84.6 93.6

22.97 24.40 2584 27 27 28 71

8.19 9 24 1036 11 54 12.79

220 240 260 280 300

21.0 22 9 24.9 26.8 287

688 8 18 960 1 1 14 128

81.1 96.2 113 130 149

239 26 9 283 304 326

89 10.6 124 144 165

j



2% lnch


2.067"tns~de d~a Flo~ US Veloclty gal fi per per mln sec

Friction of Water

124 140 156 174 192

113 134 157 181 208

Note No allowance has been made for age, d~fferenceIn dlameter or any abnormal c o n d ~ t ~ oof n ~nter~or Surface Any factor of safety must be estlmated from the local condltlons and the requ~rementsof each partlcular installat~on It IS recommended that for most commercial deslgn purposes a safety factor of 15 to 20% be added to the values In the tables-see page 3-5

n lnterlor Note No allowance has been made for age, dlfference In d~ameter or any abnormal c o n d ~ t ~ oof surface Any factor af safety must be estlmated from the local c o n d ~ t ~ o nand s the requirements of each partlcular Installallon It IS recommended that for most commerc~aldeslgn purposes a safety factor of 15 to 209b be added to the values In the tables-see page 3-5

FRICTION

CAMERON HYDRAULIC DATA Asphalt-dipped Cast lron and New Steel Pipe (Based on Darcy's Formula) (Continued)

Friction of Water

Friction of Water

Asphalt-dipped Cast lron and New Steel Pipe (Based on Darcy's Formula) (Continued) 3% lnch

3 lnch Std wt steel sch 40

Extra strong steel sch 80

3.068" i n s ~ d edla

2 . 9 0 0 inslde dla

Asphalt-d~pped cast ~ r o n ~

3.0" lnside dla Flow US gal per min

Veloclty ft per sec

Velocity head ft

Head loss R per 100 R

Velocity ft per sec

Velocity head ft


Veloclty ft per sec

10 15 20 25 30

.454 .681 ,908 1.13 1.36

.OO -01 .01 .02 .03

.042 .088 ,149 -225 .316

,434 ,651 ,868 1.09 1.30

,003 ,007 ,012 .018 .026

.038 .077 .I29 .I92 ,267

.49 .73 .97 1.21 1.45

.OO .O1 .02 .02 .03

35 40 45 50 55

1.59 1.82 2.04 2.27 2.50

.04 .05 .06 .08 .10

.421 .541 .676 .825 .990

1.52 1.74 1.95 2.17 2.39

036 .047 -059 -073 ,089

.353 .449 .557 ,676 .776

1.70 1.94 2.18 2.43 2.67

60 65 70 75 80

2.72 2.95 3.18 3.40 3.63

.12 .14 .16 .18 .21

1.17 1.36 1.57 1.79 2.03

2.60 2.82 3.04 3.25 347

,105 ,124 ,143 .I65 .I87

.912 1.06 1.22 1.38 1.56

85 90 95 100 110

3.86 4.08 4.31 4.54 4.99

.23 .26 .29 .32 .39

2.28 2.55 2.83 3.12 3.75

3.69 3.91 4.12 4.34 4.77

,211 .237 .264 .293 -354

120 130 140 150 160

5.45 5.90 6.35 6.81 7.26

.46 .54 .63 .72 .82

4.45 5.19 6.00 6.87 7.79

5.21 5.64 6.08 6.51 6.94

180 200 220 240 260

8.17 9.08 9.98 10.9 11.8

1.04 1.28 1.55 1.84 2.16

9.81 12.1 14.5 17.3 20.2

7.81 8.68 9.55 10.4 11.3

1

1

1

1

1

Head Vel o c ~ t y loss R per head ft 100 H

2.624 ~ n s l d ed ~ a Head IOSS R per

Velocity ft per sec

Veloclty head ft

.050 .I01 .I69 .253 .351

,593 ,890 1.19 1.48 1.78

,005 ,012 .022 .034 .049

.080 .I64 .275 .411 .572

.04 .06 .07 .09 .ll

.464 .592 .734 360 1.03

2.08 2.37 2.67 2.97 3.26

.067 -087 ,111 ,137 ,165

.757 .933 1.16 1.41 1.69

2.91 3.16 3.40 3.64 3.88

13 .15 .18 .21 .23

1.21 1.40 1.61 1.83 2.07

3.56 3.86 4.15 4.45 4.75

-197 ,231 ,268 ,307 ,350

1.99 2.31 2.65 3.02 3.41

1.75 1.95 2.16 2.37 2.84

4.12 4.37 4.61 4.85 5.33

.26 .29 .33 .36 .44

2.31 2.58 2.86 3.15 3.77

5.04 5.34 5.63 5.93 6.53

,395 .443 ,493 ,546 .661

3.83 4.27 4.73 5.21 6.25

.421 ,495 .574 .659 .749

3.35 3.90 4.50

5.81 6.30 6.79

5.80

7.76

.52 .62 .71 .82 .93

4.45 5.19 5.98 6.82 7.72

7.12 7.71 8.31 8.90 9.49

.787 .923 1.07 1.23 1.40

7.38 8.61 9.92 11.3 12.8

-948 1.17 1.42 1.69 1.98

7.27 8.90 10.7 12.7 14.8

8.72 9.70 10.7 11.6 12.6

1.01 9.68 10.68 11.87 1.46 11.86 1.78 14.26 13.05 14.24 2.07 16.88 2.46 119.71 1 1 5 . 4 3

1.77 2.19 2.64 3.15 3.69

16.1 19.8 23.8 28.2 32.9

5.13.'7.28

1

1

1

Asphalt-dlpped cast iron

Std wt steel sch 40


3.5" inside dia

3.548" inside dia

3.364" i n s ~ d edia

Schedule 160-steel

1

100 tl

1

38.0 43.5 49.4 55.6 62.2

280 300 320 340 360

12.7 13.6 14.5 15.4 16.3

2.51 2.88 3.28 3.70 4.15

23.4 26.8 30.4 34.3 38.4

12.2 13.0 13.9 14.8 15.6

2.29 2.63 3.00 3.38 3.79

17.1 19.5 22.1 24.9 27.8

13.6 14.5 15.5 16.5 17.5

2.88 3.26 3.77 4.22 473

22.77 26.04 29.53 33.24 37.16

16.61 17.80 18.99 20.17 21.36

4.28 4.92 5.59 6.32 7.08

380 400 420 440 460

17.2 18.2 19.1 20.0 20.9

4.62 5.12 5.65 6.20 6.77

42.7 47.3 52.1 57.1 62.4

16.5 17.4 18.2 19.1 20.0

4.23 4.68 5.16 5.67 6.19

30.9 34.2 37.6 41.2 44.9

18.4 19.4 20.4 21.4 22.3

5.27 5.81 6.43 7.13 7.75

41.31 45.67 50.25 55.05 60.06

22.55 23.73 24.92 26.11 27.29

7.89 8.74 9.64 10.58 11.56

69.2 76.5 84.2 92.2 101

480 500 550 600 650

21.8 22.7 25.0 27.2 29.5

7.38 8.00 9.68 11.5 13.5

67.9 73.6 88.9 106 124

20.8 21.7 23.9 26.0 28.2

6.74 7.32 8.85 10.5 12.4

48.8 52.9 63.8 75.7 88.6

23.3 24.2 26.7 29.1 31.6

8.37 9.15 11.1 13.1 15.5

65.30 70.75 85.33 101 119

28.48 29.66 32.63 35.60 38.56

12.59 13.66 16.53 19.67 23.08

109 119 143 170 199

Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

Flow US gal per mln

Velocity ft per sec

Veloclty head ft

15 20 25 30

.500 ,667 ,834 1.000

,004 ,007 ,011 ,016

Head loss R per

100fl

Velocity ft per sec

Velocity head ft


,043 .070 .lo5 .I46

.487 ,649 ,811 .974

-004 ,007 ,010 .015 -020

.038 ,064 .095 .I32 .I74

.54 72 -90 1.08 1.26

.OO .01 .01 -02 02

.050 -083 1 23 .I71 .225

.026 .033 041 ,059 080

.221 .274 332 .463 -614

1.44 1.63 1.80 2.17 2 53

.03 .04 .05 .07 .lo

.430 .601 .769

.379 .535 .717

1.62 1.95 2.27

Velocity ft per sec

Velocity head ft


Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It is recommended that for most commercial deslgn purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5

CAMERON HYDRAULIC DATA Friction of Water

Asphalt-dipped Cast Iron and New Steel Pipe

Friction of Water ' ~ e wSteel Pipe (Continued)


5 lnch

Asphalt-dipped cast iron

Std wt steel sch 40


Schedule 160-steel


4.0" inside dia

4 . 0 2 6 inside dia

3.826" inside dia

3.438" inside dia

5.047" inside dia

Flow US gal per mln

Velocity ft per sec

Velocity head ft

Head loss ft per

20 30 40

511 .766 1.02

,004 ,009 -016

.038 .076 128

50 60


(Continued)

4 Inch

1 1 I 128 1.53

100 ft

:W::

Velocity head ft

Head loss ft per

,504 .756 1.01 1.26 1.51 1

,004 ,009 016 :025 ,036

.035 .072 .I20

Ve locity ft per sec

1

]

100 ft

Velocity f t per sec

Ve locity head ft

.56 .84 1.12 1.40 1.67

.OO .01 02

.06

Head loss f t per

10Oft .W5 .092 153

Ve locity ft per sec

.691 1.04 1.38

Velocity head ft

Head loss ft per

.007 ,017 030

.074 .I54 .258

100ft

40


80

Schedule 160-steel



Flow US gal per mln

Velocity ft per sec

Velocity head ft

.481 .641 ,802 .962 1.12

-004 ,006 ,010 ,014 ,020

.024 .040 .060 .083 .I10

53 .71 . -88 1.06 1.23

.OO .O1 .01 .02 .02

Head loss R per

l00ft

Velocity ft per sec

Velocity head ft

Head loss ft per

Velocity ft per sec

Velocity head ft

.030 .051 .075 .lo5 .I38

,659 ,878 1.10 1.32 1.54

,007 ,012 ,019 ,027 ,037

100 ft

Head loss

fl per 100 tt .051 .OW .I28

.540 387

30 40 50 60 70

2.42 2.77 3.11 3.46 3.80

,091 ,119 ,150 ,185 ,224

.691 385 1.10 1.34 1.61

80 90 100 120 140

1.28 1.44 1.60 1.92 2.25

,026 ,032 .040 ,058 .078

.I40 .I73 .210 -293 -389

1.41 1.59 1.76 2.11 2.47

.03 .04 .05 .07 .09

.I76 .218 -265 370 -491

1.76 1.98 2.20 2.64 3.07

,048 ,061 ,075 108 147

1.11 1.29 1.48 1.69 1.91

4.15 4.49 4.84 5.18 5.53

,267 ,313 ,363 ,417 ,475

1.89 2.20 2.53 2.89 3.26

160 180 200 220 240

2.57 2.89 3.21 3.53 3.85

102 ,129 160 193 ,230

.480 .598 .728 .870 1.03

2.82 3.17 3.52 3.88 4.23

.12 -16 .19 .23 .28

.607 .757 .922 1.10 1.30

3.51 3.95 4.39 4.83 5.27

192 .243 -299 .362 .431

1.05 1.31 1.60 1.91 2.25

5.88 6.22 6.57 6.91 7.60

,536 .601 .669 .742 ,897

3.66 4.09 4.53 5.00 6.00

260 280 300 320 340

4.17 4.49 4.81 5.13 5.45

,270 -313 .360 .409 .462

1.19 1.37 1.56 1.77 1.98

4.58 4.94 5.29 5.64 5.99

.33

.48 .59

2.14 2.38 2.64 2.91 3.49

.56

1.51 1.74 1.99 2.25 2.52

5.71 6.15 6.59 7.03 7.47

.506 .587 -674 -766 .865

2.63 3.02 3.45 3.91 4.39

6.70 7.26 7.82 8.38 8.94

-70 .82 -95 1.09 1.24

4.13 4.81 5.54 6.33 7.17

8.30 8.99 9.68 10.37 11.06

1.90

12.4

360 380 400 420 440

5.77 6.09 6.41 6.74 7.06

,518 .577 .639 ,705 ,774

2.21 2.45 2.71 2.97 3.25

6.35 6.70 7.05 7.40 7.76

-63 .70 .77 .85 .94

2.81 3.12 3.44 3.78 4.13

7.91 8.35 8.78 9.22 9.66

.970 1.08 1.20 1.32 1.45

4.90 5.43 6.00 6.59 7.21

6.22 6.94 7.71 8.51 9.35

9.50 10.0 10.6 11.2 11.7

1.40 1.6 1.7 1.9 2.1

8.06 9.00 9.99 11.0 12.1

11.75 12.44 13.13 13.82 14.52

2.14 2.40 2.68 2.97 3.27

13.9 15.5 17.3 19.1 21.0

460 480 500 550 600

7.38 7.70 8.02 8.82 9.62

,846 ,921 ,999 1.21 1.44

3.54 3.84 4.15 4.99 5.90

8.11 8.46 8.82 9.70 10.6

1.02 1.11 1.21 1.46 1.7

4.50 4.88 5.28 6.35 7.51

10.10 10.54 10.98 12.08 13.18

1.58 1.73 1.87 2.26 2.70

7.85 8.53 9.23 11.1 13.1

1.91 2.09 2.27 2.47 2.99

10.2 11.2 12.1 13.1 15.8

12.3 12.8 13.4 14.0 15.3

2.3 2.5 2.8 3.0 3.6

13.3 14.5 15.7 17.0 20.5

15.21 15.90 16.59 17.28 19.00

3.59 3.92 4.27 4.64 5.61

22.9 25.0 27.2 29.5 35.5

650 700 750 800 850

10.4 11.2 12.0 12.8 13.6

1.69 1.96 2.25 2.56 2.89

6.89 7.95 9.09 10.3 11.6

11.5 12.3 13.2 14.1 15.0

2.1 2.4 2.7 3.1 3.5

8.77 10.1 11.6 13.1 14.8

14.27 15.37 16.47 17.57 18.67

3.16 3.67 4.21 4.79 5.41

15.4 17.8 20.3 23.0 25.9

15.1 16.4 17.6 18.9 20.2

3.55 4.17 4.84 5.55 6.32

18.7 21.7 25.3 28.9 32.8

16.7 18.1 19.5 20.9 22.3

4.3 5.1 5.9 6.8 7.7

24.3 28.4 32.8 37.6 42.7

20.74 22.46 24.19 25.92 27.65

6.67 7.83 9.08 10.4 11.7

42.1 49.2 57.0 65.2 74.1

900 950 1000 1100 1200

14.4 15.2 16.0 17.6 19.2

3.24 3.61 4.00 4.84 5.76

13.0 14.4 15.9 19.2 22.7

15.9 16.7 17.6 19.4 21.1

3.9 4.3 4.8 5.8 6.9

16.5 18.4 20.3 24.5 29.0

19.76 20.86 21.96 24.16 26.35

6.06 6.76 7.49 9.06 10.78

29.0 32.3 36.7 43.0 51.0

21.4 22.7 2?.9 25.2 27.7

7.13 8.00 8.91 9.87 11.9

37.0 41.4 46.0 50.9 61.4

23.7 25.1 26.5 27.9 30.7

8.7 9.8 10.9 12.1 146

48.1 53.8 59.8 66.2 79.8

29.38 31.10 32.83 34.56 38.02

13.4 15.0 16.7 18.5 22.4

83.4 93.4 104 115 139

1300 1400 1500 1600 1700

20.8 22.5 24.1 25.7 27.3

6.75 7.83 8.99 10.2 11.6

26.6 30.7 35.2 40.0 45.1

22.9 24.7 26.4 28.2 30.0

8.2 9.5 10.8 12.4 14.0

34.0 39.3 45.0 51.1 57.6

28.55 30.74 32.94 35.14 37.33

12.65 14.67 16.84 19.16 21.63

59.8 69.2 79.2 90.0 101

1

I 1 1 :I; :1 1 1 1::: 1 :lVi

70 80 90 100 110

1.79 2.04 2.30 2.55 2.81

,050 ,065 -082 .I01 .I23

365 .470 .588 .719 .862

1.76 2.02 2.27 2.52 2.77

,048 ,063 ,080 ,099 ,119

-330 -422 .523 .613 .732

1.95 2.23 2.51 2.79 3.07

120 130 140 150 160

3.06 3.32 3.57 3.83 4.08

-146 ,171 .I99 ,228 ,259

1.02 1.19 1.37 1.57 1.77

3.02 3.28 3.53 3.78 4.03

,142 ,167 ,193 -222 ,253

.861 1.00 1.15 1.31 1.48

170 180 190 200 220

4.34 4.60 4.85 5.11 5.62

,293 ,328 ,368 ,406 .490

1.99 2.23 2.47 2.73 3.29

4.28 4.54 4.79 5.04 5.54

.285 ,320 ,356 ,395 ,478

240 260 280 300 320

6.13 6.64 7.15 7.66 8.17

,583 ,685 ,794 .912 1.04

3.90 4.55 5.26 6.02 6.84

6.05 6.55 7.06 7.56 8.06

340 360 380 400 420

8.68 9.19 9.70 10.2 10.7

1.17 1.31 1.46 1.62 1.79

7.70 8.61 9.58 10.6 11.6

440 460 480 500 550

11.2 11.7 12.3 12.8 14.0

1.96 2.14 2.33 2.53 3.06

600 650 700 750 800

15.3 16.6 17.9 191 20.4

850 900 950 1000 1100

21.7 23.0 24.3 25.5 28.1

2.07 1.73

.08 .10 .12 .15

.424 .541 .649 .789 .943

3.35 3.63 3.91 4.19 4.47

.17 .20 .24 .27 .31

1.66 1.85 2.05 2.25 2.70

4.75 5.02 5.30 5.58 6.14

.35 .39

,569 ,667 ,774 ,888 1.01

3.19 3.72 4.28 4.89 5.53

8.57 9.07 9.58 10.1 10.6

1.14 1.28 1.43 1.58 1.74

12.8 13.9 15.2 16.4 19.8

11.1 11.6 12.1 12.6 13.9

3.65 4.28 4.96 5.70 6.48

23.6 27.6 32.0 36.6 41.6

7.32 8.20 9.14 10.1 12.3

46.9 52.6 58.5 64.8 78.3

.44

N o t e No allowance has been made for age, difference In diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

-38 .43 .49

:::: 301 373 .453 .612 .816

' Cast iron not commercially available in this size.

Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

1

FRICTION


Asphalt-dipped Cast lron and New Steel Pipe (Based on Darcy's Formula) (Continued)

Friction of Water


6 lnch

8 lnch

Asphalt-dipped cast lron

Std wt steel sch 40


Schedule 160-steel

6 . 0 inside dia

6.065" inside dia

5.761" inside dia


A

Std wt steel sch 40


7.981" Inside dla

7 . 6 2 5 insld dla

#halt-dipped zast iron

8 " inside dia

ule 160-steel

6.8 3 inside dia

Flow US gal per mln

Velocity ft per sec

Veloclty head ft

Head loss tt per 100 ft

Velocity ft per sec

Velocity head ft


Velocity ft per sec

Velocity head ft


Velocity ft per sec

Velocity head ft

Head loss fl per 100 ft

Flow US gal per mln

locity ft per sec

Veloclty head ft


Velocity ft per sec

Velocity head ft

Head loss tt per 100 tt

50 60 70 80 90

.57 .68 .79 .91 1.02

.005 .007 -010 ,013 ,016

.027 .038 ,048 .062 .077

.56 .67 .78 .89 1.00

.005 ,007 ,009 ,012 ,016

.025 .034 .045 .057 .071

.62 .74 .86 .98 1.11

.01 .01 .01 .01 .02

.032 .044 .058 .074 .091

,759 ,911 1.06 1.22 1.37

,009 ,013 ,018 ,023 ,029

.053 .073 ,096 .I23 .I52

130 140 150 160 170

.83 .89 .96 1.02 1.00

,011 ,012 ,014 .016 ,018

.037 .042 .048 .054 .060

.83 .90 .96 1.03 1.09

.Oll ,013 ,014 .016 ,018

.036 .042 .047 .053 .059

.020 .024 ,027 ,031 ,035

.079 .OW .lo2 .I15 .I28

100 120 140 160 180

1.13 1.36 1.59 1.82 2.04

.020 ,029 ,039 ,051 ,065

.094 .I32 .I76 .226 .283

1.11 1.33 1.55 1.78 2.00

,019 ,028 .038 -049 .062

.086 .I20 .I58 .202 .251

1.23 1.48 1.72 1.97 2.22

.02 .03 .05 .06 .08

.I10 .I54 ,203 .260 .323

1.52 1.82 2.13 2.43 2.73

,036 ,052 .070 ,092 .I16

.I84 .256 .340 .435 .522

180 190 200 220 240

1.15 1.21 1.28 1.40. 1.53

,021 .023 ,025 .031 ,037

.067 -074 .082 -098 .I15

1.15 1.22 1.28 1.41 1.54

.021 .023 .026 ,031 ,037

.066 .073 .080 .095 .I11

,039 ,043 ,048 ,058 ,069

.I42 .I57 .I72 .205 .241

200 220 240 260 280

2.27 2.50 2.72 2.95 3.18

-080 ,097 ,115 .135 -157

-346 .415 .490 .571 .658

2.22 2.44 2.66 2.89 3.11

,077. .093 ,110 ,130 ,150

.304 .363 .411 .477 548

2.46 2.71 2.96 3.20 3.45

09 .ll .14 .16 .19

392 .451 .530 .616 .708

3.04 3.34 3.64 3.95 4.25

.I43 -173 ,206 .242 ,281

-635 .760 395 1.04 1.20

.043 ,050 .057 ,077 ,101

.I34 .I54 .I75 .235 .303

,081. ,094 108 147 192

.279 .320 .350 .467 .601

300 320 340 360 380

3.40 3.63 3.86 4.08 4.31

.I80 ,205 .231 ,259 .289

.752 .851 .957 1.07 1.19

3.33 3.55 3.78 4.00 4.22

.I72 -196 ,222 ,240 ,277

.624 ,705 .790 .880 -975

3.69 3.94 4.19 4.43 4.68

.21 .24 .27 .31 .34

.807 .911 1.02 1.14 1.26

4.56 4.86 5.16 5.47 5.77

,322 .366 ,414 ,464 ,517

1.36 1.54 1.73 1.93 2.14

,128 .I58 ,191 ,228 ,267

.380 .465 .559 .661 .772

400 450 500 550 600

4.54 5.10 5.67 6.24 6.81

.320 -403 .500 ,605, ,720

1.31 1.65 2.02 2.44 2.89

4.44 5.00 5.55 6.11 6.66

,307 ,388 ,479 ,580 ,690

1.07 1.34 1.64 1.97 2.33

4.93 5.54 6.16 6.77 7.39

.38 .48 .59 .71 .85

1.39 1.74 2.13 2.55 3.02

6.07 6.82 7.59 8.35 9.11

,572 ,725 ,894 1.08 1.29

2.36 2.95 3.61 4.34 5.13

.310 ,356 ,405 .457 ,513

.891 1.02 1.16 1.30 1.45

650 700 750 800 850

7.37 7.94 8.51 9.08 9.64

.845 -980 1.12 1.28 1.44

3.38 3.90 4.47 5.07 5.72

7.22 7.77 8.33 8.88 9.44

,810 .939 1.08 1.23 1.38

2.71 3.13 3.57 4.04 4.55

8.00 8.63 9.24 9.85 10.5

.99 1.16 1.33 1.51 1.7

3.52 4.06 4.64 5.25 5.90

9.87 10.63 11.39 12.15 12.91

1.51 1.75 2.01 2.29 2.59

5.99 6.92 7.91 8.96 10.1

,571 ,633 ,766 ,911 1.07

1.61 1.78 2.15 2.55 2.98

900 950 1000 11M) 1200

10.2 10.8 11.3 12.5 13.6

1.62 1.80 2.00 2.42 2.88

6.40 7.11 7.87 9.50 11.3

9.99 10.5 11.1 12.2 13 3

1.55 1.73 1.92 2 32 2 76

5.08 5.64 6.23 7.49 8.87

11.1 11.7 12.3 13.5 14.8

1.9 2.1 2.4 2.8 3.4

6.60 7.33 8.09 9.74 11.5

1367 14 42 15.18 16.71 18.22

2.90 3.23 3.58 4.33 5.15

11.3 12.5 13.8 16.7 19.8

1.24 1.42 1.62 2.05 2.53

3.45 3.95 4.48 5.65 6.96

1300 1400 1500 1600 1700

14.7 15.9 17.0 18.2 19.3

3.38 3.92 4.50 5.12 5.78

13.2 15.3 17.5 19.9 22.4

14.4 15.5 16.7 17.8 18.9

3.24 3.76 4 31 4 91 5.54

10.4 12.0 13.7 15.6 17.5

16.0 17.2 18.5 19.7 20.9

40 4.6 5.3 6.0 6.8

13.5 15.6 17.8 20.3 22.8

19.74 21.26 22.78 24.29 25.81

6.05 7.01 8.05 9.16 10.34

23.1 26.7 30.6 34.7 39.1

3.06 3.65 4.28 4.96 5.70

8.40 9.98 11.7 13.5 15.5

1800 1900 2000 2200 2400

20.4 21.6 22.7 25.0 27.2

6.48 7.22 8.00 968 11.5

25.1 28.0 31.0 37.4 44.5

20.0 21.1 22.2 24.4 26.6

6 21 691 7.67 9.27 11.0

19.6 21.8 24.1 29.1 34.5

22.2 23.4 24.6 271 29.6

7.7 84 9.4 114 13.6

25.5 28.4 31.4 37.9 44.9

27.33 28.85 30.37 33.40 36.44

11.59 12.92 14.31 17.32 20.61

43.8 48.7 53.9 65.0 77.2

7.70 10.1 12.8 15.8 19.1

21.1 27.4 34.7 42.7 51.7

.


ve-

Head loss ft per 100 A

V e locity ft per sec

Veloc1ty head ft

Head loss ftper 100 ft

Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each Particular installation. It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

INGERSOLL-RAND CAMERON HYDRAULIC DATA Friction of Water


FRICTION Asphalt-dipped Cast lron and New Steel Pipe

Friction of Water


10 lnch

Std wt steel sch 40

Schedule 80 steel

10.0" ~nsldedla

10.020 inslde dia

9 . 5 6 2 lnslde dla

Flow US gal per min

Ve loclty ft per sec

Veloclty head ft


Veloclty ft per sec

180 200 220 240 260

74 .82 .90 .98 1.06

,008 010 .013 01 5 .018

.023 .028 .032 .038 .044

Schedule 160-steel


Veloclty ft per sec

Ve locity head ft


Velocity ft per sec

Ve loclty head ft

Head loss f t per 100 R

.73 .81 .90 98 1.06

008 ,010 013 01 5 017

.022 ,026 ,031 ,037 .042

304 ,894 ,983 1.07 1.16

,010 ,012 ,015 .018 ,021

,027 .033 .039 .046 .053

1.02 1.13 1.24 1.36 1.47

,016 ,020 024 ,029 ,034

.048 .059 .070 .082 .094

1 14 1 22 1.42 1.63 1.83

,020 023 -032 ,041 .052

.049 .055 .073 ,093 ,116

1.25 1.34 1-56 1.79 2.01

,024 ,028 ,038 ,050 ,063

.061 .069 .092 .I17 ,145

1.58 1.70 1.98 2.26 2.54

,039 ,045 ,061 ,079 ,100

.I08 .I23 .I63 .208 .259

280 300 350 400 450

1.14 1.23 1.43 1.63 1.84

,020 ,023 ,032 ,042 ,053

.051 .057 .077 .099 .I23

500 550 600 650 700

2.04 2.25 2.45 2.66 2.86

,065 ,079 .093 ,110 -127

.I50 .I80 .213 .248 .286

2.03 2.24 2.44 2.64 2.85

.064 ,078 ,093 .la9 126

.I40 ,167 .I97 .228 .253

234 2.46 2.68 2.90 3.13

,077 ,094 ,112 ,131 .I52

.I77 .211 .239 .277 .319

2.83 3.11 3.39 3.68 3.96

,124 -150 -179 .210 ,243

304 .364 .428 .498 .573

800 900 1000 1100 1200

3.27 3.68 4.09 4.49 4.90

-166 .210 .259 ,314 373

370 .464 .569 .685 .811

3.25 3.66 4.07 4.48 4.88

,165 -208 .257 -311 .370

.325 .405 .494 ,592 .699

3.57 4.02 4.47 4.92 5.36

.I98 .251 -310 ,375 .446

.410 .512 .625 ,749 ,884

4.52 5.09 5.65 6.22 6.79

.318 .402 ,496 ,600 ,714

7.38 9.23 1.13 1.35 1.60

1300 1400 1500 1600 1700

5.31 5.72 6.13 6.54 ,6.94

,438 .508 ,584 ,664 .749

,947 1.25 1.42 1.60

5.29 5.70 6.10 6.51 6.92

,435 ,504 ,579 ,659 .743

.814 .938 1.07 1.21 1.36

5.81 6.26 6.70 7.15 760

,524 607 ,697 .793 ,895

1.03 1.19 1.35 1.53 1.72

7.35 7.92 8.48 9.05 9.61

-839 .972 1.12 1.27 1.43

1.86 2.15 2.46 2.78 3.13

1800 1900 2000 2200 2400

7.35 7.76 8.17 8.99 9.80

,840 .936 1.04 1.26 1.49

1.79 1.99 2.20 2.65 3.15

7.32 773 8.14 8.95 9.76

834 ,929 1.03 1.,25 1.48

1.52 1.68 1.86 2.24 2.64

8.04 8.49 8.94 9.83 10.72

1.00 1.12 1.24 1.50 1.79

1.92 2.13 2.36 2.83 3.35

10.18 10.74 11.31 12.44 13.57

1.61 1.79 1.99 2.40 2.86

3.49 3.88 4.29 5.16 6.11

2600 2800 3000 3200 3400

10.6 114 12 3 13 1 13.9

1.75 2.03 2.33 2.66 3.00

3.68 4.26 4.88 5.54 6.25

10.6 11.4 12.2 13.0 13.8

1.74 2.02 2.32 2.63 2.97

3.09 3.57 4.08 4.62 5.20

11.62 12.51 13.40 14.30 15.19

2.09 2.43 2.79 3.17 3.58

3.92 4.52 5.17 5.87 6.60

14.70 15.83 16.96 18.09 19.22

3.35 3.89 4.47 5.08 5.74

7.14 8.25 9.44 10.7 12.1

3600 3800 4000 4500 5000

14.7 15.5 16.3 18.4 20.4

3.36 3.74 4.15 5.25 6.48

6.99 7.79 8.62 10.9 13.4

14.6 15.5 16.3 18.3 20.3

3.33 3.71 4.12 5.21 6 43

5.81 6.46 7.14 8.99 11.1

16.08 16.98 17.87 20.11 22.34

4.02 4.47 4.96 6.27 7.75

7.38 8.21 9.07 11.4 14.1

20.35 21.49 22.62 25.44 28.27

6.43 7.17 7.94 10.05 12 40

13.5 15.0 16.6 20.9 25.7

5500 6000 6500 7000 7500

22.5 24.5 26.6 28.6 30.6

7.85 9.34 11.0 12.7 14.6

16.2 19.2 22.6 26.1 30.0

22.4 24.4 26.4 28.5 305

7.78 9.26 10.9 12.6 14.5

13.3 15.8 18.5 21.4 24.5

24.57 26.81 29.04 31.28 33.51

9.37 11.15 13.09 15.18 17.43

17.0 20.1 23.6 27.3 31.2

31.10 33.92 36.75 39.58 42.41

15.01 17.86 20.96 24.31 27.91

31.1 36.9 43.2 50.0 57.3

1.09

Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It IS recommended that for most commercial deslgn purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

Std wt steel sch 40

Schedule 80 steel

Schedule 160 steel

11.938" inside dia

11.374 inside dia

10.126 inside dia


8 . 5 0 0 lnslde dia

Velocity head ft

,

(Continued)

12 Inch


1 2 . 0 inside dia Flow US gal per mln

Velocity head ft

Head loss R per

100fl

Velocity ft per sec

,006 .010 ,014 ,019 ,025

.014 .021 .030 .039 .050

,797 ,996 1.20 1.39 1.59

,010 ,015 ,022 ,030 ,039

.025 .038 .052 .069 .088

1.42 1.58 1.74 1.90 2.21

,031 ,039 .047 .056 .076

.062 .076 .090 .lo6 .I40

1.79 1.99 2.19 2.39 2.79

,050 ,062 .075 .089 ,121

.I10 .I33 -159 .I87 .240

.I42 .I76 .207 .247 .291

2.53 2.84 3.16 3.47 3.79

,099 ,125 ,155 .I87 .223

.I80 .216 .263 .315 .371

3.19 3.59 3.98 4.38 4.78

,158 ,200 ,246 ,298 .355

.308 .384 .469 .562 .663

,216 ,250 .287 ,327 ,414

.339 .390 .444 .502 .629

4.11 4.42 4.73 5.05 5.68

.262 .303 .348 ,396 ,501

.432 .497 .566 .640 .802

5.18 5.58 5.98 6.37 7.17

,416 ,483 ,554 ,631 ,798

.772 .889 1.02 1.15 1.44

511 .618 .735 ,863 1.00

.769 .923 1.09 1.27 1.47

6.32 6.95 7.58 8.21 8.84

.619 .749 .891 1.05 1.21

.981 1.18 1.39 1.62 1.87

7.97 8.77 9.56 10.36 11.16

.985 1.19 1.42 1.67 1.93

1.76 2.12 2.51 2.93 3.38

8.60 10.0 11.5 12.9 14.3

1.15 1.55 2.04 2.59 3.19

1.68 2.26 2.92 3.68 4.52

9.47 11.05 12.63 14.21 15.79

1.39 1.90 2.48 3.13 3.87

2.14 2.89 3.74 4.71 5.78

11.95 13.94 15.94 17.93 19.92

2.22 3.02 3.94 4.99 6.16

3.86 5.22 6.77 8.52 10.5

6.30 7.48 8.76 10.1 1 .

15.8 17.2 18.6 20.1 21.5

3.86 4.60 5.39 6.26 7.18

5.44 6.45 7.54 8.72 9.98

17.37 18.95 20.53 22.10 23.68

4.68 5.57 6.54 7.58 8.71

6.97 8.26 9.66 11.2 12.8

21.91 23.90 25.90 27.89 29.88

7.45 8.87 10.41 12.07 13.86

12.6 15.0 17.5 20.3 23.3

8.00 9.04 10.1 11.3 12.5

13.2 14.9 16.7 18.6 20.6

22.9 24.4 25.8 27.2 28.7

8.17 9.22 10.3 11.5 12.8

11.3 12.8 14.3 15.9 17.6

25.26 26.84 28.42 30.00 31.58

9.90 11.18 12.54 13.97 15.48

14.5 16.4 18.3 20.4 22.6

31.87 33.86 35.86 37.85 39.84

15.77 17.80 19.95 22.23 24.64

26.4 29.8 33.3 37.1 41.0

15.1 18.0 21.1 24.5 28.1

24.9 29.6 34.7 40.2 46.1

31.5 34.4 37.3 40.1 43.0

15.4 18.3 21.6 25.0 28.7

21.2 25.2 29.5 34.2 39.2

34.73 37.89 41.05 44.21 47.37

18.73 22.29 26.15 30.33 34.82

27.2 32.3 37.9 43.8 50.3

43.82 47.81 51.79 55.78 59.76

29.81 35.47 41.63 48.28 55.43

49.6 58.7 69.0 79.9 91.6

Velocity head ft

Head loss R per

100R

Velocity ft per sec

,005 ,008 ,012 ,016 ,020

.011 .017 .024 .031 .040

,632 ,789 ,947 1.11 1.26

1.29 1.43 1.58 1.72 2.01

.026 .032 ,039 ,046 .063

.049 460 .071 .083 .I11

.I47 .I84 -225 .271 .320

2.29 2.58 2.87 3.15 3.44

,082 ,103 ,128 ,154 ,184

,211 ,245 ,281 .320 .405

.374 .431 .493 .558 .702

3.73 4.01 4.30 4.59 5.16

5.67 6.24 6.81 7.38 7.94

.500 .605 .720 ,845 ,980

.862 1.04 1.23 1.44 1.67

5.73 6.31 6.88 7.45 8.03

3000 3500 4000 4500 5000

8.51 9.93 11.3 12.8 14.2

1.13 1.53 2.00 2.53 3.13

1.91 2.58 3.36 4.24 5.21

5500 6000 6500 7000 7500

15.6 17.0 18.4 19.9 21.3

3.78 4.50 5.28 6.13 7.03

8000 8500 9000 9500 10,000

22.7 24.1 25.5 26.9 28.4

11,000 12,000 13.000 14,000 15,000

31.2 34.0 36.9 39.7 42.6

Velocity ft per sec

Velocity head ft

ft per 100fl

Velocity ft per sec

Velocity head ft

Head loss ft per

200 250 300 350 400

.57 .71 .85 .99 1.13

,005 .008 ,011 .015 .020

.011 .017 .024 .031 .040

.57 .72 .86 1.00 1.15

450 500 550 600 700

1.28 1.42 1.56 1.70 1.99

.025 .031 .038 ,045 .061

.049 .060 .072 .085 -114

800 900 1000 1100 1200

2.27 2.55 2.84 3.12 3.40

.080 .I01 .I25 .I51 ,180

1300 1400 1500 1600 1800

3.69 3.97 4.26 4.54 5.11

2000 2200 2400 2600 2800

Head loss

'

100R

Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It is recommended that for most commercial design purposes a safety factor Of 15 to 20% be added to the values in the tables-see page 3-5.

CAMERON HYDRAULIC DATA Friction of Water (Continued)

Friction of Water (Continued) (Based on Darcy's Formula)


Asphalt-dipped cast iron and new steel pipe


14 lnch

Flow US gal per mln


New steel schedule 40

14.0"lnside dia

13.124"inside dla

Velocity ft per sec

Velocity head ft

Head loss fl per 100 A

18 Inch

16 lnch

Veloclty ft per sec

Veloclty head ft

Head loss tt per 100 ft

Flow US gal per min



16.0 inside dia

15.000" inslde dla

Velocity ft per sec

Velocity head ft

Head loss R per 100 fl

Velocity ft per sec

Velocity head ft

Head loss A per 100 fl

Asphalt-dipped cast iron Flow US gal per mln

-

18.0"inside dia

20 Inch Asphalt-dipped cast iron


16.876"inside dia

Velocity ft per sec

Velocity head ft

Head loss ft per 100 R

Velocity ft per sec

Veloclty head ft

tiead loss fl per 100 f l

20.0"inside dia Flow US gal per mln


18.812"inside dia

Veloclty ft per sec

Veloclty head ft

Head loss fl per 100 R

Velocity ft per sec

Velocity head ft

Head loss R per 100 fl

300 400 500 600 700

.625 -834 1.04 1.25 1.46

.006 -011 .017 ,024 ,033

.011 .019 .028 -039 .053

,712 ,949 1.19 1.42 1.66

,008 ,014 ,022 .031 ,043

.015 -025 .038 .052 .070

500 600 700 800 900

,798 .957 1.12 1.28 1.44

,010 .014 -019 ,025 ,032

.015 -020 -027 .035 .043

,908 1.09 1.27 1.45 1.63

,013 ,018 ,025 -033 .041

.020 .027 .036 .046 .058

500 600 700 800 900

,630 ,756 .883 1.01 1.14

,006 .009 -012 ,016 .020

,008 ,012 .016 ,019 .024

.717 ,861 1 .OO 1.1 5 1.29

.008 ,011 ,016 .020 ,026

.011 .015 .020 .026 .032

800 1000 1200 1400 1600

317 1.02 1.23 1.43 1.63

,010 ,016 ,023 .032 ,041

.012 .017 .025 -033 .042

,923 1.15 1.39 1.62 1.85

.013 ,021 ,030 ,041 ,053

.015 .023 .032 .043 ,055

800 900 1000 1100 1200

1.67 1.88 2.08 2.29 2.50

-043 ,055 ,067 ,082 ,097

.068 -085 .lo3 .I24 .I47

1.90 2.14 2.37 2.61 2.85

,056 .089 .071 .I11 .087 .I34 .I06 .I60 ,126 -182

1000 1200 1400 1600 1800

1.60 1.92 2.23 2.55 2.87

,040 ,057 ,077 .I01 ,128

.053 .075 .lo0 .I30 .I62

1.82 2.18 2.54 2.91 3.27

,051 ,074 .lo0 .I31 .I66

.070 .098 .I30 .I61 .201

1000 1200 1400 1600 1800

1.26 1.51 1.77 2.02 2.27

.025 .036 -048 -063 -080

.029 -041 .056 .072 .090

1.43 1.72 2.08 2.96 2.58

,032 ,046 ,063 ,082 ,103

,039 .055 .073 .093 ,116

1800 2000 2400 2800 3200

1.84 2.04 2.45 2.86 3.27

.052 ,065 ,093 ,127 ,166

.053 .065 .091 .I23 .I59

2.08 2.31 2.77 3.23 3.69

,067 ,083 ,119 ,162 ,212

,068 .083 .I12 .I50 .I93

1300 1400 1500 1600 1700

2.71 ,114 2.92 .I32 3.13 .I52 3.34 ,173 3.54 ,195

.I71 .I97 .225 .255 ,286

3.08 3.32 3.56 3.80 4.03

,148 ,171 ,196 ,223 .252

.212 .243 .277 .313 .351

2000 2500 3000 3500 4000

3.19 ,158 3.99 ,247 4.79 ,356 5.59 ,484 6.38 ,632

-199 .306 .436 .589 .764

3.63 4.54 5.45 6.35 7.26

,205 ,320 ,460 ,627 ,819

.245 .374 .530 .712 .920

2000 2500 3000 3500 4000

2.52 3.15 3.78 4.41 5.04

.099 .I54 .222 ,302 ,395

.I10 .I68 .239 .323 .418

2.87 3.59 4.30 5.02 5.74

,128 ,200 ,287 ,391 ,511

.I37 ,208 .294 ,394 SO8

3600 4000 5000 6000 7000

3.68 4.09 5.10 6.13 7.15

,210 ,259 ,405 ,583 ,793

.I99 .245 .377 .539 .728

4.16 4.62 5.77 6.93 8.08

,268 ,331 ,517 ,744 1.01

.241 .295 .452 .641 .862

1800 1900 2000 2500 3000

3.75 3.96 4.17 5.21 6.25

,218 .243 .270 -421 .607

.320 .355 .392 .605 .864

4.27 4.51 4.74 5.93 7.12

,283 ,315 ,349 ,546 ,786

-391 .434 .478 .732 1.04

4500 5000 6000 7000 8000

7 18 ,800 7.98 ,988 9.57 1.42 11.17 1.94 12.77 2.53

.962 1.18 1.69 2.29 2.98

8.17 9.08 10.89 12.71 14.52

1.04 1.28 1.84 2.51 3.27

1.15 1.42 2.01 2.72 3.53

4500 5000 6000 7000 8000

5.67 6.30 7.57 8.83 10.1

,500 ,617 ,888 1.21 1.58

.526 .647 ,924 1.25 1.63

6.46 7.17 8.61 10.0 11.5

.647 .798 1.15 1.57 2.04

.637 -780 1.11 1.49 1.94

8000 8.17 9000 9.19 10,000 10.2 12,000 12.3 14,000 14.3

1.04 1.31 1.62 2.33 3.17

.946 1.19 1.47 2.10 2.85

9.23 10.4 11.5 13.9 16.2

1.32 1.68 2.07 2.98 4.05

1.12 1.40 1.72 2.45 3.32

3500 7.30 4000 8.34 4500 9.38 5000 10.42 6000 12.51

.826 1.08 1.37 1.69 2.43

1.17 1.52 1.91 2.35 3.37

8.30 9.49 10.67 11.86 14.23

1.07 1.40 1.77 2.18 3.14

1.40 1.81 2.27 2.79 3.98

9000 10,000 11,000 12.000 13,000

14.36 15.96 17.55 19.15 20.74

3.20 3.95 4.78 5.69 6.68

3.77 4.64 5.60 6.65 7.98

16.34 18.16 19.97 21.79 23.60

4.14 5.12 6.19 7.37 8.65

4.44 5.45 6.58 7.80 9.13

9000 10.000 12,000 14,000 16,000

11.3 12.6 15.1 17.7 20.2

2.00 2.47 3.55 4.84 6.32

2.05 2.52 3.62 4.91 6.40

12.9 14.3 17.2 20.1 22.9

2.59 3.19 4.60 6.26 8.18

2.43 2.99 4.27 5.77 7.51

15,000 16.000 18,000 20,000 22,000

15.3 16.3 18.4 20.4 22.5

3.64 4.14 5.25 6.48 7.84

3.27 3.71 4.68 5.77 6.97

17.3 18.5 20.8 23.1 25.4

4.65 5.29 6.70 8.27 10.0

3.79 4.31 5.42 6.67 8.05

5.37 6.98 8.79 10.8 13.0

14,000 15.000 16.000 17,000 18.000

22.3 23.9 25.5 27.1 28.7

7.75 8.89 10.1 11.4 12.8

9.03 10.4 11.8 13.3 14.9

25.42 27.23 29.05 30.86 32.68

10.03 11.51 13.10 14.79 16.58

10.6 12.1 13.7 15.5 17.3

18,000 20,000 22,000 24,000 26.000

22.7 25.2 27.7 30.3 32.8

7.99 9.87 11.9 14.2 16.7

8.08 9.96 12.0 14.3 16.8

25.8 28.7 31.6 34.4 37.3

10.3 12.8 15.5 18.4 21.6

9.46 11.6 14.1 16.7 19.5

24,000 26,000 28.000 30.000 32,000

24.5 26.6 28.6 30.6 32.7

9.32 10.9 12.7 14.6 16.6

8.29 9.71 11.3 12.9 14.7

27.7 30.0 32.3 34.6 36.9

11.9 14.0 162 18.6 21.2

9.55 11.2 12.9 14.8 16.9

-

7000 8000 9000 10,000 11,000

14.6 16.7 18.8 20.8 22.9

3.30 4.32 5.47 6.75 8.17

4.49 5.86 7.39 9.11 11.0

16.60 4.28 18.97 5.59 21.35 7.07 23.72 8.73 26.09 10.56

12,000 13.000 14.000 15,000 16,000

25.0 27.1 29.2 31.3 33.3

9.71 11.4 13.2 15.2 17.3

13.3 15.3 17.7 20.3 23.1

28.46 30.83 33.20 35.58 37.95

12.57 15.5 14.75 18.1 17.11 21.0 19.64 24.0 22.35 27.3

20,000 22.000 24.000 26,000 28.000

31.9 35.1 38.3 41.5 44.7

15.8 19.1 22.8 26.7 31.0

18.3 22.2 26.4 30,9 35.8

36.31 38.94 45.57 47.20 50.84

20.46 24.76 29.47 34.58 40.11

21.3 25.8 30.6 35.9 41.5

28.000 30.000 32,000 34.000 36.000

35.3 37.8 40.3 42.9 45.4

19.3 22.2 25.3 28.5 32.0

19.4 22.3 25.3 28.6 32.0

40.2 43.0 45.9 48.8 51.6

25.0 28.7 32.7 36.9 41.4

22.6 25.9 29.5 33.2 37.2

34,000 36.000 38,000 40.000 45,000

34.7 36.8 38.8 40.9 46.0

18.7 21.0 23.4 25.9 32.8

16.6 18.5 20.7 22.9 28.9

39.2 41.6 43.9 46.2 51.9

23.9 26.8 29.9 33.1 41.9

19.0 21.3 23.7 26.2 33.1

17,000 18,000 20,000 22,000 24.000

35.4 37.5 41.7 45.9 50.0

19.5 21.8 27.0 32.7 38.8

26.1 29.7 36.0 43.5 52.7

40.32 42.69 47.43 52.18 56.92

25.23 28.27 34.92 42.26 50.29

30,000 32.000 34.000 36.000 38,000

47.9 51.1 54.3 57.4 60.6

35.6 40.5 45.7 51.2 57.1

41.1 46.7 52.7 59.1 65.8

54.47 58.10 61.73 65.36 68.99

46.04 52.39 59.14 66.30 73.88

47.6 54.1 61.0 68.4 76.1

38.000 40.000 42,000 44.000 46,000

47.9 50.4 53.0 55.5 58.0

35.6 39.5 43.5 47.8 52.2

35.7 39.5 43.6 47.8 52.2

54.5 57.4 60.2 63.1 66.0

46.1 ' 51.1 56.3 61.8 67.6

41.4 45.9 50.5 55.4 60.5

50.000 55,000 60,000 65,000 70,000

51.1 56.2 62.3 66.4 71.5

40.5 49.0 58.3 68.4 79.3

35.7 43.1 51.3 60.2 69.8

57.7 63.5 69.3 75.0 80.8

51.7 62.6 74.5 87.4 101

40.8 49.3 58.6 68.6 79.5

30.8 34.5 42.9 51.3 61.0

Note: No allowance has been made for age, difference In d~ameter,or any abnormal condition of ~nterlor surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It IS recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.



INGERSOLLRAND

Friction of Water (Continued)






Flow US gal per mln

-

Asphalt-dlpped cast ~ r o n


24.0"inslde dia

22.624"lnslde dla

VeVel o c ~ t y loclty f l per head sec ft

36 Inch

30 Inch

24 Inch

Head loss ft per l00ft

Veloclty ft per sec

Velocity head ft

Head loss ft per l00R

-

Flow US gal per mln

Asphalt-dlpped cast iron


30.0"lnslde dla

28.750"lnslde dla

Veloclty ft per sec

Veloc:ty head ft

Head loss ft per l00fl

Veloclty ft per sec

Veloclty head ft

Head loss ft per l00ft

,567 ,709 .851 ,993 1.14

,005 .008 .011 ,015 ,020

,005 .007 .010 .013 ,017

.638 .798 ,958 1.12 1.28

.006 010 -014 ,019 ,025

.006 .009 .013 .017 .022

1000 1200 1400 1600 1800

.454 ,545 ,635 ,726 ,817

003 .005 ,006 ,008 ,010

.002 .003 .005 .006 .007

.494 .593 ,692 ,791 ,890

004 005 ,007 ,010 ,012

.003 .004 .005 .007 .009

1800 1.28 2000 1.42 2400 1.70 2800 1.99 3200 2.27

,025 ,031 ,045 .061 ,080

.021 .026 .037 -049 .063

1.44 1.60 1.92 2.24 2.55

,032 ,040 ,057 078 ,101

.028 .034 -047 .063 .080

2000 2400 2800 3200 3600

,908 1.09 1.27 1.45 1.63

,013 ,018 ,025 -033 .041

.009 .012 .016 .021 .026

,988 1.19 1.38 1.58 1.78

,015 ,022 ,030 -039 .049

.010 .015 .019 .025 .031

3600 2.55 4000 2.84 5000 3.55 6000 4.26 7000 4.96

.I01 .I25 .I95 ,281 ,383

.079 .097 .I49 .212 .287

2.87 3.19 3.99 4.79 5.59

.I28 ,158 ,247 356 .484

.096 .I18 .I79 -254 .341

4000 5000 6000 7000 8000

1.82 2.27 2.72 3.18 3.63

,051 ,080 ,115 157 205

.032 ,048 .069 .092 .I19

1.98 2.47 2.97 3.46 3.95

.061 ,095 ,136 .I86 .243

.037 .057 .077 .I03 -133

800 1000 1200 1400 1600

26,000 28.000 30,000 34.000 38.000

18.4 19.9 21.3 24.1 27.0

5.28 6.12 7.03 9.02 11.3

3.78 4.38 5.02 6.44 8.03

20.8 22.3 23.9 27.1 30.3

6.68 7.75 8.90 11.4 14.3

4.34 5.03 5.76 7.36 9.17

28.000 30,000 35.000 40,000 45,000

12.7 13.6 15.9 18.2 20.4

2.51 2.88 3.92 5.12 6.48

1.39 1.59 2.15 2.81 3.54

13.8 14.8 17.3 19.8 22.2

2.97 3.41 4.64 6.07 7.68

1.48 1.69 2.29 2.97 3.75

42,000 46,000 50.000 60.000 70.000

29.8 32.6 35.5 42.6 49.6

13.8 16.5 19.5 28.1 38.3

9.80 11.7 13.9 19.9 27.1

33.5 36.7 39.9 47.9 55.9

17.4 20.9 24.7 35.6 48.4

11.2 13.4 15.8 22.6 30.7

50.000 55.000 60.000 65,000 70.000

22.7 25.0 27.2 29.5 31.8

7.99 9.67 11.5 13.5 15.7

4.37 5.28 6.27 7.35 8.52

24.7 27.2 29.7 32.1 34.6

9.48 115 13.6 16.0 18.6

4.61 5.56 6.60 7.73 8.95

80,000 90,000 100,000 110,000 120.000

56.7 63.8 70.9 78.0 85.1

50.0 63.2 78.1 94.3 112

35.3 44.7 55.1 65.6 78.5

63.8 71.8 79.8 87.8 95.8

63.3 80.1 98.9 110 142

40.0 50.6 62.3 75.3 89.6

75,000 80,000 85.000 90,000 100,000

34.0 36.3 38.6 40.9 45.4

18.0 20.5 23.1 25.9 32.0

9.77 11.1 12.5 14.0 17.3

37.1 39.5 42.0 44.5 49.4

21.3 24.3 27.4 30.7 379

10.3 11.7 13.1 14.7 18.1

.

Flow US gal per mln

42 Inch 42.0lnslde dla

Asphalt-d~pped cast ~ r o n


36.0"Inside dla

34.500"lnside dla

Velocity ft per sec

Veloclty head ft

Head loss ft per 100 R

Veloclty ft p e r sec

Velocity head ft

Head loss A per 100 ft

Flow US gal per mln

Veloclty ft per sec

Veloclty head ft

Cast iron asphalt dlpped

New steel

Head loss tU100 ft

1400 1600 1800 2000 2400

,441 ,504 ,567 ,630 -756

,003 ,004 ,005 .006 .009

.002 .002 .003 .004 .005

,480 .549 ,618 .686 .824

,004 ,005 ,006 ,007 ,011

.002 .003 ,004 ,004 .006

2000 3000 4000 5000 6000

,463 ,695 ,926 1.16 1 39

003 007 ,013 ,021 .030

.002 ,004 .006 ,009 .013

.002 .003 .006 .009 .012

2800 3200 3600 4000 5000

,883 1.01 1 .I 4 1.26 1.58

,012 .016 ,020 ,025 ,039

.007 .008 .010 .013 .019

,961 1.10 1.24 1.37 1.72

,014 ,019 ,024 ,029 .046

.008 .010 .013 .015 .023

7000 8000 9000 1 0,000 11,000

1.62 1.85 2.08 2.32 2.55

.041 ,053 .067 ,083 ,101

.017 .022 ,027 .034 ,040

.017 .021 .026 .032 .037

6000 7000 8000 9000 10,000

1.89 2.21 2.52 2.84 3.15

.056 ,076 .099 ,125 .I54

.027 .037 .048 .060 .073

2.06 2.40 2.75 3.09 3.43

-066 .090 -117 -148 ,183

-033 .043 -054 .067 .082

12,000 14,000 16,000 18,000 20,000

2.78 3.24 3.71 4.17 4.63

,120 ,163 ,213 ,270 .333

.048 .064 .083 .lo4 .I28

.043 .058 ,075 .094 .I14

12,000 14,000 16,000 18.000 20.000

3.78 4.41 5.04 5.67 6.30

.222 302 ,395 ,500 -617

.lo4 .I40 ,182 .228 .281

4.12 4.81 5.49 6.18 6.86

.263 -358 ,468 ,592 ,731

.I15 .I55 .200 .250 307

25,000 30,000 35.000 40,000 45.000

5.79 6.95 8.11 9.26 10.4

,520 ,749 1.02 1.33 1.69

.I98 .282 382 .497 .626

.I75 .249 335 .434 .545

25,000 30,000 35.000 40,000 50,000

7.88 9.46 11.0 12.6 15.8

,962 1.39 1.89 2.47 3.86

.433 .622 ,843 1.10 1.70

8.58 10.30 12.0 13.7 17.2

1.14 1.65 2.24 2.93 4.57

.471 .671 .906 1.18 1.82

50.000 60.000 70,000 80,000 90,000

11.6 13.9 16.2 18.5 20.8 .

2.08 3.00 4.08 15.33 6.74

.771 1.11 1.50 1.95 2.47

.669 .954 1.29 1.67 2.11

60.000 70.000 80,000 90,000 100,000

18.9 22.1 25.2 28.4 31.5

5.55 7.56 9.87 12.5 15.4

2.45 3.32 4.33 5.47 6.74

20.6 24.0 27.5 30.9 34.3

6.58 8.96 11.7 14.8 18.3

2.60 3.52 4.58 5.77 7.11

100,000 110,000 120.000 130.000 140.000

23.2 25.5 27.8 30.1 32.4

8.32 10.1 12.0 14.1 16.3

3.04 3.67 4.37 5.12 5.93

2.60 3.13 3.72 4.35 5.04

110,000 120.000 130,000 140.000 150.000

34.7 37.8 41.0 44.1 47.3

18.7 22.2 26.1 30.2 34.7

8.15 9.69 11.4 13.2 15.1

37.7 41.2 44.6 48.0 51.5

22.1 26.3 30.9 35.8 41.1

8.58 10.2 11.9 13.8 15.8

150.000 160.000 170.000 180.000 190.000

34.7 37.1 39.4 41 7 44.0

18.7 21.3 24.1 27.0 30.0

6.80 7.73 8.73 9.78 10.9

5.77 6.56 7.39 8.28 9.21

160,000 170.000 180,000 190.000 200.000

50.4 53.6 567 59.9 63.0

39.5 44.6 50.0 55.7 61.7

17.2 19.4 21.7 24.2 26.8

54.9 58.3 61.8 65.2 68 6

46.8 52.8 59.2 66.0 73.1

18.0 20.3 22.8 25.3 28.0

200,000 250,000 300.000 350.000 400.000

46.3 57.9 69.5 81.1 92 6

33.3 52.0 74.9 102 133

12.1 18.8 27.1 36.8 48.0

10.2 15.6 22.4 30.4 39.6

-

Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added t o the values in the tables-see page 3-5.

Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It IS recommended that for most commerc~aldesign purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.



54 lnch 54.0"Inside d ~ a

Flow US gal per rnln

2000 3000 4000 5000 6000

Cast Iron asphalt dipped

New steel

Flow US gal per rnin

Cast Iron asphalt d~pped

New steel

Veloc~ty ft per sec

Veloc~ty head ft

.355 .532 .709 ,887 1.06

,002 ,004 ,008 .012 .018

.DO1 .002 .003 .005 .007

.oo: .002 .003 .005 .006

10,000 12.000 14.000 16.000 18.000

1.40 1.68 1.96 2.24 2.52

,030 ,044 ,060 .078 099

.010 .013 .018 .023 ,029

.009 ,013 ,017 ,022 .027

1 24

.009 .011 .014 .017 .024

.009 ,010 ,014 .017 .023

20,000 22.000 24.000 26,000 28,000

2.80 3.08 3.36 3.64 3.92

122 147 .I75 206 .239

.036 .043 .051 ,059 .069

,033 .039 .047 ,054 .062

30,000 35,000 40,000 45,000 50.000

4.20 4.90 5.60 6.30 7.00

.274 .373 .487 ,617 ,761

.079 .lo6 .I37 ,173 ,213

,071 .096 ,123 .I54 .I89

head loss

ft1100 tt

7000 8000 9000 10,000 12,000

1.42 1.60 1.77 2.13

,024 .031 .040 ,049 ,070

14,000 16,000 18,000 20,000 25.000

2.48 2.84 3.19 3.55 4.43

,096 125 ,158 .I95 .304

-033 .042 ,053 .065 .I00

.031 .039 .048 .059 .092

30.000 35.000 40.000 45,000 50,000

5.32 6.21 7.09 7.98 8.87

.439 .598 -779 .987 1.22

.I43 .I93 .251 .316 .389

.I30 ,175 .225 .279 .340

55,000 60,000 70,000 80.000 90,000

9.75 10.64 12.41 14.18 15.96

1.47 1.76 2.39 3.12 3.95

.469 .556 .754 .982 1.24

.406 .485 .654 .849 1.07

100,000 110,000 120,000 130,000 140.000

17.73 19.50 21.28 23.05 24.82

4.88 5.90 7.03 8.25 9.56

1.53 1.84 2.19 2.52 2.98

1.31 1.58 1.88 2.20 2.54

Veloc~ty ft per sec

Veloc~ty head ft

head loss ft per 100 ft

84 lnch

72 lnch

60 lnch

Asphalt-dipped cast iron and new steel pipe 48 lnch




Nom~nalslze

Nom~nalsize

Nominal size

60.0inside dia

7 2 inside dia

84.0inside dia

Flow US gal per min

Flow US gal per mln

Flow US gal per mln

VeVeHead l o c ~ t y l o c ~ t y loss ft per head R per ft sec 100 R

14.000 16,000 18,000 20,000 22,000

1.59 1.82 2.04 2.27 2.50

,039 -051 .065 ,080 ,097

.010 .013 .017 .020 .023

18,000 20.000 22.000 24,000 26,000

1.42 1.58 1.73 1.89 2.05

,031 ,039 ,047 ,056 ,065

.007 .008 ,010 .012 .013

24,000 26.000 28,000 30,000 35,000

24,000 26.000 28.000 30.000 35,000

2.72 2.95 3.18 3.40 3.97

,115 ,135 -157 .I80 -245

.027 .032 -037 .042 .056

28,000 30,000 35.000 40,000 45.000

2.21 2.36 2.76 3.15 3.55

,076 -087 ,118 ,154 ,195

.015 .018 .023 .029 .036

40,000 45,000 50,000 55.000 60,000

40.000 45.000 50,000 60.000 70,000

4.54 5.11 5.67 6.81 7.94

.320 ,405 ,500 ,719 ,979

.072 .091 .l 11 .I57 .212

50,000 60,000 70,000 80.000 90,000

3.94 4.73 5.52 6.30 7.09

,241 ,347 ,472 .617 ,781

,045 ,063 .085 .I10 .I37

80.000 90,000 100,000 110,000 120.000

9.08 10.2 11.3 12.5 13.6

1.28 1.62 2.00 2.42 2.88

.274 .345 .423 SO9 .603

100,000 110,000 120,000 130,000 140,000

7.88 8.67 9.46 10.2 11.0

,964 1.17 1.39 1.63 1.89

130,000 140,000 150.000 160,000 170.000

14.8 15.9 17.0 18.2 19.3

3.38 3.92 4.50 5.12 5.78

.705 .815 .933 1.06 1.19

150,000 160,000 170,000 180.000 190,000

11.8 12.6 13.4 14.2 15.0

180,000 190,000 200.000 250.000 300.000

20.4 21.6 22.7 28.4 34.0

6.48 7.21 7.99 12.5 18.0

1.33 1.48 1.64 2.55 3.65

200,000 250.000 300.000 350,000 400,000

350.000 400.000 450.000 500,000 550.000

39.7 45.4 51.1 56.7 62.4

24.5 32.0 40.5 50.0 60.5

4.95 6.45 8.14 10.0 12.1

600,000 650.000 700.000 750.000 800.000

68.1 73.8 79.4 85.1 90.8

71.9 84.4 97.9 112 128

14.4 16.9 19.7 22.4 25.5

Velocity ft per sec

Velocity head ft

Head loss ft per

l00R

Velocity ft per sec

Velocity head

Head loss R per

ft

100 R

1.39 1.51 1.62 1.74 2.03

,030 ,035 .041 ,047 ,064

.005 .006 .007 .008 ,011

2.32 2.90 3.18 3.47

,083 ,105 -130 ,157 ,187

.014 .017 .021 .025 .029

70.000 80,000 90,000 100,000 1 1 0,000

4.05 4.63 5.21 5.79 6.37

,255 ,333 ,421 ,520 ,629

.039 .051 .063 .078 .093

.I68 .203 .240 .280 323

120,000 130,000 140,000 150,000 160,000

6.95 7.53 8.11 8.64 9.26

,749 ,879 1.02 1.17 1.33

.I10 .I29 .I49 .I70 .I92

2.17 2.47 7.89 3.12 3.48

.370 .419 .472 .528 .587

170,000 180,000 190,000 200,000 250.000

9.84 10.4 11.0 11.6 14.5

1.50 1.69 1.88 2.08 3.25

.216 .242 .269 .297 .459

15.8 19.7 23.6 27.6 31.5

3.86 6.02 8.67 11.8 15.4

.648 1.00 1.44 1.95 2.53

300,000 350,000 400,000 450.000 500,000

17.4 20.3 23.2 26.1 28.9

4.68 6.37 8.32 10.5 13.0

.655 .886 1.15 1.45 1.79

450,000 500.000 550,000 600,000 650.000

35.5 39.4 43.3 47.3 51.2

19.5 24.1 29.2 34.7 40.7

3.20 3.94 4.75 5.65 6.62

550,000 600,000 650,000 700,000 750,000

31.8 34.7 37.6 40.5 43.4

15.7 18.7 22.0 25.5 29.3

2.16 2.56 3.00 3.48 3.99

700,000 750,000 800,000 850,000 900,000

55.2 59.1 63.0 67.0 70.9

47.2 54.2 61.7 69.6 78.1

7.66 8.79 9.99 11.3 12.6

800,000 850,000 900,000 950,000 1,000,000

46.3 49.2 52.1 55.0 57.9

33.3 37.6 42.1 46.9 52.0

4.53 5.11 5.72 6.37 7.05

2.61

Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each partlcular installat~on It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values In the tables-see page 3-5. Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

INGERSOLLRAND Friction of Water

FRICTION



96 Inch

108 Inch

Nominal size

120.0inside dia

108.0 inside dia

96.0 inside dia Flow US gal per min

Flow US gal per mln

Velocity ft per sec

Velocity head ft

Head loss ft per

Flow US gal per mln

Velocity ft per sec

Veloclty head ft

Head loss ft per

Velocity ft per sec

Velocity head ft

Head loss ft per

12.000 14,000 1 6,000 18.000 20.000

,532 .621 ,709 ,798 ,887

,004 ,006 ,008 ,010 ,012

.001 ,001 .001 .002 .002

15:000 20,000 25.000 30,000 35,000

-525 .700 ,876 1.05 1.23

.004 .008 ,012 ,017 ,023

.OOl ,001 .002 .002 .003

20.000 30.000 40.000 50,000 60,000

,567 ,851 1.14 1.42 1.70

,005 ,011 .020 .031 .045

.001 .001 .002 .004 .005

22,000 24,000 26.000 28,000 30,000

,975 1.06 1.15 1.24 1.33

,015 ,018 .021 ,024 ,027

.002 .003 .003 .004 .004

40,000 45 000 50,000 60.000 70,000

1.40 1.58 1.75 2.10 2.45

,030 .039 .048 .069 ,093

,004 .005 .006 .009 .011

70,000 80,000 90.000 100,000 110,000

1.99 2.27 2.55 2.84 3.12

,061 ,080 ,101 .I25 ,151

.007 .009 .011 .013 .016

40,000 50,000 60,000 70.000 80,000

1.77 2.22 2.66 3.10 3.55

.049 ,076 .I10 ,149 - 195

.007 -011 .015 .020 .026

80.000 90.000 100,000 110,000 120,000

2.80 3.15 3.50 3.85 4.20

,122 -154 ,190 ,230 ,274

.015 .018 .022 .027 .031

120.000 130.000 140.000 150.000 160.000

3.40 3.69 3.97 4.26 4.54

,180 ,211 ,245 ,281 ,320

.019 .022 .025 .028 .032

90,000 100,000 110,000 120,000 130,000

3.99 4.43 4.88 5.32 5.76

,247 ,305 ,369 ,439 ,515

,033 .040 ,048 .056 .066

130,000 140,000 150,000 160,000 170,000

4.55 4.90 5.25 5.60 5.95

,322 ,373 ,428 ,487 ,550

.037 .042 .048 .054 .061

170,000 4.83 180,000 5.11 190,000 5.39 200.000 5.67 250,000 7.09

,361 .405 .451 ,500 ,781

.036 .040 .045 -049 .076

140,000 1 50,000 160,000 170,000 180,000

6.21 6.65 7.09 7.54 7.98

,598 ,686 ,781 ,881 ,988

,076 .087 .098 .llO .I23

180.000 6.30 ,617 190,000 6.65 ,687 ,761 200,000 7.00 250,000 8.76 1.19 300,000 10.5'1.71

.068 .076 .084 .I29 .I83

300.000 350.000 400,000 450,000 500,000

8.51 9.93 11.3 12.8 14.2

1.12 1.53 2.00 2.53 3.12

.I08 .I45 .I88 .237 .291

190,000 200,000 250.000 300,000 350.000

8.42 8.87 13.3 15.5

1.10 1.22 1.91 2.74 3.74

,137 .I51 .233 .333 .449

350,000 400,000 450.000 500.000 600,000

12.3 14.0 15.8 17.5 21.0

2.33 3.05 3.86 4.76 6.85

.247 .321 .404 .497 .710

600,000 700.000 800,000 900,000 1,000,000

17.0 19.9 22.7 25.5 28.4

4.50 6.12 7.99 10.1 12.5

.416 -562 .731 .922 1.14

400.000 450.000 500.000 600,000 700,000

17.7 19.9 22.2 26.6 31.0

4.88 6.18 7.62 11.0 14.9

.584 .735 .905 1.30 1.76

700.000 800.000 900.000 1,000,000 1,100,000

24.5 28.0 31.5 35.0 38.5

9.33 12.2 15.4 19.0 23.0

.962 1.25 1.58 1.94 2.35

1,100,000 1,200.000 1,300.000 1,400,000 1,500,000

31.2 34.0 36.9 39.7 42.6

15.1 18.0 21.1 24.5 28.1

1.37 1.63 1.91 2.21 2.53

800,000 900.000 1,000,000 1,100,000 1,200,000

35.5 39.9 44.3 48.8 53.2

19.5 24.7 30.5 36.9 43.9

2.29 2.88 3.55 4.29 5.10

1,200,000 1,300.000 1,400,000 1,500,000

42.0 45.5 49.0 52.5

27.4 32.2 37.3 42.8

2.79 3.27 3.78 4.34

1,600,000 1,700,000 1,800,000 1.900.000 2,000,000

45.4 48.2 51.1 53.9 56.7

32.0 36.1 40.5 45.1 50.0

2.87 3.24 3.63 4.04 4.47

11.1

l00R

l00ft

168 Inch

144 Inch

120 Inch

Nominal size

Nominal size




l00n


Flow US gal per mln

192 Inch

Nominal size

Nominal slze

144.W inside dia

168.0inside dia Flow US gal pef mln

Velocity head ft

Nominal size

Head loss ft per

Flow US gal per min

Velocity ft per sec

Velocity head ft


30,000 .591 40.000 .788 50,000 .985 60,000 1.18 70,000 1.38

,005 ,010 ,015 .022 ,030

.001 .001 .002 ,002 .003

50.000 ,724 60,000 ,868 70,000 1.01 80.000 1.16 90,000 1.30

,008 ,012 ,016 ,021 ,026

.001 .001 .002 .002

60.000 80,000 100,000 120.000 140.000

1.58 1.77 1.97 2.17 2.36

.039 .049 .060 .073 ,087

.004 .005 .DO6 .006 .008

100,000 1.45 120,000 1.74 140,000 2.03 150.000 2.17 160,000 2.32

.033 ,047 ,064 ,073 ,083

130,000 2.56 140,000 2.76 150.000 2.96 160,000 3.15 170.000 3.35

.I02 .I 18 .I36 .I54 ,174

.009 ,010 .011 .013 .015

180,000 200,000 220,000 240.000 250,000

2.61 2.90 3.18 3.47 3.62

180,000 190,000 200,000 250,000 300.000

3.55 3.74 3.94 4.93 5.91

,195 .217 ,241 ,376 ,542

.016 .018 .020 .030 -043

260.000 280.000 300.000 350,000 400,000

350,000 400,000 450,000 500,000 600,000

6.90 7.88 8.87 9.85 11.8

,738 ,964 1.22 1.51 2.17

.058 .075 .094 .I16 .I65

700.000 800,000 900.000 1,000.000 1,200,000

13.8 15.8 17.7 19.7 23.6

2.95 3.86 4.88 6.02 8.67

1,400,000 1,5M],000 1,600,000 1,800.000 2,000.000

27.6 29.6 31.5 35.5 39.4

2.200,OOO 2,400,000 2,500.000 2.600.000 2.800,OOO

43.3 47.3 49.3 51.2 55.2

80,000 90,000 100,000 110,000 120,000

Velocity ft per sec

100 ft

-

192.0"inside dia Velocity ft per sec

,665 ,887

Veloclty head ft

Head

loss

n per 100 ft

1.33 1.55

,007 -012 -019 .027 .037

.001 .001 .001 .002 .003

.003 .004 .005 .005 .006

150,000 1.66 160,000 1.77 180.000 2.00 200,000 2.22 220.000 2.44

,043 ,049 ,062 .076 ,092

.003 .003 .004 .005 .006

.I05 ,130 ,157 ,187 ,203

.008 .009 .011 .013 .014

240,000 250,000 260,000 280.000 300,000

2.66 2.77 2.88 3.10 3.32

,110 ,119 ,129 ,149 ,172

,007 .007 .008 .009 .010

3.76 4.05 4.34 5.07 5.79

,220 .255 ,293 ,398 .520

.015 .018 .020 .027 .035

350.000 400.000 450.000 500,000 600.000

3.88 4.43 5.00 5.54 6.65

,233 305 ,386 ,476 .686

.014 .018 .022 .027 .039

450,000 500,000 600,000 700,000 800.000

6.51 7.24 8.68 10.1 11.6

,658 .813 1.17 1.59 2.08

.043 .053 .076 .lo2 .I33

700,000 800,000 900,000 1,000,000 1.200.000

7.76 8.87 9.97 13.3

,934 1.22 1.54 1.91 2.74

.052 .068 .085 .lo4 .I49

.223 .289 .364 .448 .641

900.000 1.000.000 1,200,000 1,400,000 1,600,000

13.0 14.5 17.4 20.3 23.7

2.63 3.25 4.68 6.37 8.73

.I67 .205 .293 .396 .547

1.400.000 1,600.000 1,800,000 2,000,000 2,200,000

15.5 17.7 19.9 22.2 24.4

3.74 4.88 6.18 7.62 9.22

.201 .261 .329 .405 .488

11.8 13.6 15.4 19.5 24.1

.869 .995 1.13 1.43 1.76

1,800,000 2,000,000 2,200,000 2,400,000 2,600,000

26.7 29.6 32.6 35.6 38.5

11.1

13.6 16.5 19.6 23.1

.690 .850 1.03 1.22 1.43

2,400,000 2,600,000 2,800,000 3.000.000 3,200.000

26.6 28.8 31.0 33.2 35.5

11.0 12.9 14.9 17.2 19.5

.580 .679 .786 .900 1.02

29.2 34.7 37.6 40.7 47.2

2.12 2.52 2.73 2.95 3.42

2.800.000 3.000.000 3,200,000 3,400,000 3.600,OOO

41.5 44.5 47.4 50.4 53.4

26.7 307 34.9 39.4 44.2

1.65 1.89 2.15 2.43 2.72

3,400.000 3,600,000 3.800.000 4,000,000 4,500,000

37.7 39.9 42.1 44.3 49.9

22.0 24.7 27.5 30.5 38.6

1.15 1.29 1.44 1.59 2.01

.001

1.11

11.1

Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interior Surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.


Friction Losses in Smooth Tubing and Pipe

(Eased on Darcy's Formula)

Copper Tubing (Type K, L and M)- S. P. S. Copper and Brass Pipe, Plastic and Glass Pipe. Smooth copper tubing and pipe, brass pipe, plastic and glass pipe are available in various sizes and types to meet individual requirements a s specified-sizes may be different than standard. To avoid the necessity of interpolation and applying correction factors to t h e values for cast iron and steel pipe, a special set of tables is included herewith on pages 3-34 to 3-48 figured on t h e basis of commercially available copper tubing, and S.P.S. copper and brass pipe. These tables are calculated using the Darcy-Weisbach equation (see page 3-3) and basis an absolute roughness parameter of 0.000005 (see page 3;5); since this roughness parameter applies to very smooth pipe or tubing a safety factor should' be applied in those cases to compensate for possible questionable conditions; a s discussed on page 3-5 it is suggested that for most commercial design purposes a safety factor of 15 to 20% be added to the head loss values in the tables. I t should be noted t h a t t h e head loss d a t a can apply to a n y fluid having a kinematic viscosity v = 0.000 012 16 ft2/sec (1.130 centistokes), which is t h e viscosity for pure fresh water a t 60°F. Greater viscosities (colder water) will increase t h e friction; lower viscosities (warmer water) will decrease the friction. Friction losses for tubing and pipe sizes between those listed in the tables may be determined with reasonable accuracy using a ratio of the fifth powers of the diameters; for example: Desired friction loss pipe B = known friction loss pipe A

Copper Tubing-*S.P.S. l/2

Copper and Brass Pipe lnch

Type K tublng

Type L t u b ~ n g

Type M t u b ~ n g

-

.527" ~ n s ~ d e~ a 049" wall thk

545" ~ n s ~ d e~ a 0 4 0 wall thk

,569" ~ n s ~ ddia e ,028'' wall thk

US gal per mln

Head loss ftI100ft

Head

Flow

Veloc~ty ftisec

Velocity ftisec

loss fti100ft

Veloc~ty ftlsec

Head loss fV100ft

' Pipe

625" ~ n s i d ed ~ a 1075" wall thk Veloc~ty ftisec

Head loss fV100n'

Flow

-

US gal per mln

1' 2 1 1112 2 21/2

0.74 1 47 220 2.94 3 67

0.88 2.87 5.77 9.52 14.05

0.69 1.38 2.06 2.75 3.44

0.75 2.45 4.93 8.11 11.98

0.63 1 26 1 90 253 3.16

0.62 2.00 4.02 6.61 9.76

0.52 1.04 1.57 2.09 2.61

0.40 1.28 2.58 4.24 6.25

3 3'/2 4 4% 5

4.40 5.14 5.87 6.61 7.35

19.34 25.36 32.09 39.51 47.61

4.12 4.81 5.50 6.19 6.87

16.48 21.61 27.33 33.65 40.52

3.79 4.42 5.05 5.68 6.31

13.42 17.59 22.25 27.39 32.99

3.13 3.66 4.18 4.70 5.22

8.59 11.25 14.22 17.50 21.07

3 3% 4 4th 5

8.81 10.3 11.8 13.2 14.7

65.79 86.57 109.9 135.6 163.8

825 9.62 11 .O 124 13.8

56.02 73.69 93.50 115.4 139.4

7.59 8.84 10.1 11.4 12.6

45.57 59.93 76.03 93.82 113.3

6.26 7.31 8.35 9.40 10.4

29.09 38.23 48.47 59.79 72.16

6 7

6 7 8 9 10

I/ 1 Ill2

2 2'12

8 9 10

%I lnch

Friction of Water (Eased on Darcy's Formula)

Copper and Brass Pipe 34 lnch

Copper Tubing-*S.P.S.

Flow

-

US gal per min

.

Type K t u b ~ n g

Type L t u b ~ n g

Type M tublng

4 0 2 inside d ~ a 0 4 9 wall thk

430" ~ n s ~ d e~ a 035" wall th k

450 ~ n s ~ d e~ a 025 wall thk

Veloc~ty ftisec

Head loss W100 fl

Veloclty ftisec

Head loss tV100 ft

Veloc~ty ftisec

Head loss N 1 0 0 ft

Flow -

Type M tubing

,690" inside d ~ a . 0 3 0 wall thk

loss

Veloc~ty ftlsec

Head loss fUl00 fl

Flow

-

niioo

n

'Pipe Flow

-

I 1 Velocity itisec

U S gal per mln

051 101 152 202 2 52

0.66 2.15 4.29 7.02 10.32

0 44 0 88 1 33 1 77 2 20

0.48 1.57 3.12 5.11 7.50

0 40 0 81 1 21 1 61 201

0.39 1.27 2.52 4.12 6.05

0 34 0 67 1 00 1 34 1 68

0.26 0.82 1.63 2.66 3.89

02 04 06 08 1

ll/z 2 2'/2 3

3 78 504 6 30 7 55

20.86 34.48 51.03 70.38

3 30 440 5 50 6 60

15.15 20.03 37.01 51.02

3 02 402 5 03 6 04

12.21 20.16 29.80 41.07

2 51 335 4 19 5 02

7.84 12.94 19 11 26 32

I l/2 2 2'2 3

3'12

8 82 10 I 11 4 126

92.44 117.1 144.4 174.3

7 70 8 80 9 90 110

66.98 84.85 104.6 126.1

7 04 8 05 9 05 10 05

53.90 68.26 84.1 1 101.4

5 86 6 70 7 53 8 36

34 52 43.70 53.82 64.87

3l2 4 4'2 5

4M 5

Type L tubing

.666" ins~dedia , 0 4 2 wall th k

Head

Pipe

494' ~ n s ~ d dla e 0905 wall thk

02 04 06 08 1

4

Type K t u b ~ n g

,652" inside dia ,049" wall thk

Calculations on pages 3-34 to 3-48 are by lngersoll-Rand Co. Note No allowance has been made for age, dlfference in diameter, or any abnormal condit~onof ~ n t e r ~ o r surface Any factor of safety must be est~matedfrom the local c o n d ~ t ~ o nand s the requirements of each PartlC~larlnstallatlon It IS recommended that for most commerc~aldes~gnpurposes a safety factor of 15 to 20% be added to the values In the tables-see page 3-5

Note: No allowance has been made for age, d~fferenceIn diameter, or any abnormal condition of Interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each Particular installation. It is recommended that for most commerc~aldesign purposes a safety factor of 15 to 2O0/o be added to the values in the tables-see page 3-5.


INGERSOLLRAND






Copper Tubing-*S.P.S. Copper and Brass Pipe 1l/4 lnch

Copper and Brass Pipe

Y4 lnch

I

Type K tublng

Type K t u b ~ n g

Type L t u b ~ n g

Type M t u b ~ n g

,745' ~ n s ~ d e~ a ,065'' wall thk

,785'' ~ n s ~ d dia e 045" wall thk

.811" ~ n s ~ dd e~ a .032" wall thk

Flow

Pipe

A

Flow -

US gal per mln

Ielocity ftisec

1 2 3 4 5

Head loss WlOO A

3.73 6.1 6

2 94

8 2 2 ~ n s ~ d e~ a 114" wall thk

Flow

Head loss W100 ft

gal Per min

Head Veloc~ty ftisec

loss W100 ft

Velocity ftisec

0 66 1.33 1.99 2.65 3.31

0.44 1.44 2.91 4.81 7.1 1

0.62 1.24 1.86 2.48 3 10

0.38 1.23 2.49 4.12 6.09

0.60 1.21 1.81 2.42 3.02

0.35 1.16 2.34 3.86 5.71

3.98 4.64 5.30 5.96 6.62

9.80 12.86 16.28 20.06 24.19

3.72 4 34 4.96 5.59 6.20

8.39 11.01 13.94 17.17 20.70

3.62 4.23 4.83 5.44 6.04

7.86 10.32 13.07 16.10 19.41

7.29 7.95 8.61 9 27 9.94

28.66 33.47 38.61 44.07 49.86

6.82 7.44 8.06 8.68 9.30

24.52 28.63 33.02 37.69 42.64

6.64 7.25 7.85 8 45 9 05

22.99 26.84 30.96 35.33 39.97

10.6 11.25 11.92

55.97 62.39 69.13

9.92 10.55 11 17

47.86 53.35 59.10

9.65 10.25 10.85

44.86 50.00 55.40

U S

US g a1 per mln

1 245" Inside d ~ a , 0 6 5 wall thk Velocity ftisec

Head loss W100ft

Type M t u b ~ n g

1.265" i n s ~ d ed ~ a ,055" wall thk

1.291" Inside d ~ a . 0 4 2 wall th k

1.368" inside d ~ a 146" wall thk

Head loss W100R

Head loss W100ft

Head loss W100ft

US gal per mln

Veloc~ty ftlsec

Type K t u b ~ n g

I

Type L tublng

I

-

US gal per mln

1

,995" ~ n s ~ d e~ a ,065'' wall thk veloc~ty ftlsec

1

Head loss W100 ft

1

1.025" inside dia ,050" wall thk veloc~ty ftlsec

/

Head loss ft/100 ft

1

Velocity ftlsec

-

1.31 1.58 1.84 2.11 2.37

0.79 1.09 1.43 1.81 2.22

1.28 1.53 1.79 2.04 2.30

0.74 1.01 1.32 1.67 2.06

1.22 1.47 1.71 1.96 2.20

0.67 0.92 1.20 1.52 1.87

1.09 1.31 1 53 1.75 1.96

0.51 0.70 0.91 1.15 1.42

5 6 7 8 9

10 12 15 20 25

2.63 3.16 3.95 5.26 6.58

2.67 3.69 5.47 9.13 13.59

2.55 3.06 3.83 5.10 6.38

2.48 3.42 5.07 8.46 12.59

2.45 2.93 3.66 4.89 6.11

2.25 3.10 4.60 7.67 11.42

2.18 2.62 3.27 4.36 5.46

1.71 2.35 3.49 5.81 8.65

10 12 15 20 25

30 35 40 45 50

7.90 9.21 10.5 11.8 13.2

18.83 24.83 31.57 38.03 47.20

7.65 8.94 10.2 11.5 12.8

17.44 23.00 29.24 36.15 43.71

7.33 8.55 9.77 11.0 12.2

15.82 20.86 26.51 32.77 39.63

6.55 7.65 8.74 9.83 10.9

11.98 15.79 20.06 24.80 29.98

30 35 40 45 50

60 70 80 90 100

15.8 18.4 21.1 23.7 26.3

65.65 86.82 110.7 137.2 166.3

15.3 17.9 20.4 23.0 25.5

60.78 80.38 102.5 127.0 153.9

14.7 17.1 19.6 22.0 24.4

55.10 72.86 92.85 115.1 139.4

41.66 55.07 70.16 86.91 105.3

60 70 80 90 100

13.1 15.3 17.5 19.6 21.8

1112 ' lnch Type M t u b ~ n p

I

I

'Pipe

Flow Flow

Veloc~ty ftisec

Flow

5 6 7 8 9

1 lnch

(

Pipe

Type L t u b ~ n g

1.055" i n s ~ d ed ~ a ,035" wall thk e o c i t ftisec

1

Head loss W100 f l

1

1.062" i n s ~ d ed ~ a 1 2 6 5 wall thk e o c t ftisec

1

Head loss W100 ft

Flow

1

-

LJ - S -

gal ppr mln

-

US gal per mln

Type L tubing

Type M tubing

Pipe

1.481" inside dia ,072" wall thk

1.505" i n s ~ d edia ,060" wall thk

1.527" Inside dia . 0 4 9 wall thk


Velocity ftlsec

Head loss tVlOOtt

Velocity ftlsec

Head loss Wl00n

Velocity ftlsec

Head loss tV100ft

Veloclty ftlsec

Head loss W100fi

Flow

-

US gal per mln

9 10 12 15

1.49 1.67 1.86 2.23 2.79

0.79 0.97 1.17 1.61 2.39

1.44 1.62 1.80 2.16 2.70

0.73 0.90 1.08 1.49 2.21

1.40 1.57 1.75 210 2.63

0.68 0.84 1.01 1.39 2.07

1.27 1 43 1.59 1.91 2.39

0.55 0.67 0.81 1.12 1.65

8 9 10 12 15

20 25 30 35 40

3.72 4.65 5.58 6.51 7.44

3.98 5.91 8.19 10.79 13.70

3.60 4.51 5.41 6.31 7.21

3.68 5.48 7.58 9.99 12.68

3.50 4.38 5.25 6.13 7.00

3.44 5.1 1 7.07 9.31 11.83

3.19 3.98 4.78 5.58 6.37

2.75 4.09 5.65 7.45 9.45

20 25 30 35 40

45

60 70 80 90

837 9.30 11.2 13.0 14.9 16.7

16.93 20.46 28.42 37.55 47.82 59.21

8.11 9.01 10.8 12.6 14.4 16 2

15.67 18.94 26.30 34.74 44.24 54.78

7.88 8.76 10.5 12.3 14 0 15 8

14.61 17.66 24.53 32.40 41.25 51.07

7.16 7.96 9 56 11.2 12.8 14 4

11.68 14.11 19.59 25.87 32.93 40.76

45 50 60 70 80 90

100 110 120 130

18.6 20.5 22.3 24 2

71.70 85.29 99.95 115.7

18.0 19.8 21.6 23.4

66.34 78.90 92.46 107.0

17.5 19.3 21.0 22.8

61.84 73.55 86.18 99.73

15 9 17 5 19.1 20.7

49.34 58.67 68.74 79.53

100 110 120 130

8

50

Note: No allowance has been made for age, difference In diameter, or any abnormal c o n d ~ t ~ oof n ~nter~or surface. Any factor of safety must be estimated from the local conditions and the requirements of each Particular installation It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

Type K tubing

Note: No allowance has been made for age, difference in d~ameter,or any abnormal condition of ~nterior surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It IS recommended that for most commerc~aldesign purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

INGERSOLLRAND






Copper Tubing-'S.P.S.


21/2

2 lnch

Flow

-

US gal per rnln

Type L t u b ~ n g

Type M t u b ~ n g

Pipe

1 959" ~ n s ~ dd e~ a 083" wall thk

1.985" ~ n s ~ d e~ a .070" wall thk

2.009' ~ n s ~ d e~ a 058' wall thk

2 062" Inside d ~ a .1565' wall thk

Veloc~ty ftisec

Head loss WlOO fl

Veloc~ty ft:sec

Head loss W100 fl

Veloc~ty ft!sec

Head loss f11100 ft

Veloclty ftssec

Type L tubing

Type K t u b ~ n g

Type K t u b ~ n g

Flow -

Head loss WlOO ft

US gal per mln

Type M tu b ~ n g

*

Pipe

-

2.435" i n s ~ d ed ~ a .095" wall thk

2.465" ~ n s ~ d e~ a .080" wall thk

2.495" i n s ~ d ed ~ a .065" wall thk

2.500" ~ n s ~ dd e~ a 1875" wall thk

US gal per mln

Veloc~ty ftlsec

Head loss ft/100 A

Head loss tt1100 A

Head loss W100 ft

Head loss f11100 A

U S gal per rnln

Flow

Veloc~ty ftlsec

Veloc~ty ftisec

Veloc~ty ftlsec

Flow -

1.34 1.68 2.02 2.35 2.69 3.02

0.35 0.52 0.72 0.94 1.19 1.47

1.31 1.64 1.97 2.30 2.62 2.95

0.33 0.49 0.68 0.89 1.13 1.39

1.31 1.63 1.96 2.29 2.61 2.94

0.33 0.49 0.67 0.88 1.12 1.38

20 25 30 35 40 45

1.88 2.61 3.43 4.36 5.39 6.52

3.36 4.03 4.70 5.37 6.04 6.71

1.77 2.46 3.24 4.12 5.08 6.15

3.28 3.93 4.59 525 5.90 6.55

1.68 2.32 3.06 3.88 4.80 5.80

3.26 3.92 4.57 5.22 5.88 6.53

1.66 2.30 3.03 3.85 4.75 5.74

50 60 70 80 90 100

7.58 8.27 8.96 9.65

7.74 9.06 10.46 11.97

7.38 8 05 8.73 9.40

7.30 8.54 9.87 11.28

7.21 7.86 8.52 9.18

6.89 8.05 9.31 10.64

7.19 7.84 8.49 9.14

6.82 7.98 9.22 10.54

110 120 130 140

150 160 170 180 190

10.35 11.0 11.7 12.4 13.1

13.56 15.24 17.01 18.87 20.81

10.1 10.8 11.4 12.1 12 8

12.78 14.36 16.03 17.79 19.62

9.83 10.5 11.1 11.8 12.5

12.06 13.55 15.12 16.78 18.51

9.79 10.45 11.1 11.8 12.4

11.94 13.42 14.98 16.61 18.33

150 160 170 180 190

200 220 240 260 280

13.8 15.2 16.5 17.9 19.3

22.85 27.18 31.84 36.85 42.19

13.4 14.8 16.1 17.5 18.8

21.54 25.61 30.01 34.73 39.76

13.1 14.4 15.7 17.1 18.4

20.31 24.16 28.31 32.75 37.50

13.1 14.4 15.7 17.0 18.3

20.12 23.93 28.03 32.44 37.13

200 220 240 260 280

300 320 340 360 380

20.7 22.1 23.4 24.8 26.2

47.86 53.86 60.18 66.83 73.80

20.1 21.5 22.8 24.2 25.5

45.10 50.75 56.71 62.97 69.54

19.7 21.0 22.3 23.6 24.9

42.53 47.86 53.48 59.38 65.57

19.6 20.9 22.2 23.5 24.8

42.12 47.40 52.96 58.81 64.94

300 320 340 300 380

400 420 440 460 480

27.6 29.0 30.3 31.7 33.1

81.09 88.70 96.62 104.9 113.4

26.9 28 2 29 5 30.9 32 2

76.41 83.57 91.04 98.80 106.8

26.2 27.5 28.8 30 2 31.5

72.04 78.80 85.83 93.15 100.7

26.1 27.4 28.7 30 0 31.4

71.35 78.04 85.00 92.24 99.76

400 420 440 460 480

500

34.5

122.3

33 6

115.2

32 8

108.6

32 6

10 12 14 16 18

1.07 1.28 149 170 1.92

0.31 0.43 0.56 0.71 0.87

1 04 1.24 1.45 1.66 1.87

0.29 0.40 0.52 0.66 0.82

1.01 1.21 1 42 1.62 1.82

0.27 0.38 0.50 0.63 0.77

.96 1 15 1 34 1 53 1 72

0.24 0.33 0.44 0.55 0.68

10 12 14 16 18

20 25 30 35 40 45

1.38 1.72 2.07 2.41 2.76 3.10

0.37 0.55 0.76 1.00 1.26 1.56

20 25 30 35 40 45

2.13 2.66 3.19 3.73 4.26 4.79

1.05 1.55 2.15 2.82 3.58 4.42

2.07 2.59 311 3 62 4.14 4.66

0.98 1.46 2.01 2.65 3.36 4.15

2.02 2.53 3.03 3 54 4.05 4 55

0.93 1.38 1.90 2.50 3.17 3.92

1.92 2 39 2 87 3.35 3.83 4.30

0.82 1.22 1.68 2.21 2.80 3.46

20 25 30 35 40 45

50 60 70 80 90 100

3.45 4.14 4.82 5.51 6.20 6.89

50 60 70 80 90

5.32 6.39 7.45 8.52 958

5.34 7.40 9.76 12.4' 15.36

5.17 6.21 7.25 8.28 9.31

5.01 6.95 9.16 11.65 14.41

5 05 6 06 7.07 8.09 910

4.73 6.56 8.65 11.00 13.60

4.80 5.75 6.70 7.65 861

4.17 5.79 7.63 9.70 12.00

50 60 70 80 90

110 120 130 140

I00 110 120 130 140

10.65 11.71 12.78 13.85 14.9

18.58 22.07 25.84 29.88 34.18

10.4 11.4 12.4 13 4 14.5

17.43 20.71 24.25 28.04 32.07

10.1 11 1 12 1 13 1 14.2

16.45 19.55 22.88 26.45 30.26

9.57 10.5 11.5 12.5 13 4

14.51 17.24 20.18 23.33 26.69

100 110 120 130 140

150 160 170 180 190

16.0 17.0 18 1 192 20.2

38.75 43.58 48.67 54.01 59.61

15.5 16.5 17.6 18.6 19.6

36.36 40.89 45.66 50.67 55.92

15 2 16.2 17.2 18.2 19.2

34.30 38.58 43.08 47.81 52.76

14 4 15 3 16 3 17 2 18.2

30.25 34.01 37.98 42.15 46.51

150 160 170 180 190

200 210 220 230 240

21.3 22.4 23.4 24.5 25.6

65.46 71.57 77.93 84.53 91.38

20.7 217 22 8 23 8 24 8

61.41 67.14 73.10 79.29 55.72

20 2 21.2 22.2 23 2 24.3

57.94 63.34 68.96 74.80 80.86

19.2 20.1 21 .O 22 0 23 0

51.07 55.83 60.78 65.93 71.26

200 210 220 230 240

250 260 270 280 290 300

26.6 27.7 28.8 29.8 30 9 32.0

98.43 105.8 113.4 121.3 129.3 137.6

25.9 26.9 27.9 29.0 30.0 31 1

92.37 99.26 106.4 113.7 121.3 129.1

25.3 26.3 273 28.3 29.4 30.4

87.14 93.63 100.3 107.3 114.4 121.8

23.9 24 9 258 26 8 27 8 28 7

76.79 82.51 88.42 94.52 100.8 107.3

250 260 270 280 290 300

Note: No allowance has been made for age, difference In diameter, or any abnormal c o n d ~ t ~ oofn Interlor surface. Any factor of safety must be est~rnatedfrom the local c o n d ~ t ~ o nand s the requirements of each particular lnstallat~on.It is recommended that for most comrnerc~ald e s ~ g npurposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

Copper and Brass Pipe lnch

.

107.5

500

Note: No allowance has been made for age, difference In d~ameter,or any abnormal c o n d ~ t ~ oofn Interior surface. Any factor of safety must be est~matedfrom the local conditions and the requirements of each particular installation. It IS recommended that for most cornrnerc~ald e s ~ g npurposes a safety factor of 1 5 to 20% be added to the values in the tables-see page 3-5.

FRICTION








3% lnch

3 lnch

I Flow -

US gal per mln

Type K t u b ~ n g

2.907"~ n s ~ d e~ a 109" wall thk

1

Type L t u b ~ n g

090"wall thk

I


Type M tublng

072" wall thk

1

3.062"~ n s ~ dd e~ a ,219"wall thk Vloclty ftlsec

Type K t u b ~ n g

I

'Pipe

1 7::

ft/100 ft

Flow Flow -

Us gal Per mln


US gal per mln

Type L tubing

Pipe

Type M tublng

3.385"inside d ~ a 1 2 0 wall thk

3.425ins~ded ~ a

3 459 ins~ded ~ a ,083wall th k

Head loss ftI100 R

Head loss ill100 ft

Velocity ftlsec

Head loss ill100 ft 0.49 0.64 0.81 1.00

2.00 2.33 2.66 3.00

0.46 0.60 0.77 0.95

60 70 80 90

1.21 1.43 1.68 1.93 2.21

3.33 3.67 4.00 4.33 4.66

1.14 1.35 1.58 1.83 2.09

I00 110 120 130 140

Veloc~ty ttlsec

.loo"wall thk

Veloc~ty ftlsec

3.500 ~ n s ~ ddia e .250wall thk Velocity ftlsec

Head loss ill100 R

Flow

-

US gal per mln

60 70 80 90

2.14 2.49 2.84 3.20

0.54 0.71 0.90 1.11

2.09 2.44 2 78 3.13

0.51 0.67 0.85 1.05

2 05 2.39 2.73 3.07

100 110 120 130 140

3.56 3.92 4.26 4.62 4.98

1.34 1.59 1.86 2.15 2.45

3.48 3.82 4.18 4.52 4.87

1.27 1.50 1.76 2.03 2.32

3.41 3.76 4.10 4.45 4.79

150 160 170 180 190

5.34 5.69 6.05 6.40 6.76

2.78 3.12 3.48 3.86 4.25

5.21 5.56 5.91 6.26 6.60

2.62 2.95 3.29 3.64 4.02

5.12 5.46 5.80 6.16 6.49

2.50 2.81 3.14 3.48 3.83

5.00 5.33 5.66 6.00 6.33

2.36 2.66 2.96 3.28 3.62

150 160 170 180 190

200 220 240 260 280

7.11 7.82 8.54 9.25 9.95

4.67 5.54 6.49 7.50 8.58

6.95 7.65 8.35 9.05 9.74

4.41 5.24 6.13 7.09 8.11

6.82 7.51 8.19 8.87 9.55

4.20 4.99 5.85 6.76 7.73

6.66 7.33 8.00 8.66 9.33

3.97 4.72 5.52 6.39 7.30

200 220 240 260 280

'

300 350 400 450 500

10.7 12.5 14.2 16.0 17.8

9.73 12.87 16.42 20.36 24.68

10.4 12.2 13.9 15.6 17 4

9.19 12.16 15.51 19.23 23.32

10.2 11.9 13.7 15.4 17.1

8.76 11.60 14.79 18.33 22.23

10.0 11.7 13.3 15.0 16.7

8.28 10.95 13.97 17.32 20.99

300 350 400 450 500

550 600 650 700

19.6 21.4 23.1 24.9

29.39 34.47 39.92 45.75

19.1 20.9 22.6 24.4

27.76 32.56 37.71 43.21

18.8 20.5 22.2 23.9

26.46 31.04 35.94 41.18

18.3 20.0 21.6 23.3

24.99 29.31 33.95 38.89

550 600 650 700

750 800 850 900 950

26.6 28.4 30.2 32.0 33.8

51.94 58.49 65.40 72.68 80.31

26.1 27.8 29.6 31.3 33.0

49.05 55.24 61.77 68.63 75.84

25.6 27.3 29.0 30.7 32.4

46.75 52.65 58.87 65.41 72.27

25.0 26.6 28.3 30.0 31.6

44.15 49.72 55.59 61.77 68.24

750 800 850 900 950

1000 1100 1200 1300 1400

35.6 39.2 42.6 46.2 49.8

88.29 105.3 123.7 143.5 164.7

34.8 38.2 41.8 45.2 48.7

83.37 99.45 116.8 135.5 155.5

34.1 37.6 41.0 44.5 47.9

79.46 94.77 111.3 129.1 148.2

33.3 36.7 40.0 43.3 46.6

75.02 89.47 105.1 121.9 139.9

1000 1100 1200 1300 1400

Note: No allowance has been made for age, difference In diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It is recommended that for most commerc~aldesign purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

INGERSOLLRAND CAMERON HYDRAULIC DATA Friction of Water (Continued)







5 lnch

4 lnch Type K tubing Flow

-

US gal per min

3.857" ins~dedia 1 3 4 " wall thk Velocity ftlsec

Head loss W100 fi

Type L t u b ~ n g

3.905" inside dia 1 1 0 " wall thk Veloc~ty ftisec

Head loss fVlOO ft


Type M tubing

Pipe

3.935" ~ n s ~ d dia e .095" wall thk

4 . 0 0 0 i n s ~ d edia ,250'' wall thk

Velocity ftlsec

Head loss W l 0 0 fi

Velocity ftisec

Head loss W100 n

Flow

Flow

Us gal per mln

us .

-

-

gal per

mln

Type K tubing

Type L tubing

Type M tubing

Pipe

4.805" inside dia 160" wall thk

4.875 inside dia 1 2 5 wall thk

4.907" inside dia 1 0 9 wall thk


Velocity ftisec

Head loss fU1W ft

Velocity ftisec

Head loss fUlOO ft

Velocity ftisec

Head loss fU100 ft

Velocity ftisec

Head loss fU100 ft

Flow

US gal per min

0.68 0.80 0.94 1.08 1.23

2 64 2.90 3.16 3.42 3.69

0.65 0.77 0.90 1.04 1.19

2.55 2.81 3.06 3.31 3.57

0.60 0.71 0.83 0.96 1.10

100 110 120 130 140

150 160 170 180 190

2.64 2.82 3.00 3.17 3.35

0.52 0.58 0.65 0.72 0.79

2.58 2.75 2.92 3 09 3.26

0.48 0.54 0.60 0.67 0.74

2.53 2.70 2.87 3.04 3.21

0.47 0.52 0.58 0.65 0.71

2.38 2.54 2.70 2.86 3.02

0.40 0.45 0.50 0.56 0.61

150 160 170 180 190

4.28 4 55 4 81 5.08

1.40 1.57 1.75 1.94 2.14

3.95 4.21 4 48 4.74 5.00

1.35 1.51 1.69 1.87 2.06

3.83 4.08 4.33 4.58 4.84

1.25 1.39 1.56 1.73 1.91

150 160 170 180 190

200 220 240 260 280

3.53 3.88 4.24 4.59 4.94

0.87 1.03 1.20 1.39 1.59

3 44 3 78 4.12 4.46 4.81

0.81 0.96 1.12 1.30 1.48

3.38 3.72 4.05 4.39 4.73

0.78 0.93 1.09 1.26 1.43

3.18 3.50 3.81 4.14 4.45

0.67 0.80 0.94 1.08 1.23

200 220 240 260 280

2.49 2.96 3.46 4.00 4.57

5.35 5 89 6.42 6.95 7.49

2.35 2.79 3.26 3.77 4.31

5.27 5.80 6.32 6.85 7.38

2.26 2.68 3.14 3.63 4.15

5.10 5.61 6.12 6.63 7.14

2.09 2.48 2.90 3.36 3.84

200 220 240 260 280

300 350 400 450

5.29 6.17 7.05 7.94

1.80 2.38 3.03 3.75

5.15 6.01 6.87 7 73

1.68 2.22 2.82 3.49

5.07 5.91 6.75 7.60

1.63 2.15 2.73 3.39

4.76 5.56 6.35 7.15

1.40 1.85 2.35 2.91

300 350 400 450

8.24 9.60 11 0 12.4 13 7

5.18 6.85 8.74 10.83 13.12

8.02 9.36 10.7 12.0 13.4

4.88 6.46 8.23 10.20 12.36

7.90 9.22 10.5 11.9 13 2

4.70 6.22 7.93 9.83 11.91

7.65 8.92 10.2 11.5 12.8

4.35 5.75 7.33 9.08 11.00

300 350 400 450 500

500 550 600 650 700

8.81 9.70 10.6 11.5 12.4

4.54 5.40 6.32 7.32 8.37

8.59 9.45 10.3 11.2 12.0

4.23 5.03 5.90 6.82 7.81

8.45 9 29 10.1 11.O 11.8

4.10 4.88 5.71 6.61 7.57

7 95 8.75 9.54 10.3 11.1

3.53 4.19 4.91 5.68 6.50

500 550 600 650 700

550 600 650 700 750

15.1 16.5 17.9 19.2 20.6

15.61 18.31 21.19 24.28 27.55

14.7 16.0 17.4 18.7 20.1

14.71 17.24 19.96 22.86 25.95

14.5 15.8 17.1 18.4 19.8

14.17 16.61 19.23 22.03 25.00

14.1 15.3 16.6 17.9 19.1

13.09 15.35 17.77 20.35 23.09

550 600 650. 700 750

750 800 850 900 950

13.2 14.1 15.0 15.9 16.8

9.50 10.69 11.94 13.26 14.64

12.9 13.7 14.6 15.5 16.3

8.86 9.97 11.13 12.36 13.67

12.7 13.5 14.4 15.2 16.1

8.58 9.65 10.79 11.98 13.22

11 9 12.7 13.5 14.3 15.1

7.38 8.30 9.27 10.29 11.36

750 800 850 900 950

800 850 900 950 1000 1100

22.0 23.3 24.7 26 1 27.4 30.2

31.01 34.67 38.51 42.54 46.76 55.74

21.4 22.8 24.1 25.4 26.8 29.4

29.21 32.65 36.27 40.06 44.03 52.48

21.1 22.4 23.7 25.0 26.4 29.0

28.14 31.46 34.94 38.60 42.42 50.56

20.4 21.7 23.0 24.2 25.5 28.1

25.99 29.05 32.27 35.64 39.17 46.69

800 850 900 950 1000 1100

1000 1100 1200 1300 1400

17.6 19.4 21.2 22.9 24.7

16.08 19.16 22.48 26.04 29.85

17.2 18.9 20.6 22.4 24.0

14.99 17.86 20.95 24.27 27.82

16.9 18.6 20.3 22.0 23.7

14.52 17.30 20.30 23.51 26.95

15.9 17.5 19.1 20.6 22.2

12.48 14.86 17.44 20.20 23.15

1000 1100 1200 1300 1400

1200 1300 1400

32.9 35.7 38.4

65.45 75.89 87.05

32.1 34.8 37.4

61.62 71.45 81.95

31.6 34.2 36.9

59.37 68.83 78.95

30.6 33.1 35.7

54.82 63.55 72.89

1200 1300 1400

1500 1600 1800 2000 2200

26.4 28.2 31.8 35.3 38.8

33.89 38.18 47.46 57.68 68.82

25.8 27.5 30.9 34.4 37.8

31.59 35.59 44.23 53.75 64.13

25.4 27.0 30.4 33.8 37 2

30.60 34.47 42.85 52.06 62.12

23.8 25.4 28.6 31.8 35.0

26.28 29.60 36.79 44.70 53.32

1500 1600 1800 2000 2200

1500 1600 1800 2000 2200

41.1 43 9 49.4 54.9 60.4

98.23 111.5 138.8 168.9 201.7

40.1 42.8 48.1 53 5 58.9

93.13 105.0 130.6 158.9 189.8

39.5 42.1 47.4 52.7 580

89.71 101.1 125.8 153.1 182.8

38.3 40.8 45.8 51.0 56.1

82.82 93.34 116.1 141.3 168.7

1500 1600 1800 2000 2200

2400 2600 2800 3000

42.4 45.9 49.4 52.9

80.89 93.86 107.7 122.5

41.2 44.6 48.1 51.5

75.37 87.45 100.4 114.1

40 5 44 0 473 50.7

73.00 84.70 97.21 110.5

38.1 41.4 44.5 47.6

62.65 72.69 83.42 94.84

2400 2600 2800 3000

100 110 120 130 140

2 74 302 3 29 3.57 3.84

0.72 0.85 0.99 1.15 1.31

150 160 170 180 190

4.11 4.39 4.66 4.94 5.21

1.48 1.67 1.86 2.06 2.27

200 220 240 260 280

5.49 6.04 6.59 7.14 7.69

300 350 400 450 500

2.68 2.94 3.21 348

::::1


Note: No allowance has been made for age, difference in diameter, or any abnormal condit~onof Interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5

INGERSOLL-RAND CAMERON HYDRAULIC DATA Friction of Water (Continued)

Friction of Water (Continued) (Based on Darcy's Formula)



Copper Tubing-'S.P.S.


12 lnch

10 lnch Flow

-

-

US gal per mln

Type K tublng

Type K tublng

'P ~ p e

Type M t u b ~ n g

Type L tubrng

Flow

9 449 ~ n s l d ed ~ a Veloc~ty ftisec

Head loss fU100 ft

9 700 ~nslded ~ a

9 625 l n s ~ d ed ~ a Veloclty ftisec

Head loss tUlOO ft

10 020 ~ n s l d edla

-

US gal per mln

US gal per mln

Veloc~ty ftisec

Head loss it1100 tt

2 17 2 39 2 61 2 82 3 04

0.15 0.18 0.21 0.25 0.28

2 03 2 24 2 44 2 65 2 85

0.13 0.16 0.18 0.21 0.24

500 550 600 6 50 700

Type L tublng

'P ~ p e

Type M tublng

Flow

Flow

-

Head loss fU100 ft

Velocity ftlsec


11 31 5 ' ~ n s ~ d e~ a Velocity ftisec

11 565 ~ n s ~ d e~ a

Head loss fU100 ll

Veloc~ty ftisec

Head loss fU100 ft

11 617 ~ n s ~ d e~ a Veloc~ty ftlsec

Head loss ft1100 it

12 000 lnslde d ~ a Veloc~ty ftisec

Head loss ftilOO ft

-

Us gal per mln

800

2.55

0.17

2.44

0.16

242

0.15

2.27

0.13

800

750 800 850 900 950

1500 1600 1800

4.79 5.11 5 74

0.54 0.60 0.75

4.58 4.89 5.50

0.48 0.54 0.67

4.54 4.84 5.45

0.47 0.53 0.66

426 4.54 5 11

0.40 0.45 0.56

1500 1600 1800

0.46 0.50 0.59 0.68 0.78

1000 1100 1200 1300 1400

2000 2200 2400 2600 2800

6.38 7.02 7.66 8.30 8.93

0.91 1.08 1.26 1.46 1.68

6.11 6.72 7.33 7.94 8 55

0.82 0.97 1.14 1.32 1.51

6.05 6.66 7.27 7.87 8.48

0.80 0.95 1.11 1.29 1.48

5.67 6.24 6.81 7.38 7.94

0.68 0.81 0.95 1.10 1.26

2000 2200 2400 2600 2800

589 6 28 7 32 8 14 8 95

0.89 1.00 1.35 1.63 1.94

1500 1600 1800 2000 2200

3000 3500 4000 4500 5000

9.57 11.2 12.8 14.4 16.0

1.90 2.52 3.22 4.00 4.86

9.16 10.7 12.2 13.7 15.3

1.71 2.27 2.90 3.60 4.37

9.08 10.6 12.1 13.6 15.1

1.67 2.22 2.84 3.52 4.27

8.51 9 93 11.3 12.8 14.2

1.43 1.90 2.42 3.01 3.65

3000 3500 4000 4500 5000

2.66 3.08 3.53 4.01 5.32

9 77 10 6 11 4 12 2 14 2

2.28 2.63 3.02 3.42 4.55

2400 2600 2800 3000 3500

5500 6000 6500 7000 7500

17.5 19.1 20.7 22.3 23.9

5.79 6.80 7.88 9.04 10.27

16.8 18.3 19.9 21.4 22.9

5.21 6.11 7.09 8.13 9.23

16.6 18.2 19.7 21.2 22.7

5.10 5.98 6.93 7.95 9.03

15.6 17 0 18.4 19.6 21 3

4.35 5.11 5.92 6.79 7.71

5500 6000 6500 7000 7500

17 4 19 5 21 7 23 9 26 1

6.80 8.45 10.26 12.24 14.38

16 3 18 3 20 3 22 4 24 4

5.81 7.22 8.77 10.45 12.28

4000 4500 5000 5500 6000

8000 8500 9000 9500 10,000

25.5 271 28 7 303 31.9

11.57 12.95 14.39 15.91 17.50

24.4 26.0 27.5 29.0 30.5

10.40 11.64 12.94 14.31 15.73

24 2 25 7 27 2 28.8 30.7

10.18 11.39 12.66 14.00 15.39

22 7 24 1 25.5 270 28.4

8.69 9.72 10.81 11.95 13.14

8000 8500 9000 9500 10,000

17.32 19.87 22.59 25.46 28.50

28 2 30 4 32 6 34 7 36 9

16.68 19.13 21.75 24.52 27.44

26 4 28 5 30 5 32 6 34 6

14.24 16.33 18.56 20.92 23.42

6500 7000 7500 8000 8500

10,500 11,000 11,500 12,000 12,500

33.5 35 1 36 7 38.3 39.9

19.17 20.90 22.70 24.57 26.51

32.1 33.6 35 1 36.7 38 2

17.23 18.78 20.40 22.08 23.83

31.8 33.3 34.8 36.3 37 8

16.85 18.38 19.96 21.60 23.31

29 8 31 2 32 6 34.0 35 5

14.39 15.69 17.04 18.44 19.89

10,500 11.000 11,500 12.000 12,500

31.70 35.06 38.57

39 1 41 2 43 4

30.52 33.75 37.14

36 6 38 7 40 7

26.05 28.80 31.69

9000 9500 10,000

13,000 14,000 15.000

41 5 44.7 47.9

28.52 32.75 37.25

39.7 42.8 45 8

25.63 29.43 33.47

39.4 42 4 45.4

25.08 28.79 32.75

36 9 39 7 42.6

21.40 24.57 27.94

13.000 14.000 15.000

500 550 600 650 700

229 2 52 2 75 2 97 3 20

0.18 0.21 0.24 0.28 0.32

221 2 43 2 65 2 87 3 09

0.16 0.19 0.22 0.26 0.29

750 800 850 900 950-

3 43 3 66 3 89 4 12 435

0.36 0.41 0.46 0.51 0.56

3 31 3 53 3 75 3 97 419

0.33 0.37 0.42 0.46 0.51

3 26 3 47 3 69 3 91 413

0.32 0.36 0.40 0.45 0.49

3 05 3 26 3 46 3 66 387

0.27 0.31 0.34 0.38 0.42

1000 1100 1200 1300 1400

4 56 5 03 5 49 5 95 641

0.61 0.73 0.85 0.99 1.13

4 41 4 48 5 29 5 73 617

0.56 0.67 0.78 0.90 1.03

4 34 4 78 5 21 5 64 608

0.54 0.64 0.75 0.87 1.00

4 07 4 32 4 71 5 10 550

1500 1600 1800 2000 2200

6 86 7 32 8 24 9 15 10 1

1.28 1.44 1.79 2.17 2.58

6 61 7 06 7 94 8 82 9 70

1.17 1.32 1.63 1.98 2.36

6 51 6 95 7 82 8 68 9 55

1.13 1.27 1.57 1.91 2.27

2400 2600 2800 3000 3500

11 0 11 9 12 8 13 7 16 0

3.02 3.50 4.01 4.55 6.04

10 6 11 5 12 3 132 15 4

2.76 3.20 3.67 4.16 5.52

10 4 11 3 12 2 13 0 15 2

4000 4500 5000 5500 6000

18 3 206 22 9 25 2 27 5

7.72 9.60 11.66 13.91 16.34

17 6 19 8 22 0 24 3 26 5

7.06 8.78 10.66 12.71 14.93

6500 7000 7500 8000 8500

29 7 32 0 34 3 36 6 38 9

18.95 21.74 24.71 27.86 31.19

28 7 30 9 33 1 35 3 37 5

9000 9500 10 000

41 2 43 5 45 6

34.69 38.37 42.22

39 7 41 9 44 I

p~

-

Note: No allowance has been made for age, dlfference In diameter, or any abnormal condltlon of Interlor surface Any factor of safety must be estimated from the local condltlons and the requlrernents of each particular ~nstallation.It IS recommended that for most commerc~aldesign purposes a safety factor of 15 to 20°h be added to the values In the tables-see page 3-5

-

Note: No allowance has been made for age, d~fferenceIn diameter, or any abnormal condition of Interior surface. Any factor of safety must be estimated from the local conditions and the requlrernents of each part~cularinstallation. It is recommended that for most commercial d e s ~ g npurposes a safety factor of 15 to 2OoA be added to the values in the tables-see page 3-5.

FRICTION

INGERSOLL-RAND CAMERON HYDRAULIC DATA

Friction Loss for Viscous Liquids (Continued)

Friction Loss for Viscous Liquids



Loss in Feet of Liquid per 1000 Feet of Pipe 1% lnch (1.610" inside dia) Sch 40 New Steel Pipe

Loss in Feet of Liquid per 1000 Feet of Pipe 1 lnch (1.049" inside dia) Sch 40 New Steel Pipe Kinematic viscosity-centistokes

-

Flow US nal

Bbl ner

0.6

1.1

2.1

2.7

4.3

7.4

10.3

13.1

15.7

206

Approx SSU viscosity

Kinematic viscosity-centistokes

- 26.4

Flow

US gal per min

Bbl per h r (42 gal)

32.0

43.2

65.0

108.4 Approx

. 125

I

I

I

1

I

I

1

150

1

200

1

300

1

500

162.3

216.5

325

435

650

SSU viscosity

1

750

1

1000

I

1500

I

2000

I

3000

For t h ~ spipe size: V = 0.1576 x gpm; h, = 0.000385gpm2. Figures in shaded area are laminar (viscous) flow. For velocity data see page 3-15 .

Calculations on pages 3-48to 3-88are by lngersoll-Rand CO. For velocity data see page 3-14. Note: No allowance has been made for age, d~fferencein diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It is recommended that for most commercial design purposes a safety factor of 15 t o 20°/0 be added to the values in the tables-see page 3-5.

Note: No allowance has been made for age, difference in diameter, or any abnormal cond~tionof interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each Particular installation. It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

FRICTION

INGERSOLLRAND CAMERON HYDRAULIC DATA

Friction Loss for. Viscous Liquids (Continued)




Loss in Feet of Liquid per 1000 Feet of Pipe 2 lnch (2.067" inside dia) Sch 40 New Steel Pipe


Klnematlc vlscoslty-cent~stokes Flow

Flow 2.1 .

-

I

~ a l

- .

per

I

2.7

4.3

7.4

10.3

13.1

15.7

26 4

20.6

US gal per mln


For this pipe size: V = 0.0956 x gpm; h, = 0.000142 gpm2. Figures in shaded area are laminar (viscous) flow. For velocity data see page 3-16.


I

Bbl per hr (42 gal)

32.0

65.C

43 2

Approx 125

150

200

1

300

162.3

108 4

(

500

216.5

325

435

650

SSU viscosity

1

750

1

1000

1

1500

1

2000

1

3000

Loss In lb per sq in = ,433 (sp gr) (flgures from table). Flgures in shaded area are laminar (VISCOUS) flow. For veloclty data see page 3-16.

Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requ~rementsof each particular installation. It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

CAMERON HYDRAULIC DATA Friction Loss for Viscous Liquids (Continued)





Loss in Feet of Liquid per 1000 Feet of Pipe 2% lnch (2.469 inside dia) Sch 40 New Steel Pipe


K~nematlcv~scos~ty-centstokes Flow

-

Per hr (42 gal)


31.5

33

35

40

50

60

70

80

100

US gal per mln

Bbl per hr (42 gal)

1

2 4 6 8

1.4 29 57 86 114

10 12 14 16 18

26.4

32 0

43 2

125

150

200

65 0

300

108.4

1623

216 5

325

435

650

1500

2000

3000

6.52 17.0 22.1 33.1 44.1

7.38 14.8 29.5 44.3

11.0 22.0 44.1 66.2

Approx SSU v~scos~ty

3.58

.54 1.09 2.17 3.28 4.34

14.3 17 1 200 22.8 257

4.48 5.38 6.27 7.16 8.06

5.43 6.51 7.60 8-68 Q.77

20 25 30 35 41,

286 35 7 42.9 50.0 57 1

8.96 11.2 13.4 15.7 17.9

45 50 60 70 80

64.3 71.4 85.7 100 114

33.0 392 54.0 70 0 87.7

.45 .90 1.79

2.W

70.9 13.6 16-3 19.0

27.7

.73 1.47

293 4.40 $87

7.33 8.80 10.3 11.7 13.2

500

750

1.84 3.68 7.36 11.0 14.7

2.75 5.50 11.0 16.5 22.0

11.0 73.2 15.4 17.6 19.8

18.4 22.1 25.7 a.4 XI.1

27.5 33.0 38.5 44.0 49.5

36.7

22.0

36.8 46.0

55.0

73.4 91.8 170 129 147

1.10 2.20 4.41 6.82 8.32

14.7 18.3 22*0 25.6 29.3

27.6 33,l 38.6 44.2

33.0 36.6 44.0 51.3

49.6 55.2 66.2 77.2

88.8

55.2

82.5 96.3

64.4 73.6

116

1000 3.67 7.35 14.7

22.0 29.4 44.1 5f.4 58.8 66.1

55.2 66.2 77.2 83,2 99.3

293

332 383

885

101

88.3

220

244

129 143 157 171 186

110 130 154 180 206

115 137 164 188 216

125 148 176 205 232

99.3 110

1 184

248 275

330

497

202

305 330 358

367 403

552

197 226 263

447 477

662

574 551

772 827 882 937 993

221 239

190 200 220 240 260

271 286 314 343 371

233 258 310 367 429

243 269 322 381 445

260 286 343 404 470

265 292 351 416 482

280 308 369 436 505

306 334 400 469 543

140 150 160 170 180

200 214 228 243 257

234 265 296 328 364

247 279 312 345 384

267 305 338 373 412

299 333 374 415 461

257 276 29rl 312

280 300 320 340 360

400 429 457 486 514

497 568 643 725 809

513 586 663 745 835

540 617 695 776 866

556 632 716 800 892

580 659 747 839 936

630 705 799 894 994

190 200 220 240 260

271 286 314 343 371

403 438 522 612 71 1

420 457 540 633 732

454 493 586 682 782

514 550 658 760 867

587 628 752 866

385 413 440 468 495

530

765 f&Q

220

257

588 624 661

523 550 605

698

660

881 955

715

133

221

90 100 110 120 130

110

124 138 165 193

118

148 185 222 258

129 147

56.5 73 5 93.4

82.8 92.0

73.8

BB.8 103

110 138 165 193

248 276 331 3B6 441

24.4 27,2

.

#7 717

443 517 591

88.2 110 132 154 176 $98

220 276 331 386 r141 496

551 662 772 882

738

812 686 960

734

808

i

Forthis pipe size: V = 0.0670 x gpm; h, = 6.97 x Figures in shaded area are laminar (viscous) flow. For velocity data see page 3-17.

x gpm2.


Loss in lb per sq In = ,433(sp gr) (figures in table). Figures in shaded area are laminar (viscous) flow. For velocity data see page 3-17. Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local condit~onsand the requirements of each particular installation. It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.



Friction Loss for Viscous Liquids (Continued) (Based on Darcy's Formula)




--

K~nemat~c v~scos~ty-cent~stokes

Flow

US gal per mln

Bbl per hr(42 gal)

8 10 15 20 25

11 4 14 3 21 4 28 6 35 7

30 35 40 50 60

42 9 50.0 57 1 714 857

FRICTION

6

11

21

27

43

74

103

131

157

206

60

70

80

100

Approx SSU vlscoslty

315

33

35

40

50 .42

.59 .73

.?4

.89 1.11 1.67 2.23 2.79

1.18 1.47

22 32 70 1 12 1 69

25 37 76 1 27 1 93

29 43 89 1 47 2 23

32 .47 94 1 57 2 31

.24 54 107 1 78 2 61

79 2 07 3 01

1.10 1.46 3 29

2.33

2 36 3 13 4 03 610 857

2 64 3 48 4 42 6.70 932

2 99 3.97 5 02 750 104

3 22 4 21 5 29 793 110

3 60 4 66 5 90 876 120

4 12 5 41 6 80 101 137

4 50 5 89 7 46 109 15.0

4 83 6 35 7 93 117 160

661 8 37 123 168

4.40 5.13 5.87 132 180

.a

.93 1.40 1.86

3.35

2.20 2.93

3.66

70 80 90 100 120

100 114 129 143 171

115 147 184 224 31.8

124 159 199 242 341

138 175 218 263 369

145 184 228 275 386

159 203 25.0 302 419

180 229 280 337 468

196 246 304 364 505

209 264 324 390 53.4

219 27.7 338 408 564

236 298 363 436 600

140 160 180 200 225

200 228 257 286 322

424 54 8 690 847 107

456 58 0 727 889 112

494 63.3 787 957 120

509 65 4 816 994 124

554 70 4 872 106 132

655 79 1 972 117 145

66.0 83.8 104 125 155

700 87 9 109 131 164

732 92 3 114 137 169

786 98 2 122 146 180

250 275 300 325 350

357 393 429 464 500

131 158 187 218 253

137 164 193 225 260

147 175 204 238 275

151 180 212 247 283

160 191 225 261 300

175 208 244 283 324

188 226 260 300 344

195 233 273 316 361

204 243 281 325 373

218 258 298 345 396

375 400 425 450 475

536 571 607 643 679

288 328 368 410 457

298 339 381 427 473

314 354 397 443 493

322 363 407 455 504

341 385 432 480 532

367 414 463 515 571

388 436 488 543 599

407 458 511 568 625

424 476 529 587 646

448 498 550 619 681

500 525 550 575 600

714 750 786 822 857

504 555 606 663 721

524 574 627 685 742

544 597 651 708 767

555 609 665 723 783

587 644 703 761 820

627 688 748 814 882

658 720 783 852 919

684 748 814 886 960

707 770 838 912 989

750 821 890 962

For this pipe size: V = 0.0434 x gpm; h, = 2.923-' x gpm2 Figures in shaded area are laminar (viscous)flow. For velocity data see page 3-18.


Figures in shaded area are laminar (viscous) flow. For velocity data see page 3-18.


FRICTION

INGERSOLL-RAND CAMERON HYDRAULIC DATA Friction Loss for Viscous Liquids (Continued)





Loss in Feet of Liquid per 1000 Feet of Pipe 3% lnch (3.548 inside dia) Sch 40 New Steel Pipe Flow

US gal per mln

For this pipe size: V = 0.03245 x gpm; h, = 1.634 x Figures in shaded area are laminar (viscous)flow. For velocity data see page 3-19.

gpm2.


Bbl per hr (42 gal)

Kinematic viscosity-centistokes 216.5

.

325

435

Approx SSU viscosity 125

150

Loss in Ib per sq in = ,433 (sp gr) (figures in table). Figures in shaded area are laminar (viscous) flow. For velocity data see page 3-19.

Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each Particular installation. It is recommended that tor most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

INGERSOLL-RAND CAMERON HYDRAULlC DATA Friction Loss for Viscous Liquids (Continued)


Loss in Feet of Liquid per 1000 Feet of Pipe 4 lnch (4.026 inside dia) Sch 40 New Steel Pipe




K~nemat~c v~scoslty-centtr okes

-

- 264

Flow US gal per mln

Bbl per hr (42 gal)

15 20 30 40 50

21 4 28 6 429 57 1 71 4

lo4

gpm2.


432

650

2165

1623

1084

125

150

200

435

650

500

750

1000

1500

2000

3000

3.91 5.21 7.82 10.4 13.0

5.85 7.80 11.7 15.8 79.5

7.80 10.4 15.6 20.8 26.0

11.7 15.6 23.4 31.2 39.0

15.7 20.8 31.3 41.8 52.2

23.4 31.2 46.8

23.4 27.3 31.2 35.1 39.0

31.2

46.8 54.6 82.4

62.7 73.2 83.6

15.6

15.6 18.2 20.8 23,4 2&0

48.8 52.0

70.2 78,O

91.1 705

125 141 15%

93.7

72.8 83.2 93.6 I#

125 146 $67 188 209

187 218 250 281 372

230

343

251 2032 292 313

437 488

300

"95 1.27 1.90 2.54 3.17

1.15 1.54 2.30 3.08 3.84

1.55 2.07 3.11 4.15 5.78

3.80

4.61

4.44

5.38 6.15

9.37 10.9 125 14.1

2.34

3.12 4.08 6.25 7.81

1

85 7 100 114 129 143

881 108 12 9

11.3 13 7

6.22 7.25 8.29 9.33 10.4

120 140 160 180 200

171 200 228 257 286

17 6 22.9 29.0 35.5 426

18 6 24 3 303 37 4 45.0

20.3 26.5 332 40 7 487

18.8 21.9 25.0

31,2 36.4 41.7

45 7 548

4B.g 52.1

48.8 54.6 82.4 70.2 78.a

220 240 260 280 300

314 343 371 400 429

50 3 58 5 67 2 76 4 85 8

53 0 61 5 70.8 80 5 90.8

57 1 65 1 76.8 87.2 98.5

64.7 74.7 85.7 973 110

57-3

85.8

174

93.8

125

67.7 73.0 127

325 350 375 400 450

464 500 536 571 643

98 5 112 127 143 178

104 118 133 149 184

113 128 145 162 198

125 143 161 180 222

146 166 187 208 254

500 550 600 650 700

714 786 857 929 1000

213 252 296 338 386

221 263 305 353 402

237 280 328 378 433

265 313 364 419 474

305 360 417 480 546

---

1070 1140 1215 1285 1360

325

Approx SSU v~scoslty

60 70 80 90 100

750 800 850 900 950 For this pipe size: V = 0.0252 x gpm; h, = 9.858 x Figures in shaded area are lammar (viscous) flow. For velocity data see page 3-20.

32.0

437 490 544 603 666

62.5

488 546 608 674 743

533 570 663 739 813

616 687 763 844 927

$2.4

109

125 740 158

If2 187

35

93.7

lO@

$3

408

136 146 f58

218 254 273 293 372 351

340

508

386 932 478 470

567 585

285

t69 1SZ 195 208 234

343 404 467 528 608

280 286 507 583 663

330

523 575 gZ7 g80 732

745 830 920

585 624

101

l@ 117 127 t35 146 156

a

455 510 570 629 696

36.4 41.6

82.5 78.1

-

-

685 764 848 939

-

234

429 488 507 548

'

826

703 781 860 937

-

683

784 838 889 941

993

Loss in Ib per sq in = 433 (sp gg) (f~gures from table). Flgures In shaded area are lamlnar (VISCOUS) flow For velocity data see page 3-20.


INGERSOLLRAND

FRICTION







1 Flow

Flow

-

US nal

Bbl ner

.6

11

2.1

2.7

4.3

7.4

10.3

Klnematfc v~scos~ty-cent~stokes

-

Kinematic viscosity-centlslokes

13.1

15.7

20.6

A ~ ~ r SSU o x vlscosit~

For this pipe slze: V = 0.01 11 x gpm; h, = 1.914 x lo4 gpm2 Figures in shaded area are lamlnar (v~smus)flow. For velocity data see page 3-22.

Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interlor surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It is recommended that for most commerc~aldesign purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5

US gal per mln

Bbl Per hr (42 gal)

26.4

32.0

43.2

65 0

108 4

162 3

216.5

125

150

2W

300

500

750

1000

151 227 303 379 4%

252 378 5.05 8.31 7.58

3.78 586 7.55 9.45 113

5.04 758 101 12.6 151

530 608 882 757 137

8.84 10.7 11.4 12.8 13.9

13.2 15.1 77.0 18.9 20.8

17.6 20.2 227 252

142 183 23 1 28 6 34 1

159 208 26 2 31 9 28 0

IS,Y f77 20.2 36 9 44 2

22.6 26.4 302 340 37.8

30.2 35.3 *03

369 431 50 0 57 0 644

402 464 53 4 60 8 685

446 517 59 6 68 6 768

521 591 69 4 78 8 88 5

416 153 48 1 88 3 994

68 0 839 101 120 140

72 1 885 106 125 146

76 9 952 115 136 158

85 7 105 126 148 173

14002000 16002285 18002570 2M102860 22003140

184 234 292 350 417

193 244 299 364 435

206 260 322 387 459

2400 3403 26003710 28004000 3000 4285 3200 4570

487 564 645 734 827

507 587 669 751 850

535 620 714 805 909

9 75 100 125 150

714 107 143 178 214

175 200 225 250 275

325

435

650

1500

2000

3000

789 227

101 152 203 25.3 30.4

227 302 378 454

265 303 341 378 477

35.5 405 45.6 567 $5.8

53.0 60.8 681 757 83.2

45.4

60.9


IW

62 .92 1.23 2 75 375

.74 112 149 186 396

1.57 2.01 2.51 301

250 286 322 357 393

4 90 610 743 891 106

5 17 651 793 943 111

5 62 707 866 104 122

300 350 400 450 500

429 500 571 643 714

123 159 20 1 24 7 300

129 171 21 3 26 0 31 3

550 600 650 700 750

786 857 929 1000 1070

356 415 47 7 54 1 608

800 900 1000 1100 1200

1140 1285 1430 1570 1715

277

757 714 15 1

63.0

151

90.8

50.4

806 882 757

91.3 107

108 121 136 151

554 60.5 65 5 M.6 75.6

833 909 9BS $06 114

112 122 132 142 152

166 182 tQ7 272 227

738 151 167 182

?62 163

203

242 27'2 302

223

333

200

60.6 148 177 208 242

j2f

136 163 192 220

243

303

230 288 350 425 510

258 323 399 481 573

287 363 452 535 628

316 393 480 576 683

353 445 543 652 771

284 324 591 707 833

424 484 545 665 868

585 677 773 667 982

668 769 874 993

730 841 954

799 913

885

968

726 787

97 8 120 I44 171

111

55.3

71.0

1

Loss In ib per sq In = 433 jsp gg) (hguros In table) F~guresIn shaded area are lam~nar(v~swuslflow velocity data see page 3-22.

or

Note. NO allowance has been made for age, difference in diameter, or any abnormal c o n d ~ t ~ oofn interior surface. Any factor of safety must be estimated from the local condtlions and the requirements of each particular installation. It is recommended that for most commercial deslgn purposes a safety factor of 15 to 2046 be added to the values in the tables-see page 3-5

INGERSOLLRAND

FRICTION








Kinernat~cvlscos~ly-centlstokes Flow

32 0

26 4

US gai per mln

For thls plpe sue V = 000641 x gpm h For veloclty data see page 3 23

=

6 383

x

10

* gpm

Note No allowance has been made for age difference In diameter, or any abnormal condltlon of Interior surface Any factor of safety must be estlmated from the local condlt~onsand the requ~rementsof each particular lnstallatlon It is recommended that for most commerclal deslgn purposes a safety factor of 15 to 20% be added to the values In the tables-see page 3-5

Bbl per hr (42 gal)

43 2

65 0

108 4

1623

216 5

325

435

650

Approx SSU viscosity 125

1

150

1

XX]

1

300

1

500

1

750

1

1000

1

1500

1

2000

1

3000

LOSS In Ib per sq In = 433 jsp gr) (figures ~n table). Figures in shaded area are lamlnar (VISCOUS) flow. For veloc~tydata see page 3-23. Note. No allowance has been made for age, d~fferenceIn d~ameter.or any abnormal c o n d ~ t ~ oofn interior surface. Any factor of safety must be estimated from the local condit~onsand the requ~rementsof each Rartlcular installation. It IS recommended that for most commercial design purposes a safety factor of 15 to 20% be added l o the values in the tables-see page 3-5

INGERSOLLRAND


I

/ I

FRICTION



(Bared on Darcy's Formula)



Klnematlc v ~ s c o s ~ t y c e n t l s t o k e s

-

Flow

6

US gal per rn~n

/

Bbl per hr (42 aal)

2200 3140 2400 3430 26003710 2800 4000 4285 3000

11

27

21

74

43

103

Klnemallc viscosity-cent~stokes 131

157

206

Approx SSU v~scos~ly

. 1 3 1 5 1

33

1 3 5

1 4 0

1 5 0

1 6 0

1 7 0

1 8 0

(100

21 3 25 2 296 34 1 39 1

22 2 26 3 306 35 3 40 2

23 7 28 0 325 37 4 42 7

24 6 28 9 335 38 4 43 5

26 1 30 7 356 40 8 46 6

28 6 33 4 387 44 5 50 7

303 35 5 410 47 1 53 2

32 1 37 3 429 49 0 55 7

31 8 38 9 448 51 0 57 7

350 41 0 473 54 1 61 3

52 5 68 0 861 106 128

54 4 70 5 886 109 131

57 4 73 9 923 113 136

58 9 75 9 948 116 139

62 3 79 9 992 122 145

66 4 85 8 107 130 156

70 6 90 2 112 136 162

73 6 94 2 117 142 169

76 2 97 1 120 146 173

80 8 102 127 153 182

3500 4000 4500 5000 5500

5000 5715 6430 7145 7855

6000 6500 7000 7500 8000

8570 9280 10000 10700 11400

152 177 205 236 266

154 180 208 239 272

161 187 217 248 282

164 191 220 251 286

172 201 231 262 296

183 212 243 277 314

191 221 255 291 329

197 228 263 298 337

204 236 369 303 345

213 246 282 321 360

850012100 9000 12900 10000 14300 11000 15700 1200017150

301 337 416 503 599

307 341 422 511 603

318 354 434 522 617

321 359 441 533 630

334 372 453 544 643

352 392 478 574 679

367 407 492 593 701

378 422 511 611 719

387 429 524 626 737

403 447 542 649 763

For t h ~ splpe size V = 0 00407 x gpm h, For veloclty data see page 3 24

=

2 569 x 10

x gpm'

Note No allowance has been made for age dlfference ~n d~ameter,or any abnorrral condlllon of lnterlor surface Any factor of safety must be estlmated from the local condltlons and the requlrements of each particular ~nstallattonIt 15 recommended that for most cornmerc~aldeslgn purposes a safety factor Of 15 to 20% be added to the values rn the tables-see page 3 5

US gal per mln

Bbl per hr (42 gal)

7000 10OOO 750010700 8000 11400 9000 12900 1000014300

216.5

325

435

650

Approx SSU viscos~ty 125

296 335 377 469 567

1

150

305 347 389 482 582

I

200

326 369 414 512 619

I

300

355 402 452 557 666

1

500

396 447 505 624 743

I

750

436 492 550 679 817

1

IOW

468 529 594 729 872

I

1500

522 589 659 809 964

I

2000

566

638 710 869

1

3000

637 766 797 976

Loss in Ib per sq in = ,433 (sp gr) (ligures i n table). Figures in shaded area are laminar (viscous) flow. For veloc~tydata $88 page 924.

Note No allowance has been made for age, dlfference In d~ameter,or any abnormal condltlon of Interlor surface Any factor of safety must be estlmated from the local Condlt~onsand the requlrements of each Pafllcular lnstallat~on I t IS recommended that for most commercial desrgn purposes a safety factor of 15 to 20% be added to the values In the tables-see page 3-5

INGERSOLLRAND

FRICTION








-26.4

K ~ n e m a t ~vlscos~ty-cent~stokes c

Flow

Klnematic vlscoslty-cent~stokes Flow

US gal per rnln

I

0.6 Bbl per hr (42 gal)

1 13

27

2.1

4.3

7.4

10.3

13.1

15.7

20 6

60

70

80

100


31.5

40

35

33

50

I

3500 4000 4500 5000 5500

5000 5715 6430 7145 7855

21 8 283 35 7 44 0 53 1

22 6 292 368 45 2 54 4

23 8 307 38 5 47 I 566

24 4 315 39 4 48 2 578

26 0 333 41 6 50 7 60 7

28 3 362 45 0 54 7 65 3

30 1 384 47 7 57 8 68 9

31 6 403 49 9 60 4 71 9

32 9 418 51 7 62 6 74 4

34 9 443 54 8 66 2 78 7

6000 6500 7000 7500 8000

8570 9280 10000 10700 11400

63 0 738 854 979 111

64 5 754 872 998 113

66 9 781 901 103 117

68 3 796 918 105 119

71 6 833 959 109 124

76 8 892 102 117 132

80 9 938 108 122 138

84 3 977 112 127 143

87 2 101 116 131 148

92 1 106 122 138 155

9000 10000 11000 12000 13000

12850 14300 15700 17150 18550

141 173 209 249 291

143 176 212 252 295

147 180 217 258 301

149 183 220 261 305

155 190 228 269 314

164 200 240 283 330

172 209 250 294 342

178 217 269 304 353

183 223 266 312 363

192 233 278 326 373

14000 20000 15000 21400 1600022850 1800025700 20000 28600

338 387 440 557 687

342 392 445 561 692

348 399 453 571 703

353 403 457 577 709

363 414 469 590 725

380 433 490 614 752

394 449 507 634 775

406 462 522 651 795

416 473 534 666 812

434 493 556 692 842

For thls plpe slze v - 0 00287 x gpm h, For velocity data see page 3-25

=

1 275 x 10

x gpmL

Note No allowance has been made for age, dtfference in d~ameter,or any abnormal cond~tjonof Interlor surface Any factor of safety must be estimated from the local condlt~onsand the requ~rementsof each particular lnstallat~on It IS recommended that for most commercial des~gnpurposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5

US gal per mln

Bbl per hr (42 gal)

32 0

43.2

65.0

108.4

162 3

216 5

325

435

650

1000

1500

2000

3000


125

150

200

100 200 300 400 500

143 286 429 571 714

.08 "16 49 81 1 22

.10 .?9 53 86 1 25

.4? 94 137

600 700 800 900 1000

857 1000 1140 1285 1430

166 215 270 3.31 3.97

171 230 2.88 3.52 422

1200 1400 1600 1800 2000

1715 2000 2285 2570 2860

543 710 8 96 110 132

2500 3000 3500 4000 4500

3570 4285 5000 5715 6430

5000 5500 6000 6500 7000 7500 8000 9000 10000 11000

300

.13

.20 .40

500

750

.34

.51

1.02

.67 1.01 1.34 1.71

1.51 2.02 2.50

1.87 2.43 3.05 3.74 448

212 275 3.45 4.21 5.04

1.97 2.37 2.63 4.93 589

577 753 9 48 116 140

633 824 10 4 127 15.2

688 896 11.3 13.8 166

196 27 2 36 2 434 576

206 28 4 37 3 473 583

224 30 8 40 3 510 628

7145 7855 8570 9280 10000

69 8 828 968 112 128

70 3 836 982 114 131

10700 11400 12850 14300 15700

145 163 202 204 290

12000 17150 13000 18550 1400020000 15000 21400 16000 22850

341 394 452 513 578

27

62

.82

1.00

3.02 3.61 4.04 4.44

5.13

.68 1.37 2.00

1.00

2.05

2.88 3.37

3.06 3.98 5.01

4.05 4.88

6.03 7.05

5.36

8.99

6.05 6.84

7.89

1.35 2.74 4.11

5.46 6.84 7.99 9.36 70.7 12.1

2.00 4.01 6.16 8.21 10.3

10.0

13.5

12.3 13.9 15.9 18.0 20.0

12.1 14.6

16.2

16.2 18.9 21.7

24.f 28.2 32.4

17.7 20.5

24.2

36.5

27.4

40.1

34.2

51.3 61.6 71.9 82.1 92.4

9.30

801 104 13.1 16.0 191

5.91 118 14.8 18.0 215

$3.47 10.5 19.7 236

253 34 6 45 2 570 69.9

280 38 4 50 2 632 776

315 43 0 56 0 705 864

343 46 8 60 9 765 936

75.6 895 104 120 137

84 1 994 116 133 152

93.3 110 128 148 174

104 122 142 164 186

112 132 154 176 201

126 148 172 197 224

138 162 '188 215 244

103 183 212 243 275

148 167 208 253 301

155 174 215 260 309

172 192 237 286 338

196 220 270 325 384

210 235 289 347 41 1

226 253 311 373 441

253 282 346 415 490

274 306 375 450 530

310 345 422 505 594

354 409 469 532 598

361 417 477 541 608

395 456 521 589 662

448 516 588 664 745

479 551 628 710 796

514 591 673 760 851

569 655 745 840 940

616 707 804 906

689 790 898

257 53 1 68 8 863 105

41.1 47.9 945 115

F~guresin shaded area are laminar (VISCOUS) flow For velocity data see page 3-25.

Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safi?ty must be estimated from the local condlttons and the requirements of each particular installation. It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.


INGERSOLLRAND



(Bared on Darcy's Formula)


Loss in Feet of Liquid per 1000 Feet of Pipe 14 Inch (13.124" inside dia) Sch 40 New Steel Pipe

Loss in Feet of Liquid per 1000 feet of Pipe 14 Inch (13.124 inside dia) Sch 40 New Steel Pipe

Kinematic v~scoslty-cent~stokes

K~nematjcv~scos~ly-cent~stokes Flow US

gal per

Bbl per hr (42

27

43

74

Flow

103

131

157

206

Approx SSU vlscos~ty

. 1315

1

33

1

35

1

40

1

50

1

60

1

70

1

80

(

100

For thls plpe slze v - 0 00237 x gpm h = 8 73 x 10 * n gpm' For veloclty data see page 3-26 Note No allowance has been made for age d~fferenceIn dlameter or any abnormal c o n d ~ t ~ oofn lnterlor surface Any factor of safety must be estlrnated from the local condltlons and the requlrements of each particular bnstallatlon It IS recommended that for most commerc!al deslgn purposes a safety factor Of 15 to 20% be added to the values In the tables-see page 3 5

US gal per min

Bbl per hr (42 gal)

. Approx SSU v~scosity 125

1

150

1

200

1

300

1

500

1

750

1

1000

1

1500

1

2000

1

3000

F~guresin shaded area are laminar (viscous) flow For veloc~tydata see page 3-26.

Note: No allowance has been made for age, difference in dlarneter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local c o n d ~ t ~ o nand s the requlrements of each Particular installation. It is recommended that for most cornrnerclal design purposes a safety factor of 15 to 20% be added to the values In the tables-see page 3-5

INGERSOLLRAND

FRICTION




(Baaed on Darcy's Formula)




K~nemat~c v~scos~ty-centlstokes Flow

Klnematlc v~scos~ly-cenl~slokes

264

Flow US

Bbl per

gal per

hr

Approx SSU viscos~ty

(42

gal)

mln

US gal per man

1315

1

33

1

35

1

40

1

50

1

60

1

70

1

80

1

Bbl per hr (42 gall

I

I

I

I

I

I

5 116 A 10

I

I

I

I

432

650

200

300

1084

1623

2165

325

435

650


125

1

150

1

500

750

1000

100

20000 28600 22000 31400 2409034300 2600037100 2800040000

For thls plpe slze v - 0 00182 K gpm h. For veloclty data see page 3-26

320

I

' igpm-

Note No allowance has been made for age, difference In dlameler, or any abnormal condltlon of Interlor surface Any factor of safely must be estimated from the local condltlons and the requlremenls of each particular Installallon I1 IS recommended that for most commercial deslgn purposes a safety factor of 15 to 20% be added l o the values In the tables-see page 3-5

285 340 399 462 530

296 352 413 478 548

301 358 420 487 559

329 390 456 527 602

371 439 512 591 674

396 486 566 652 743

424 502 565 674 768

469 554 645

742 846

506 597 694 798 909

564 664 772 886

Figures In shaded area are iam~nar(VISCOUS) flow. For velocity data see page 3-26.

Note: No allowance has been made for age, d~fferencein diameter, or any abnormal cond~tionof interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each palticular installation. it is recommended that for most commercial design purposes a safety factor of 15 to 20% be added t o the values in the tables-see page 3-5.

INGERSOLLRAND


FRICTION Friction Loss for Viscous Liquids (Continued)


(Based on Darcy'r Formula)



Loss in Feet of Liquid per 1000 Feet of Pipe 18 lnch (16.876" inside dia) Sch 40 New Steel Pipe K~nemat~c v~scos~ty-cent~stokes Flow 06 US

Bbl

ctal

npr

mln

hFi42 gai)

GLr

113

21

27

43

74

103

131

157

206

Aonrox SSU v~scosltv 31 5

33

35

For thls plpe slze v = 0 001434 x gprn. h, = 3 193 x 10 ' x gpmFor veloclty data see page 3-27 Note No allowance has been made for age, dlfference In dlameter or any abnormal COndltlOn o f Interlor surface Any lactor of safely must be esttmaled from the local c o n d ~ l ~ o nand s the requ~rementsof each particular lnstallat~on It IS recommended that for most commercial des~gnpurposes a Safety factor Of 15 to 20% be added to the values In the tables-see page 3-5

Figures in shaded area are laminar (v~saous)flow. For velocity data see page 3-27. Note: NO allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation It is recommended that for most commercial design purposes a Safety factor of 15 to 20% be added t o the values In the tables-see page 3-5.

INGERSOLLUAND

CAMERON HYDRAULIC DATA Friction Loss for Viscous Liquids (Continued)




Loss in Feet of Liquid per 1000 Feet of Pipe 20 lnch (18.812" inside dia) Sch 40 New Steel Pipe K~nemat~c v~scos~ty-cent~slokes Flow 264 US gal

32 0

43 2

I

For lhls plpe slze v - 0 001 154 x gpm h For veloclly data see page 3-27

2 068 r 10 ' # gpm'

Note No allowance has been made for age, dlfference In dlameter or any abnormal c o n d ~ t ~ oof n tnterlor Surface Any factor of safety must be est~matedfrom the local condlllons and the requlrements of each panlcular lnstallallon It IS recommended that for most commerc~aldeslgn purposes a safety factor of 15 to 20% be added to the values In the tables-see page 3-5

650

108 4

162 3

216 5

325

435

650

Bbl ~ e r

I

I

I

I

1

I

I

Figures In shaded area are iam~nar(VISCOUS) flow For velocity data see page 3-27. Note: No allowance has been made for age. difference In d~ameter,or any abnormal c o n d ~ t ~ oof n Interlor surface. Any factor of safety must be est~rnatedfrom the local condtt~onsand the requlrements of each paniCUlar Installation It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values In the tables-see page 3-5.

INGERSOLL-RAND

FRICTION








K ~ n e m a t ~viscos~ty-cent~stokes c Flow US gal per mln

-

tic viscosity-centistokes 0.6

2.1

1.13

2.7

4.3

7.4

10.3

13.1

15 7

20.6

Flow 108.4

Bbl per hr (42 gal)

162.3

216.5

325

435

650

Approx SSU viscos~ty ,pprox SSU v~scosity 33

35

40

50

60

70

80

2000 3000 4000 5000 6000

2860 4285 5715 7145 8670

.31 .63 1.10 1.70 2.41

.34 .71 1.18 1.79 2.54

.37 -78 1.28 1.94 2.73

.39 .82 1.34 2.02 2.83

.41 .86 1.45 2.18 3.05

.47 .97 1.62 2.43 3.38

.51 1.05 1.75 2.61 3.62

.55 1.11 1.85 2.76 3.82

.57 117 1.94 2.88 3.98

7000 8000 9000 10000 12000

10000 11400 12850 14300 17150

3.24 4.21 5.29 6.50 9.29

3.41 4.40 5.52 6.76 9.62

3.65 4.69 5.86 7.16 10.1

3.77 4.85 6.04 7.37 10.4

4.06 5.19 6.46 7.85 11.0

4.47 5.71 7.08 8.59 12.0

4.78 6.09 7.54 9 13 12.7

5.03 6.40 7.92 9.58 13.3

14000 16000 18000 20000 22000

20000 22850 25700 28600 31400

12.6 16.3 20.6 25.4 30.6

13.0 16.8 21.2 26.0 31.3

13.6 17.6 22.0 27.0 32.5

13.9 18.0 22.5 27.6 33.1

14.7 18.9 23.7 28.9 34.6

16.0 20.4 25.5 31.0 37.0

26.9 21.6 26.8 32.6 38.9

17.7 22.5 28.0 33.9 40.4

24000 26000 28000 30000 32000

34300 37100 40000 42850 45700

36.4 42.6 49.3 56.6 64.3

37.1 43.5 50.3 57.6 65.4

38.4 44.9 51.8 59.2 67.2

39.1 45.7 52.7 60.2 68.2

40.8 47.6 54.8 62.5 70.7

43.6 50.6 58.2 66.3 74.9

45.7 53.0 60.9 69.2 78.1

47.5 55.0 63.1 71.8 80.9

34000 36000 38000 40000 42000

48600 51400 54300 57150 60000

72.5 81.2 90.4 100 110

73.6 82.4 91.7 101 112

75.6 84.5 93.9 104 114

76.7 85.7 95.2 105 116

79.5 88.7 98.4 109 119

84.0 93.6 104 114 125

87.5 97.4 108 119 130

90.6 101 11 1 123 134

44000 46000 48000 50000 55000

62900 65700 68600 71450 78600

121 132 144 156 188

122 134 145 158 190

125 137 148 161 194

127 138 150 163 196

131 142 154 167 201

137 149 162 175 210

142 155 168 181 217

147 159 173 186 223

60000 65000 70000 80000 90000

85710 92860 100000 114290 128570

224 263 304 397 502

226 265 307 400 506

230 269 312 406 512

232 272 314 409 515

238 278 321 417 525

248 289 333 431 541

256 298 343 443 555

263 306 352 454 568

31.5

100 500

For this pipe size: v = 7.98 x 10 For velocity data see page 3-28.

'x

.59 1.21 2.07 3.07 4.25

gpm, h, = 9.886 x 10.' x gpmY.

Note: No allowance has been made for age, difference in diameter, or any abnormal condit~onof interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

1

750

1

1000

1

1500

1

2000

1

3000

ki' Figures in shaded area are laminar (viscous) flow. For velocity data see page 3-28.


FRICTION


INGERSOLLRAND







K~nemat~c viscosity-centistokes

Klnemat~cv~scos~ty-cent~stokes

Flow

US gal per mln

Bbl

- 26 4

Flow 0.6

1.13

2.1

7.4

4.3

2.7

10.3

13.1

15.7

20.6

US gal per mln


per hr (42 gal)

31.5

33

50

40

35

60

70

80

100

Bbl per hr (42 gal)

32.0

43.2

108.4

65 0

162.3

216.5

325

435

650

1500

2000

3000

Approx SSU v~scosity 125

150

200

300

500

750

1000

1.28 1.36

1.79 202

1,44

2.15

1.53 1,62

2-29

f.4S 1.a

243

3.60 4.50 5.49

3iBS 4.14

3.24~ 6 02

,W

3200 3400 3600 3800 4000

4570 4860 5140 5425 5715

.23 .25 .28 .31 .33

.25 28 .31 .34 .37

.27 -31 -34 -38 .41

.29 .32 .36 .39 .43

.30 .34 .38 .42 .56

.34 -38 -43 -47 .51

.37 .42 .46 .51 .55

40 .44 49 .54 .59

.42 .46 .51 .56 .62

.43 .48 53 .59 .64

3200 3400 3600 3800 4000

4570 4860 5140 5425 5715

46 51 57 62 68

.49 .54 .60 .66 72

.54 60 66 .72 .79

.58 65 .72 79 86

.68 .75 .83 .91 .99

.77 86 94 1.03 1.12

5000 6000 7000 8000 9000

7145 8570 10000 11400 12850

.51 -72 .97 1.25 1.57

.57 .77 1.03 1.33 1.66

.62 .86 1.12 1.43 1.79

.65 .88 1.16 1.49 1.85

.68 .95 1.26 1.61 2.00

.77 1.06 1.40 1.79 2.21

.83 1.14 1.51 1.91 2.37

.87 1.21 1.59 2.02 2.49

.91 1.26 1.66 2.11 2.60

.97 1.35 1.77 2.25 2.77

5000 6000 7000 8000 9000

7145 8570 10000 11400 12850

1.00 1.38 181 2.32 2 89

106 1 46 191 2.42 2.97

116 1.59 2.08 2.62 3.22

1.26 1.73 2.34 2.94 3 61

146 1 99 2.60 327 4.01

164 2 24 2.91 3.66 4.48

179 2.44 3.17 3.98 4.86

10000 12000 14000 16000 18000

14300 17150 20000 22850 25700

1.92 2.74 3.70 4.80 6.05

2.03 2.87 3.86 5.00 6.27

2.18 3.07 4.11 5.29 6.62

2.25 3.17 4.23 5.44 6.80

2.43 3.40 4.52 5.80 7.22

2.68 3.73 4.95 6.33 7.86

2.86 3.98 5.27 6.72 8.33

3.01 4.19 5.53 7.04 8.72

3.14 4.35 5.74 7.31 9.05

3.34 4.63 6.10 7.75 9.57

10000 12000 14000 16000 18000

14300 17150 20000 22850 25700

351 4.89 6 44 8.17 10.1

3.58 4.94 6.54 8.37 10.4

3.87 533 6.99 8 85 10.9

4.33 5.95 7 79 9.84 12.1

4.81 6.61 8.65 10.9 13.4

537 7.35 9.60 12 1 14.9

582 796 10.4 13 1 160

6.57 8.95 11.7 14.6 179

7.19 9.78 12.7 15.9 19.5

14.4 18.0 22.0

20000 22000 24000 26000 28000

28600 31400 34300 37100 40000

7.44 8.97 10.6 12.5 14.4

7.69 9.26 11.0 12.8 14.8

8.09 9.71 11.5 13.4 15.4

8.31 9.95 11.8 13.7 15.8

8.80 10.5 12.4 14.4 16.6

9.55 11.4 13.4 15.5 17.8

10.1 12.0 14.1 16.4 18.8

10.6 12.6 14.8 17.1 19.6

11.0 13.0 15.3 177 20.2

11.6 13.8 16.1 18.6 21.3

20000 22000 24000 26000 28000

28600 31400 34300 37100 40000

12.2 14 5 16.9 19.6 22.4

12.7 15.1 177 20.4 233

13.2 15.6 18.2 21.0 24.0

146 17 2 20.1 23.1 26.4

167 19.7 230 26.4 30.1

179 21 1 24.6 283 322

19.2 22.7 26.4 304 346

21.5 25.3 29.4 33.8 38.4

233 27.5 31.9 36.6 41.6

263 30.9 35.8 41.1 46.6

30000 35000 40000 45000 50000

42850 50000 57150 62290 71450

16.5 22.4 29.1 36.8 45.3

16.9 22.9 29.7 37.5 46.1

17.6 23.7 30.7 38.6 47.4

18.0 24.2 31.3 39.3 48.2

18.9 25.3 32.6 40.8 50.0

20.3 27.0 34.7 43.3 52.9

21.3 28.4 36.4 45.3 55.2

22.2 29.5 37.8 47.0 57.1

22.9 30.4 38.9 48.3 58.8

241 32.0 40.8 50.7 61.5

30000 35000 40000 45000 50000

42850 50000 57150 62290 71450

253 33 5 42 7 52.9 642

26.4 34 9 44 4 55 0 666

27.1 35.7 45.6 56.7 68.9

29.8 39 2 49.8 61.5 74.2

34.0 44.5 56 4 69 4 837

364 47.7 60 4 77 0 92.6

390 51 1 64.6 79.5 95.8

43.3 56 6 71.5 87.8 106

46.9 61 2 77.1 94.6 114

52.5 68.3 86 0 105 126

78570 55000 85710 60000 65000 92860 70000 100000 75000107140

54.8 65.1 76.3 88.4 101

55.6 66.0 77.3 89.5 103

57.1 67.7 79.1 91.5 105

57.9 68.6 80.2 92.6 106

60.0 70.9 82.7 95.4 109

63.3 74.7 87.0 100 114

66.0 77.7 90.3 104 118

68.2 80.3 93.2 107 122

70.1 82.4 95.7 110 125

73.3 86.0 99.8 114 130

55000 78570 764 85710 60000 89 6 92860104 65000 70000 100000 119 7 5 0 0 0 1 0 7 1 4 0 135

79.3 92.9 108 123 140

82.2 96.5 112 128 146

88.1 103 119 136 154

991 116 133 152 172

110 128 147 168 190

113 132 152 174 196

125 145 167 191 216

134 156 180 205 231

149 173 199 227 256

115 130 146 162 180

117 131 147 164 181

119 134 150 167 184

120 135 151 168 186

124 139 155 172 190

129 145 162 180 198

134 150 167 185 204

138 154 172 190 210

141 158 176 195 214

147 164 183 202 222

158 176 196 216 238

164 184 204 226 248

173 193 214 236 259

193 216 239 263 289

213 237 262 289 316

220 245 281 309 339

242 269 297 327 359

259 288 319 350 384

286 318 351 386 423

80000114290 85000121430 90000 128570 95000135710 100000142860

For t h ~ spipe size: v = 4.942 x 10 For velocity data see page 3-28.

' x gpm; h, = 3.791 x

10

'I

x

80000 85000 90000 95000 100000

152 170 189 209 230

.@ .73

.n .81

.$8 t.10 t.13 t.18

2.T6

2.39

4.34

5.98

5.M

7.30


gpmL

Note: No allowance has been made for age, d~fferencein diameter, or any abnormal condition of interlor surface. Any factor of safety must be estimated from the local cond~tionsand the requ~rementsof each particular installation. It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

114290 121430 128570 135710 142860

.fE5

I

Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular ~nstallation.It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

FRICTION


INGERSOLLRAND






Kinematic viscosity-centistokes Flow

0.6 US gal per mln

Bbl per hr (42 gal)

1.13

2.1

2.7

31.5

33

35

4.3

7.4

10.3

- 26.4

15.7

20.6


40

50 .44

US gal per mln

Bbl per hr (42 gal)

60

70

80

.51 .66 .84 1.04 1.25

.53 -69 -88 1.08 1.31

.56 .74 .94 1 .16 1.40

6000 7000 8000 9000 10000

8670 10000 11400 12850 14300

100

325

435

650

1500

2000

3000


125

500

750

1000

.76 .96 1 19 1.44

1.m 1 92 2.34 2 79

17150 20000 22850 25700 28600

2.02 2.69 3.41 4.21 5.08

2.07 2.72 3.45 4.29 5.21

224 2.93 3.71 4 57 5.50

2.51 3.28 4.13 5.08 6.11

2.78 3.64 4.59 5.64 6.78

3.10 4.05 5.10 6.26 7.52

3.37 4.39 552 6 76 8.12

3.80 4.94 6.20 7.58 9.08

22000 24000 26000 28000 30000

31400 34300 37100 40000 42850

6.02 7.04 8.12 9.28 10.5

6.21 7.30 8.46 9.70 11.0

6.51 7.60 8.76 9.99 113

7.22 8.42 9.69 11.1 12.5

8.02 9.66 11.1 12.6 14.3

8.88 10.3 11.9 13.5 15.3

13.2 16.8 20.9 25.3 30.1

35000 40000 45000 50000 55000

50000 57150 62290 71450 78570

13.9 17.7 21.9 26.5 31.5

14.5 18.4 22.8 27.6 32.8

14.9 18.9 23.4 28.4 33.9

16.4 20.8 25.6 30.9 36.7

18.7 23.6 29.1 35.0 41.4

33.7 39.1 44.9 57.5 71.5

35.3 40.9 46.9 60.0 74.6

60000 85710 65000 92860 70000 100000 80000 114290 90000 128570

36.9 42.7 48.9 62.5 77.6

38.4 44.4 50.8 64.8 80.4

39.8 46.1 52.9 67.7 84.2

42.9 49.5 56.5 71.8 88.8

48.3 55.7 63.6 80.6 99.5

85.0 102 120 139 160

87.1 104 123 142 164

90.7 108 127 148 170

100000 142860 94.3 110000157140 112 120000171430 132 130000 185710 153 140000 200000 176

97.6 116 136 158 181

102 122 143 166 191

107 128 150 173 198

183 206 232 258 316

186 211 236 263 322

193 218 244 272 332

150000214290 160000 228570 170000 242860 180000 257140 200000285710

206 232 260 289 352

217 244 273 303 369

224 252 282 313 380

.39 .52 .66 .82 1.00

.74 .92 1.11

.48 .63 .80 .98 1.19

12000 14000 16000 18000 20000

17150 20000 22850 25700 28600

1.09 1.47 1.90 2.39 2.94

1.15 1.55 2.00 2.50 3.07

1.25 1.66 2.14 2.67 3.26

1.29 1.72 2.21 2.75 3.36

1.39 1.85 2.37 2.95 3.58

1.54 2.04 2.61 3.23 3.92

1.65 2.18 2.78 3.44 4.17

1.74 2.29 2.92 3.61 4.37

1.81 2.39 3.03 3.75 4.54

1.93 2.54 3.22 3.98 4.81

12000 14000 16000 18000 20000

22000 24000 26000 28000 30000

31400 34300 37100 40000 42850

3.54 4.20 4.91 5.67 6.50

3.68 4.36 5.09 5.87 6.71

3.90 4.60 5.36 6.18 7.05

4.02 4.74 5.51 6.34 7.23

4.28 5.03 5.85 6.72 7.65

4.67 5.48 6.35 7.29 8.28

4.96 5.81 6.73 7.71 8.75

5.20 6.09 7.04 8.06 9.14

5.39 6.31 7.30 8.35 9.46

5.71 6.68 7.71 8.82 9.99

35000 40000 45000 50000 55000

50000 57150 62290 71450 78570

8.80 11.4 14.4 17.8 21.5

9.06 11.8 14.8 18.2 21.9

9.47 12.2 15.4 18.8 22.7

9.70 12.5 15.7 19.2 23.1

10.2 13.2 16.4 20.1 24.1

11.0 14.1 17.6 21.4 25.6

11.6 14.9 18.5 22.5 26.9

12.1 15.5 19.2 23.4 27.9

12.5 16.0 19.9 24.1 28.7

25.5 29.9 34.6 45.0 56.9

26.0 30.4 35.2 45.8 57.7

26.8 31.3 36.2 46.9 59.1

27.3 31.8 36.8 47.6 59.9

28.4 33.1 38.1 49.3 61.8

30.2 35.1 40.4 52.0 65.0

31.6 36.7 42.1 54.1 67.6

32.8 38.0 43.6 55.9 69.7

100000 142860 70.1 110000 157140 84.8 120000171430 101 130000185710 118 140000200000 137

71.1 85.8 102 119 138

72.6 87.5 104 122 141

73.5 88.6 105 123 142

75.7 91.1 108 126 145

79.5 95.3 113 131 151

82.4 98.7 116 136 156

158 180 203 228 280

161 183 206 231 284

163 184 208 233 286

166 189 212 237 291

173 196 220 245 301

178 201 226 252 309

1 828 x

300

216.5

1.04 1.35 1.69 2.06 2 47

.37 .50 .62 .76 .92

=

200

162.3

.95 1.23 1.55 1 .89 2.27

.36 .47 .60 .73 .89

For this pipe slze. v = 3 432 x lo-' x gpm, h, For veloclty data see page 3-29

150

108 4

.84 1.10 1.38 1 69 2.03

.33 .43 .54 .67 .82

157 179 201 226 278

65.0

.73 .95 1.24 1.52 1.83

.29 .39 .50 .63 .77

150000214290 160000 228570 170000 242860 180000257140 200000285710

43 2

.67 .88 1 10 1 35 1.63

8670 10000 1 1400 1 2850 14300

60000 85710 65000 92860 70000 100000 80000 114290 90000 128570

32.0

.61 .80 1.01 1.25 1.50

6000 7000 8000 9000 10000

.58

Kinematic v~scos~ty-cent~stokes

Flow

13.1

x gpm2

Note No allowance has been made for age, difference In diameter, or any abnormal condltlon of Interlor surface Any factor of safety must be estimated from the local condltlons and the requ~rementsof each particular lnstallat~onIt IS recommended that for most commercial deslgn purposes a safety factor of 15 to 20% be added to the values In the tables-see page 3-5.

I

1

.58

200 225 252 281 342

9 57

,%@

4.161 3.45 5 . 4 0 4.m 6.77 7.68 9.36 8.26 11.2 9.89

12.8 14.6 16.4

10.7 12.4 14.3 162 18.3

11.6 13.5 15 5 17.6 19.8

13.1 15.2 17.4 19.8 22.2

20.0 25.3 31.1 37.5 46.0

21.5 271 33.4 40.2 47.5

23.9 30.1 36.9 44.4 52.5

25.8 32.5 39.9 47.9 56.5

28.9 36.4 44.5 53.4 62.9

53.5 61.6 70.2 88.9 110

55.3 63.8 72.7 92.1 113

61.1 70.3 80.1 101 125

65.8 75.6 86.1 109 134

73.1 84.0 95.5 120 148

120 142 167 192 220

132 156 183 211 240

137 168 196 226 257

150 178 207 239 272

161 190 222 255 291

178 210 244 281 320

249 280 312 346 419

272 305 340 377 456

291 326 364 403 486

308 345 385 426 514

329 369 411

362 405 451 499 600

111

454

548

Figures In shaded area are lamlnar (VISCOUS) flow. For veloclty data see page 3-29. Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

FRICTION


INGERSOLLRAND





Loss in Feet of Liquid per 1000 Feet of Pipe 42 lnch (42.0" inside dia) New Steel Pipe


K~nematicviscosity-centistokes

- 06

Flow US gal per mln

Bbl per hr (42 gal)

-

1.13

4.3

2.7

2.1

7.4


10.3

13.1

157

Approx SSU viscos~ty

31.5

35

33

40

50

60

70

80

Flow

- 26.4

206

100

US gal per mln

Bbl per hr (42 gal)

162.3

216.5

325

435

650

125

150

200

300

500

750

1000

1500

2000

3000

.38 .46 .54 .62 .71

.43 .51 .60 .69 .79

.46 .55 .64 .74 .85

49 .58 .68 .78 .89

.51 -60 .71 .81 .93

,551 .65 75 .87 .99

10000 11000 12000 13000 14000

14300 15700 17150 18600 20000

-56 .66 .78 .90 1.03

.59 .70 .81 .93 1.06

.64 .76 .88 1.01 1.15

.72 .85 .99 1.13 1.29

1.10 1.26 1.43

.90 1.06 1.23 1.41 1.60

.98 1.15 1.33 1.53 1.74

1.11 1.30 1.51 1.73 1.96

1.66 1.90 2.15

.75 .84

.89 1.00 1.12 124 1.37

.96 1.07 1.20 1.33 1.47

1.01 113 1.26 1.40 1.54

1.05 1.18 1.31 1.46 1.60

1.12 1.26 1.40 1.55 1.71

15000 16000 17000 18000 19000

21400 22850 24290 25700 27140

1.17 1.32 1.48 1.64 1.81

1.20 1.34 1.50 1.66 1.82

1.30 1.45 1.62 1.79 1.97

1.45 1.63 1.81 2.00 2.19

1.61 1.81 2.01 2.22 2.44

1.80 2.01 2.23 2.47 2.71

1.95 2.18 2.42 2.67 2.93

2.20 2.46 2.72 3.00 3.29

2.41 2.69 2.98 3.28 3.59

2.02

20000 25000 30000 35000 40000

28600 35700 42850 50000 57150

1.98 2.94 4.08 5.38 6.84

2.00 3.02 4.24 5.63 7.15

2.15 3.19 4.41 5.80 7.35

2.40 3.54 4.88 6.41 8.12

2.66 3.94 5.60 7.33 9.26

2.96 4.36 5.99 7.85 9.91

3.20 4.71 6.46 8.44 10.7

3.59 5.27 7.21 9.40 11.9

3.92 5.73 7.83 10.2 12.8

4.45 6.47 8.82 11.5 14.4

45000 62290 50000 71450 60000 85710 70000100000 80000114290

8.46 10.2 14.2 18.8 24.0

8.83 10.7 14.8 19.6 25.0

9.08 11.0 15.3 20.3 26.0

10.0 12.1 16.7 22.0 27.9

11.4 13.7 18.9 24.8 31.4

12.2 14.7 20.2 27.5 34.8

13.1 15.7 21.7 28.4 36.0

14.5 17.5 24.0 31.4 39.7

15.7 18.9 25.9 33.8 42.7

17.6 21.1 28.8 37.6 47.4

128570 142860 157140 171430 185710

29.8 36.1 43.1 50.5 58.5

31.0 37.5 44.7 52.4 60.6

32.3 39.3 46.9 55.0 63.8

34.5 41.6 49.4 57.8 66.8

38.8 46.8 55.4 64.7 74.7

42.8 51.6 61.1 71.2 82.1

44.3 53.4 63.3 73.8 85.1

48.8 58.7 69.5 81.0 93.3

52.4 63.1 74.5 86.8 100

58.2 69.9 82.5 96.0 110

67.1 76.2 85.9 96.1 107

69.5 78.9 88.8 99.3 110

73.2 83.2 93.7 105 116

76.4 86.6 97.3 109 121

85.3 96.5 108 121 134

93.7 106 119 132 147

101 114 127 142 157

106 120 135 150 166

114 129 144 160 178

126 142 159 177 195

122 134 203 285 380

128 141 213 298 397

133 146 220 307 407

148 162 242 337 447

161 177 264 367 484

173 189 282 390 515

183 200 298 413 565

195 214 318 440 579

215 235 348 481 632

.29 .34 .41 .47 .54

15000 16000 17000 18000 19000

21400 22850 24290 25700 27140

62 .70 .79 -88 -98

.66 .75 .84 .94 1.04

.72 .81 .91 1.01 1.12

1.05 1

.81 .91 1.01 1.13 1.24

20000 25000 30000 35000 40000

28600 35700 42850 50000 57150

1.08 1.67 2.39 3.22 4.19

1.14 1.75 2.49 3.35 4.34

1.23 1.87 2.64 3.54 4.56

1.27 1.93 2.72 3.64 4.69

1.37 2.07 2.90 3.87 4.96

1.51 2.27 3.17 4.21 5.38

1.61 2 41 3.36 4.46 5.70

1.69 2.53 3.52 4.66 5.95

1.76 2.63 3.66 4.83 6.16

1.87 2.79 3.87 5.11 6.51

45000 62290 50000 71450 60000 85710 70000100000 80000 114290

5.28 6.49 9.29 12.6 16.4

5.45 6.69 9.54 12.9 16 7

5.72 7.00 9.93 13.4 17.3

5.86 7.16 10.2 13.6 17.6

6.19 7.55 10.7 14.3 18.4

6.70 8.14 11.4 15.3 19.6

7.07 8.59 12.0 16.0 20.5

7.38 8.95 12.5 16.6 21.3

7.64 925 12.9 17.2 21.9

8.05 9.75 13 6 18.0 23.0

128570 142860 157140 171430 185710

20.7 25.5 30.8 36.6 42.9

21.1 260 31.3 37.2 43.5

21.8 26.7 32.2 38.1 44.6

22.1 27.1 32.7 38.7 45.2

23.0 28.2 33.8 40.0 46.6

24.5 29.8 35.7 42.1 49.1

25.6 31.1 37.2 43.9 51.0

26.5 32.2 38.5 45.3 52.6

27.3 33.1 39.6 46.5 54.0

28.6 34.7 41.3 48.5 56.3

140000 200000 150000 214290 160000 228570 170000242860 180000 257140

49.7 57.0 64.8 73.1 81.9

50.4 57.7 65.6 73.9 82.8

51.5 59.0 66.9 75.4 84.3

52.2 59.7 67.7 76.2 85.2

53.8 61.5 69.6 78.3 87.5

56.5 64.4 72.9 81.8 91.3

58.6 66.8 75.5 84.7 94.4

60.5 68.8 77.7 87.1 97.0

62.0 70.5 79.6 89.2 99.3

64.6 73.4 82.7 92.6 103

140000 200000 150000 214290 160000 228570 170000 242860 180000257140

125 191 269 360 464

190000 271430 118 200000285710 130 250000 357140 197 300000 428570 277 350000 500000 370

102 159 228 310 404

108.4

.37 .44 .50 .57 .66

14300 15700 17150 18600 20000

101 157 226 308 401

65.0

.35 42 .48 .55 .63

10000 11000 12000 13000 14000

200000285710 250000 357140 300000428570 350000 500000 400000571430

43.2


.32 .37 .43 50 -58

90000 100000 110000 120000 130000

32.0

104 161 231 313 408

.94

105 162 232 315 410

For this pipe slze: v = 2.316x lo-' x gpm: h, For velocity data see page 3-29.

107 166 237 320 416

112 171 244 329 427

115 177 250 337 436

118 181 256 344 444

121 184 261 350 451

8.322x 10 'Ox gpm'

:

Note: No allowance has been made for age, difference In diameter, or any abnormal cond~tionof interlor surface. Any factor of safety must be estimated from the local c o n d ~ t ~ o nand s the requirements of each particular ~nstallation.It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

90000 100000 110000 120000 130000

.80 .94

.90 .93

127 1.42 1.57 f.72 1.67

2.05 3.39 3.73 4.08


Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safety must be est~matedfrom the local conditions and the requirements of each particular installation. It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.







- 0.6

K~nernat~c v~scos~ty-centistokes

Flow

1.13

US gal per mln

Bbl per hr (42 gal)

14000 16000 18000 20000 25000

20000 22850 25700 28600 35700

.28 .36 .45 .55 .85

.31 .39 .48 .59 -90

30000 35000 40000 45000 50000

42850 50000 57150 64290 71430

1.21 1.64 2.12 2.67 3.28

55000 78570 60000 85710 65000 92860 70000 100000 75000 107140 80000 114290 85000 121430 90000 128570 95000135710 100000 142860

21

4.3

2.7

7.4

10.3

K~nemat~c vtscos~ty-cent~stokes

13.1

15.7

20.6


1084

162 3

216 5

325

435

650

1500

2000

3000


.57 70 .84 1.27

20000 22850 25700 28600 35700

54 69 86 104 1 55

56 71 88 1 05 1 58

61 77 95 1 14 1 69

69 86 106 1 27 1 88

76 96 118 1 41 2 09

85 1 07 131 1 57 2 32

93 1 16 142 1 70 2 50

105 1 31 160 1 92 2 81

115 1 44 175 2 09 3 06

3 46

1.65 2.19 2.81 3.49 4.23

1.76 2.33 2.98 3.69 4.48

1.85 2.44 3.12 3.86 4.68

1.92 2.54 3.23 4.00 4.84

2.04 2.69 3.42 4.23 5.11

42850 50000 57150 64290 71430

215 283 360 4 45 538

221 294 376 4 65 562

233 306 388 4 79 577

259 339 429 5 28 637

287 389 491 6 03 726

318 416 525 6 46 777

343 448 565 6 94 834

384 500 630 7 72 927

417 543 683 8 36 100

471 512 767 9 38 112

5.05 5.94 6.89 7.91 8.99

5.34 6.26 7.26 8.33 9.46

5.57 6.53 7.57 8.67 9.85

5.76 6.75 7.82 8.96 10.2

6.08 7.12 8.23 9.42 10.7

78570 85710 92860 100000 107140

638 747 864 988 112

667 780 901 103 117

685 800 925 106 121

754 880 102 116 131

858 100 115 131 148

919 107 123 141 159

986 115 132 151 170

109 127 146 167 188

118 137 158 180 202

132 154 176 200 226

.42 .52 .64 .97

.41 .53 65 .79 1.19

1.27 1.71 2.21 2.78 3.40

1.36 1.82 2.35 2.93 3.59

1.41 1.88 2.42 3.02 3.68

1.51 2.01 2.57 3.21 3.90

3.96 4.70 5.50 6.36 7.28

4.09 4.85 5.66 6.54 7.48

4.30 5.08 5.92 6.83 7.80

4.41 5.21 6.07 6.99 7.97

4.67 5.50 6.39 7.35 8.37

8.27 9.32 10.4 11.6 12.9

8.49 9.55 10.7 11.9 13.1

8.83 9.93 11.1 12.3 13.6

9.02 10.1 11.3 12.6 13.9

9.46 10.6 11.8 13.1 14.5

10.2 11.4 12.7 14.0 15.4

157140 171430 185710 200000 228570

15.5 18.4 21.6 25.0 32.6

15.8 18.8 22.0 25.4 33.1

16.4 19.4 22.6 26.1 33.9

16.6 19.7 23.0 26.5 34.4

17.3 20.5 23.9 27.5 35.5

180000 257140 200000 285710 250000 357140 300000428570 350000 500000

41.2 50.7 79.1 114 154

41.7 51.4 79.9 115 156

42.7 52.5 81.3 116 158

43.3 53.1 82.2 117 159

400000571430 450000 642860 500000 714290 550000785710 600000857140

202 255 314 380 452

203 256 316 382 454

205 259 319 386 458

207 261 321 388 461 -

65 0

.52 .66 .82 .99 1.47

.37 .47 .59 .71 1.08

For thls plpe size: v = 1.773x lo-' x gpm; h, For velocity data see page 3-30.

432

.49 .62 77 .93 1.38

.35 -44 -54 .66 1.00

.34

100

32 0

.47 .60 .74 .89 1.33

50

33

. Bbl Per hr (42 gal)

26 4

80

40

31.5

-)W

70

35

110000 120000 130000 140000 160000

FRICTION


INGERSOLL*AND

60 .44

125

150

200

300

500

750

1000

l.44

1 . S

10.7

11.1

11 9

13.3 14.7 16.1

12.4 13.8 15.2 16.8

11.4 12.8 14.2 15.7 17.3

12.0 13.4 14.9 16.5 18.1

114290 121430 128570 135710 142860

126 141 156 172 189

131 146 162 179 197

136 152 167 187 205

147 164 181 200 219

166 185 205 225 247

184 205 227 249 273

190 212 234 258 282

21 0 234 259 284 311

227 252 278 306 334

252 280 309 339 371

18.4 21.7 25.3 29.1 37.3

19.3 22.7 26.3 30.3 38.9

20.0 23.5 27.3 31.3 40.2

20.6 24.2 28.0 32.2 41.2

21.5 25.3 29.3 33.6 43.0

157140 171430 185710 200000 214290

225 264 30 5 350 397

234 274 31 7 36 3 412

245 287 333 382 434

260 304 35 1 40 1 455

292 341 39 4 449 508

323 377 43 4 49 5 559

334 390 44 9 51 3 580

368 429 494 56 3 635

395 460 529 603 681

438 509 58 5 666 752

44.6 54.7 84.2 120 162

46.6 56.7 87.7 125 168

48.6, 59.3 90.6 128 172

50.1 61.1 93.1 131 176

51.4 62.6 95.1 134 180

53.5 65.1 98.7 139 186

211 265 326 393 467

217 273 335 403 478

223 279 342 411 487

227 285 349 419 496

232 290 354 426 503

239 298 364 437 516

4.877x 10 " ' x gpm2.

Note: No allowance has been made for age, d~fferencein diameter, or any abnormal condit~onof interlor surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

197 253 315 384 459 Figures in shaded area i For velocity data see p

laminar (viscous) flow. e 3-30.

I

Note: NO allowance has been made for age, difference in diameter, or any abnormal condition of interior surface. Any factor of safety must be estimated from the local conditions and the requirements of each particular installation. It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

INGERSOLLflAND CAMERON HYDRAULIC DATA Friction Loss for Viscous Liquids-4000

SSU to 20000 SSU


Loss in Feet of Liquid per 1000 Feet of Pipe 11/4" to 6" pipe sizes-Schedule 40 Laminar flow-figures

suitable for any interior roughness

Friction Loss for Viscous Liquids-4000 SSU to 20000 SSU (cont.) ( ~ a s e d - o nDarcy's Formula)

Loss in Feet of Liquid per 1000 Feet of Pipe 3" to 18" pipe sizes-Schedule 40 Laminar flow-Figures

suitable for any interior roughness

Lok

Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interlor surface. Any factor of safety must be estimated from the local cond~tlonsand the requirements of each particular installation. It is recommended that for most commercial design purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.

Darcy formula for laminar (viscous) flow-hf 1587.6 d' in which-h, = friction loss-ft of liquid; L = length of pipe-ft: gpm = flow-gal per min; k = kinematic viscostty-centlstokes: d = ~nternalpipe d ~ a - ~ nWarnlng: This formula for lamlnar flow only, 1.e. for Reynolds number less than 2000. Note: No allowance has been made for age, difference in diameter, or any abnormal condition of interlor surface. Any factor of safety must be estimated from the local conditions and the requirements of each Particular installation. It is recommended that for most commercial deslgn purposes a safety factor of 15 to 20% be added to the values in the tables-see page 3-5.


FRICTION- PAPER STOCK

Friction losses-paper stock flow Curves relating friction loss to stock flow in pipes are shown on pages 3-91 to 3-101. These curves are based on the University of Maine's correlation of the Brecht and Heller data*. That data correlation produced a relationship between a pseudo-Reynolds Number "Re" and a friction factor "f" as shown on the chart on page 3-90. The following equations are applicable here: (1)

pseudo-Reynolds Number "Re"

(2)

**friction factor "f"

(3)

average stock velocity "V"

(4)

friction loss "hff' =

=

=

x V x p C1.157

1 I

3.97 R61.636 =

Q x 0.321 A

I

fxV2xLxK D

where: A = C = D = f = hf = K = L = p = Q= Re =

V

=

Pipe flow cross-sectional area -square inches % stock consistency -oven dry Inside diameter of pipe -feet. Friction factor**-see page 3-90 Friction loss-feet of water Friction factor multiplier (see page 3-89) Length of pipe-feet Stock density-lbs./ft3 (assumed to be 62.4) Volumetric flow rate -U. S. gallons/minute Pseudo-Reynold's number Average stock velocity in pipe-feetisecond

* Acknowledgements,

with the permission of TAPPI Brecht and Heller-TAPPI Vol. 33, No. 9 Durst, Chase and Jenness-TAPPI Vol. 35, No. 12 Durst and Jenness-TAPPI Vol. 37, No. 10 P. S. Riegel-TAPPI Vol. 49, No. 3 ** Note: This friction factor "f" is not related in any way to the Darcy-WeisbachColebrook friction factor previously discussed-(page 3-3). Note: For pump performance corrections when handling stock see discussion on page 4-49.

Given the pipe size, stock flow, and stock consistency, the stock velocity and Re number can be calculated using equations (3) and (1). The friction factor "f" corresponding to the calculated Re number can be taken from the chart on page 3-90 or calculated using equation (2). By using the appropriate given and derived values in equation (4), the stock line friction loss can be calculated. Friction loss values shown on the accompanying curves were derived in the foregoing manner for various diameters of schedule 40 steel pipe. For pipe diameters other than those shown, it is necessary to calculate friction loss values as described above. Although the R4 number was originally derived on an OD stock consistency basis, the friction loss curves shown here were calculated on the AD consistency basis, resulting in somewhat larger loss values and, therefore, more conservative results. Stock temperatures between 18°C and 35°C (65°F and 95°F) will not appreciably affect friction loss; higher temperatures should give somewhat lower friction losses. For stock consistencies below 2.0%, use water friction values. Stock velocity should not exceed 10 feetlsec. for stock consistencies of 3.0% or lower; for consistencies higher than 3.0%, maximum stock velocity should be 8 feetlsec.

1

The friction loss curves are based on unbleached, unrefined softwood sulfite pulp; for other types of pulp, the following multiplier values (K) may be applied:

T y p e of P u l p

i

Unbl. Sulfite- SW B1. sulfite-SW Unbl. kraft -SW Soda-HW Reclaimed fiber Pre-steamed groundwood -SW Stone groundwood- SW

*CSF -ml 640 560 730

200 70

Friction Factor Multiplier ( K ) 1.00 0.90 0.90 0.90** 0.90"" 1.00 1.42

* Canadian Standard Freeness ** Courtesy of Goulds Pumps, Inc. Note: This friction factor multiplier (K) is not related in any way to t h e resistance coefficient K i n t h e tables on pages 3-110 t o 3-121.

INGERSOLLRAND



Friction Factors for Stock Flow in Pipes

Friction of Paper Stock (Continued)

Friction Factor-"f"

Loss in feet of water per 100 ft of pipe Basis unbleached sulphite pulp-air dry

" f " FACTOR

g w 8

$

994904

0

0

0

0

Pq"?drn

0

0

c u -

0000 0 O Q ) b ( O V) 9999 9

0"

m

8 8

9

0

g

g

9

9

9

w

3 Inch

8

' f " FACTOR

I

.

/

I

50

,

I

.

I

/

I

100 F L O W150 -US G ZOO PM

I

250

I

1

1

1

1

1




6 lnch

4 lnch

1

bO

1

DO

I

1

I

150 200 250 FLOW-US GPM

I . . ,

300


I



I

I

I

360

I

400



INGERSOLLRAND


Friction of Paper Stock



10 lnch

8 lnch

I

1

I

.

1

I

1000 FLOW-US GPM

I

I

1500

1

u460

do

I

jZm

1200

FLOW-US GPM

2400 2d00 ~ Q O O







14 lnch

12 lnch

FLOW - US GPM

0

I

0

m

1

,

1000

. I ,

I

I

,

,

I

,

2000 3000 4000 5000 F L O W - U S GPM


FRICTION- PAPER STOCK Friction of Paper Stock (Continued)




18 lnch

16 lnch

. I

0

I

'

I 1

8

I

#

'OoO ?eO~oOfS

I

I

.

,

L

.

4000 so00 6000 OPM

.

I

1000 2000 3000 4000 5000 FLOW -US GPM

. -

-i i 6000 7000

INGERSOLLRAND


Friction of Paper Stock (Continued) Loss in feet of water per 100 ft of pipe Basis unbleached sulphite pulp-air dry 20 Inch

FRICTION- PAPER STOCK Friction loss in fittings- (paper stock) To determine frictional resistance of paper stock flowing in elbows and tees use the chart on page 3-102; these curves are drawn for 90" short radius elbows. To determine the frictional resistance for either 90" long radius elbows or 45" elbows, multiply the results obtained from the chart by a 0.8 factor. To determine the frictional resistance of a standard tee, multiply the results obtained from the chart by a 1.7 factor. The following example demonstrates how to use the chart. Find the frictional resistance in an 8 in. schedule 40, short radius 90" steel elbow for 900 gallons per minute of 3% air dry consistency unbleached sulphite paper stock. Entering the chart with 900 gallons per minute, move horizontally to the intersection of the 8 in. curve. Proceeding vertically to the intersection of the 3% air dry consistency curve results in a frictional resistance value of 1 foot. For fittings with internal diameters different from schedule 40 steel fittings, it is necessary to determine the'flow velocity. The chart can then be entered on the velocity scale and projected upward to the intersection with the consistency curves. The frictional resistance can now be read as before. For the various types of paper stock, the K values from the table on page 3-89 should be used as multipliers of the frictional resistance. See Page 3-103 for general information on Pulp & Paper Industry.

0

I000 2000 3000 4000 5000 6000 X)OO 8000 9000 F L O W - U S GPM

INGERSOLL-RAND CAMERON HYDRAULIC DATA Friction of Paper Stock (Continued) Through 90" Elbows % AIR

DRY CONSISTENCY

PAPER STOCK DATA

I

General Information -Pulp and Paper Industry* Dejnitions of Corn rnonl y Used Terms.

6% 5 % 4k%

Fiber(s):

Cellulosic cell structures derived from the original plantlife source or from previously manufactured paper products; normally considered as water insoluble.

Pulp:

A composite mixture of cellulosic fibers constituting the basic material used for paper making.

Stock:

A designation of pulp (fibers) in process flow. In this Section, the terms "stock" or "paper stock" denote pulp (fibers) and water mixtures or suspensions. This usage excludes the presence of non-cellulosic materials such as fillers or dissolved solids.

Consistency:

Equivalent to the terms "suspended solids" or "insoluble solids." In this Section, "consistency" is defined as the fiber or pulp content expressed as a weight percentage of a paper stock, pulp slurry, or pulp cake (fiber-water mixtures).

Oven Dry:

Abbreviated as OD and signifying a moisture-free condition of pulp (fibers).

Air Dry:

Abbreviated a s AD and denoting an assumed moisture content of lo%, on a wet weight basis, for a pulp (fibers). AD value

=

1.11 x OD value

OD value

=

0.90 x AD value

Tons Per Day: Pulp mill production rate, generally expressed a s tons of OD or AD pulp per day or 24 hours. The production rate can be calculated a s follows: Short Tons of Pulp per Day =

Courtesy Goulds Pumps, Inc.

3-102

* Courtesy of

(Stock Flow in U S GPM) (C) (0.06)

Where: C

=

stock consistency expressed as a percentage

0.06

=

derived constant

IMPCO Division, Ingersoll-Rand Company, Nashua, N.H. 03060.

3- 103

PAPER STOCK DATA Notes: (1) Use OD consistency value to obtain OD pulp production rate.

Commonly required weight-volume relationships a r e listed in Tables 1, 2, 3 and 4 along with values calculated using the equations shown in Table 1. Constants used are:

Use AD consistency value to obtain AD pulp production rate. (2) The equation constant, C, was derived by use of water density value of 8.34 1blU.S. gallon, the density value a t 55°F; therefore, the equation is accurate only a t stock consistencies of 0.1% or less, and a t a stock temperature of 55°F. Solutions of the production rate equation for a normal range of stock flow and consistencies are shown on the chart on page 3-109. Example: What is the flow in US GPM of 5.0% OD consistency stock equivalent to a production rate of 100 short tons of OD pulp per day? Solution: Locate 100 TPD value on Y-axis and follow horizontal line until it intersects the 5.0% consistency line. Follow vertical line from the point of intersection to the X-axis and read 333 U S GPM a s the stock flow equivalent. Note:

Chart can be used for either OD or AD values but not for mixed values.

Weight and V o l u ~ n eRelatiov~shipsfor Cellulose Fiber-Water Susperzsions The accompanying Tables (1, 2, 3 and 4) indicate weight and volume relationships for cellulose fiber-water suspensions. The appropriate values given in Tables 2, 3 and 4 were calculated to reflect stock density change with change in pulp (fiber) content of the stock. An equation, shown below, was derived to enable calculation of stock density a t any given stock consistency. Stock Density (lblgal)

=

(8.34)

+ (3.33

x % cons.)

Where: 8.34 = lb water in US Gal. @ 55°F 3.33 = rate of change factor % Cons. = % OD Stock .consistency, expressed a s a decimal.

(1) 1.388

=

2000 lblshort ton 1440 minutestday

(2) 7.48

=

*U.S. GallonslCubic Foot

**lb/U.S. Gallon of water @ 55°F (corresponding to 62.39 lb per cu ft.) In using the equations in Table 1 the values for Column E should be determined first, then proceed alphabetically starting with Column B. (3) 8.34

=

Table 1. Explanation of Equations Used A = % O.D. consistency

A

B=- 1.388 E

Gal of stock per min per ton of O.D. fiber per 24 hours

C = E x 7.48 D

= 1 = E x 7.48

-1 C

A E=-XL 100 F

=

Lb of O.D. fiber in 100 lbs of stock. % O.D. cons.

1 =

-

1

C

Lb of O.D. fiber i n 1 cu ft of stock

D

Cu ft of stock having 1 lb of O.D. fiber

E

Lb of O.D. fiber in 1 gal of stock

F

Gal of stock having 1 lb of O.D. fiber

L XEL 100 G=--- 1.388 E x 7.48 'H =

I

J =

-

1.388 C

Cu ft of stock per min per ton of O.D. fiber per 24 hours

1 388 x L E 100 = A

1 1

1

1

-1-00 I A

1

K = --I L = 8.34 +

Lb of stock per rnin per ton of O.D. fiber per 24 hours

1

x - = 1-

8.34 x

2000 =

8.34

3.33 x 100

I 8.34 -

2000

I

Lb of water per lb of O.D. fiber

J

Gal of water per Ib of O.D. fiber

K

Gal of water per ton of 0.D fiber

L

Lb total wt per gal of stock

8.34

Table 2-Weight

$0 w Q, 0

and Volume Relationships for Cellulose Fiber-water Suspensions Range 0 000% to 1 60%

Based on oven dry (OD) f ~ b e r % Cons

Gal of stock per mln per

Cu ft of

ton of OD

Lb of OD

f~berIn 100

f ~ b e rper 24

f ~ b e rIn 1 cu

Ib of stock

hours

ft of stock

,000 0.05 0 10 0 20 0.30 0 40 50

330.5 173.5 83 1 55.5 41 6 33 2

0 0314 0.0598 0 127 0 187 0.247 0 313

55 60 65 .70 75

30 2 27 7 25.6 23.7 22 1

0.344 0 375 0 406 0.438 0 469

.80 85 90 .95 1 .OO

20.7 19 5 184 17.5 16 6

1 10 1 20 1 30 1 40 1.50

15 1 13 8 12.8 11 8 11 0

Lb of OD

*

stock hav~ng

Cu ft of stock

Lbs of stock

per rnln per

per mln per

Lbs o f OD

Gal of stock

ton of OD

ton of OD

Lbs of water

Gal of water

Gal of water

Lb total wt

1 Ib of OD

f ~ b e rIn 1

hav~ng1 Ib

f ~ b e rper 24

f ~ b e rper 24

per Ib of OD

per Ib of OD

per ton of

per gal of

fiber

gal of stock

of OD fiber

hours

hours

f~ber

ftber

OD f ~ b e r

stock

31.9 16.9 7.87 5 35 4 05 3 20

004? -008 ,017 .025 ,033 ,042

238 125 58.8 40.0 30.3 23.9

44 2 23.2 10.9 7.42 5 62 4 44

2757 1447 682 464 351 278

1999 999 499 332 249 199

240 120 59.8 39.8 29.9 23 9

479377 239568 11 9664 79617 59713 47722

8.34 8 34 8 35 8 35 8 35 8.36

2.91 2 67 2 46 2.29 2 13

,046 ,050 054 ,058 ,0627

21.8 19.9 18.4 17.1 16.0

4.04 3 70 3.42 3.17 3.00

253 231 214 198 185

181 166 153 142 132

21 7 19.9 18.3 17.1 15.9

43406 39808 36691 34053 31655

8.36 8 36 8.36 8.36 8.36

0.500 0 532 0.563 0.595 0.626

2 00 1.88 1.78 1 68 1.60

,067 ,071I ,0753 0795 ,0837

15.0 14.1 13.3 12.6 12.0

2 77 2.61 2.47 2 34 2 22

174 163 154 146 139

124 117 110 104 99

14.9 14.0 13 2 12 5 11 9

29736 28058 26379 24940 23741

8 37 8.37 8.37 8.37 8.37

0.689 0.751 0.814 0.877 0.941

1.45 1 33 1.23 114 1.06

,0922 1006 ,109 ,117 ,126

10.9 9.95 9.18 8.53 7.95

2 01 1.85 1.70 1.58 1.48

126 116 107 99.2 92.5

10 8 9.87 9.10 8.45 7.87

21583 19736 18202 16883 15756

8 38 8.38 8.38 8 38 8.39

90 82 3 75 9 70 4 65.7

Basis U.S. Gallons.

" Basis temperature of approximately 55'F

Table 3-Weight

and Volume Relationships for Cellulose Fiber-water Suspensions

Based on oven dry (OD) f ~ b e r

"O

Cons

Gal of stock per mln per

Y C-L

0 -1

Range 1 60% to 5.00%

Cu ft of

Cu ft of stock

Lb of stock

per mln per

per mln per

Lb of OD

ton of OD

Lbs ot OD

Lbs ot OD

Gal of stock

ton o f OD

ton o f OD

Lb of water

Gal of water

Gal of water

Lb total wt

f ~ b e rIn 100

f~berper 24

ftber In 1 cu

1 Ib of OD

f ~ b e rIn 1

hav~ng1 Ib

f ~ b e rper 24

f ~ b a rper 24

per Ib of OD

per Ib of OD

per ton of

per gal of

Ib of stock

hours

ft of stock

f~ber

gal of stock

of OD f ~ b e r

hours

hours

f~ber

f~ber

OD f ~ b e r

stock

1 0038 1 0666 1 130 1193 1 256

0 996 0 938 0 885 0 838 0 796

134 143 151 160 168

7 45 7 01 6 62 6 27 5 95

1 1 1 1 1

38 30 23 16 10

86 7 81 7 77 1 73 1 69 4

61 5 57 8 54 6 51 6 49 0

7 37 6 93 6 54 6 19 5 88

14748 13861 13094 12374 11751

8 39 8 39 8 40 8 40 8 40

1 383

stock hav~ng

1 60 1 70 1 80 1 90 2 00

10 3 9 73 9 19 870 8 26

2 20 2 40 2 60 2 80 3 00 3 25

7 51 6 88 6 34 5 88 5 49 5 06

1510 1 637 1 765 1 892 2 05

0 723 0 662 0 611 0 567 0 528 0 487

185 202 219 236 253 274

5 41 4 95 4 57 4 24 3 95 3 65

1 00 0 919 0 848 0 787 0 733 0 676

63 2 57 9 53 4 49 6 46 3 42 7

44 5 40 7 37 5 34 7 32 3 29 8

5 33 4 88 4 49 4 16 3 88 3 57

10672 9760 8993 8321 7746 7146

8 41 8 42 8 42 8 43 8 44 8 44

3 50 3 75 4 00 4 25 4 50

4

69 4 38 4 10 3 85 3 64

2 21 2 37 2 53 2 69 2 85

0 452 0 422 0 395 0 371 0 350

296 31 7 339 360 382

3 38 3 15 2 95 2 78 2 62

0 628 0 585 0 548 0 515 0 486

39 7 37 0 34 7 32 7 30 9

27 6 25 7 24 0 22 5 21 2

3 31 3 08 2 88 2 70 2 54

6619 6163 5755 5396 5084

8 45 8 46 8 47 8 48 8 48

4 75 5 00

34 4 3 27

3 02 3 18

0 332 0315

403 425

2 48 2 35

0 460 0 437

29 2 27 8

20 1 19 0

2 40 2 28

4820 4556

8 49 8 50

PAPER STOCK DATA

INGERSOLL-RAND CAMERON HYDRAULIC DATA Weight-Volume Relationshies

Pulp and Paper Data Relationship of Pulp Production Rate to Stock Flow At Various Stock Consistencies (Tons of Pulp per 24 Hours Versus U.S. G.P.M.)

b

0.2

"Ebz

C

cnwmom m m c c m

cnm*o* mcu-om

or-mmcmm

o-mmm

U ~ N - O

CDmNr n ~ o h ommr-ICAY

q q0 q0 q 0q 00

q0 ?0 ?0 q0 0

0 0 0 0

0 0 0 0 0

00000

m*v* or-omrNe o N-N qN . p crqr qr k rrq-

t m o m h

momu~mm

-----

c n ~ m o m m t r - 9 c -q -t -tqt o $ $o &o c qo

t t r - '

qqqqq

$?%;?

00000

m m ( ~ m ---cum

mw-om

cum*r-o

~ m t -vwmm

0000

00000

KG;:?

;:?no

mmr-cn

x g ; ~ gw;~;

00000

0000

00000

00000

0

moor-

nmwcum cqm-qq """U

m-mom w q q - 7 "om"

- o w m a m - ~ c q -

o o m m

cu qamocq cnEZ>F

qoqo?

-

r-cowm m-me

mme-: momcu

qqmo m q0o0 q0 o 00

0000

L

---- ----.-

3

~ 0 0 0 00 0

a-=

5&?& 2.-e

-

-,0 0

00000

$ 2 T F $ 3o

m m-

a=0

cn cO

.,,,-

$

O

L

" 0 -

,0

00000

o- m a r - : o m o m

*

y : o ? % $ a s ~ s s s sS

V)

a 0=':0

- c z -"""" m?rq

z ... aq

mmme c c m m ""'"

Jg-

1 1 1 1 o

woX

EE ao g z aG 3z

e

n

-OOON

:;''': :::;:

n @ m ~ om m o w m

1

mmwz

2 z z z z llrL

mF-Nz mh-UY

CLnZzz

&

1 /1 0.7-6JN cmmr-m

szz2z Eidzx

Note: Use OD 70 Consistency with Tons of OD Pulp. Use AD 'fi Consistency with Tons of A D Pulp.

INGERSOLLRAND


Friction of Water Head Losses Through Valves and Fittings Head losses (hf) through valves, fittings, sudden contractions and efilargements, entrance and exit losss can be expressed in terms of the velocity head (V2/2g)by using the applicable resistance coefficient (K) in the equations:

Select applicable (K) from tables on pages 3-111 to 3-117; select (V) for average velocity in pipe of diameter required to accommodate fitting; see examples on page 3-119. A second method of expressing head losses (hf) through valves and fittings etc. is in terms of the equivalent length of straight pipe that will produce the same loss as calculated by the Darcy-Weisbach equation for straight pipe. (See table on page 3-120). The applicable equations are:

where d = pipe diameter-inches D = pipe diameter in feet f = friction factor (from chart, Page 3-11) for zone of complete turbulence. g = gravitational constant -32.174 ft/sec2 hf = head loss in feet of liquid K = resistance coefficient (from tables on pages 3-111 to 3-120) is based on test data, or extrapolated from test data; and depends on design, size and type of fitting. L =friction loss in pipe fittings in terms of equivalent length in feet of straight pipe (See table page 3-120). V = average velocity in pipe of diameter required to accommodate fittingftlsec. From the above one can solve for (L) and LID ratio using the value of K from the tables and selecting f for the zone of complete turbulence. A third method of expressing head losses, particularly for control valves, is in terms of a flow coefficient C,. This is defined as the flow of liquid at 60°F in gallons per minute at a pressure drop of one pound per square inch across the valve. The relationship of C, and K is shown by the following formulas. 29.9 x d2 894 x d4 C, = -------- and K = (CJ2 The tables on pages 3-111 to 3-119 list K values for schedule 40 pipe in sizes up to and including 24" and are based on flows for complete turbulence. Since the K values between pipe sizes are close, it is reasonable to interpolate between sizes if they do not correspond to schedule 40 diameters. For K values for pipes larger than 24" it is suggested that the 24" value be used. The above text and tables on pages 3-111 to 3-120 are based on material in Crane Co. Technical Paper No. 410*. Reference to this paper is suggested for more complete review of this subject.

a

* I t should be noted that there is considerable variation in published values of resistance coefficient K for different valves and fittings.

FRICTION- WATER-PIPE FITTINGS Friction of Water (Continued) Friction Loss in Pipe Fittings Resistance coefficient K

use in formula h, = K

.

" 29

i

INGERSOLLRAND CAMERON HYDRAULIC M A

Friction of Water (Continued) Friction Losses in Pipe Fittings

Friction of Water (Continued) Friction Losses in Pipe Fittings Resistance coefficient K

z

0

1

-

u,

m

Q,

r.

0

2

g

A

-

In

0;

2

Q

t-

2

w

-

I-

m

)

7

'

3

& N m2 ' m C g

z

Y C

U

-

N

X

F

( 0 0 )

Q)

2 2

0 r

-

m

v-

2:

W

C

2

In

0

7

F

7

0

2

m

0

CU

*

2

2 *

w

2

S

-

-

2

I-

-

-

.-

,rr

. 13

2

z z

2

P O I

m

I - 0

0

v - r .

2:

I-

2

2 2

2

0,

0

7-

$ 3 0 0

" 2

W

Q

W v )

LD

0

.-

$ 2

Q,

I-

z

O I L

$ 2

2

I n 0

0

e

-

P

2 2

m

'9

0

0

rp*

.-

.r

2

w

.-

-

7

U7P

N

7

X

f

N

N

0

0

3

.-

U

2 :

2 2

7-

F

In

2

e

Q

m

2

v

$

.gl n

use in formula h, = K -

2

2

7

a

I N

Resistance coefficient K use in formula h, = K -

i

2

2 I-

In

u,

In

0

0

CU

2;

2

rn

-

m

7

0

X

2

2

e

0

0

m

'?X

2

g z

? I an

0

a

C

2 =

Z J - ~f

z "

a e1.X i

rf 01

E

i .

.4

5 w.

;

,q;rl-" U

w a rn

-n

e+i~

-0

-

qii!l 0

w rn h

FRICTION- WATER-PIPE FITTINGS

I Eu

L

\



INGERSOLL-RAND CAMERON HYDRAUUC DATA Friction of Water (Continued) Friction Loss in Pipe Fittings Resistance coefficient

Pipe exit

I .-

--I

1

*

1 -

Pipeentrance

I Pipe entrance flush

use in formula h, = K

K value

Description projecting sharp edged rounded inward projecting

0.78

sharp edged

0.5

=

0.02

rld = 0.04

0.28 1

0.24

0.06

0.15

rld =0.10

0.09

rld

From Crane Co. Technical Paper 410.

All pipe sizes

rld

=

FRICTION- WATER-PIPE FITTINGS Friction of Water (Continued)

i

Fitting

i

INGERSOLLRAND


CAMERON HYDRAULIC DATA --


Friction of Water Friction toss in Pipe Fittings

Formulas for Calculating "K" Factors for Sudden and Gradual Contractions and Enlargements

Resistance coefficient K use in formula h, = K -

(K values are for velocity in the small pipe) Gradual Contraction (Based on velocity in small pipe)

- I

a?

~ d ,

il

d,

I'

The K factors in the table below are given for use in making estimates of friction loss for fittings not covered in the preceding pages.

a, I

Type of fitting

K value

Disk or wobble meter Rotary meter (star or cog-wheel piston) Reciprocating piston meter Turbine wheel (double-flow) meter Bends having corrugated inner radius

3.4 to 10 10 15 5 to 7.5 1.3 to 1.6 times value for smooth bend

Example: Determine L (Friction loss in pipe fittings in terms of equivalent length in feet of straight pipe). Assume a 6" angle valveSchedule 40 pipe size. Select K from table on page 3-111; select D and f for schedule 40 pipe from table below where D is pipe diameter in feet.

Gradual Enlargement (Based on velocity in small pipe)

Pipe size inches sch. 40

D Feet

f

Y2

0.0518 0.027

%

0.0687 0.025 0.0874 0.023 0.115 0.022 0.1342 0.021 0.1723 0.019

1 4

1% 2


2% 3 4 5

6 8

D Feet

0.2058 0.2557 0.3355 0.4206 0.5054 0.6651

f


D Feet

f

0.018 0.018 0.017 0.016 0.015 0.014

10 12 14 16 18 20

0.835 0.9948 1.0937 1.250 1.4063 1.5678

0.014 0.013 0.013 0.013 0.012 0.012

Pipe size inches

D Feet

f

24 30* 36. 42' 48'

1.8857 2.3333 2.8333 3.3333 3.8333

0.012 0.011 0.011 0.010 0.010

Based on 1"thick wall

K=

2.6 sin

2

Solution: For angle valve in 6" pipe 1-

dl2

d?)

K from page 3-1 11 = 2.25; D = 0.5054; f = 0.015 L = -KD f

-

2.25 x 0.5054 = 75.8 ft.-equivalent 0.015

length of straight

pipe. (this is shown in the table on page 3-120)

v2

Substitute above values of K in formula h, = K If desired, 2g areas can be used instead of diameters in which case substitute a, dl2 for a2 dZ2

and

(:]2f~r(--)

For an example not covered in the table on page 3-120, take a 4" plug valve with flow through branch (From page 3-112; K = 1.53)

dl = 30.2

ft. -equivalent

length of straight pipe.

b

u

0

m

c

D

L

mm '?=?"=?" b m w w w

maurn"0=?0? a m m m w

N

h h r - m m oyooo

II

m

L

N

?? '

Zm 0 Z



INGERSOLLflAND

N

O

U

w-"" m-mwm F N N N O

---

~

t-m ocnomwr-0-rn 7

-

2gZ

tC 7

--

-

o ~ m w m m m ~ mw o w .---cum m u *

-

Friction of Water (Continued) Resistance of Valves and Fittings to Flow of Fluids in Equivalent Length of Pipe

-

;,

11

2

0

Globc Valvc. Open mw YN'Cy? t-m-mrn - 7 -

k=?N?? N N

~ N

~

N

,- -

ON?-

- mWa t . ~ m~ m m*

U

\

_ ,

-NNPYU

S m

~5

4

CU

mCU---

8

.

- c

12%

-

m h w - U

b N m O b

~~~~~ z % $ z z $ z m m u ~ ( ~ m m m w

- - - N

~

~

(

7

# f z gN ma w$ ma wc o,

i5 P o U S

u

t j ~ l k n

2 3

n o

mdlgg

?,m G,, o N w . 7 - - N

-NUlOln T-:No!0 ?**-N O N ~ O ~ g~ 3 ~ m w - m - - - w ( ~

sfieee s y = c F mwlocom

- - - N N

U

-

~

-m m q ~ b (

U

~

P

C!O!T'?* T00,01r,lo , mmmmw

N O W P $ P f ~ ~b b r

0 " -

2

N

n -

--

b

u w m F T

Angle Valve, Open

~

0

Swing Check Valve, Fully Open

7

F - ( U8r n4

-??,?

q

~

0 m 7 - 7 w-mN-

mN N aO - bm %

7

0

'2

%

m e e m 0 b m m - u

7

~ 6.2 mCDh

c

- - N N ~

u m w b m

Z5'ZZZ

-

m o -

,Standard Tcr

Borda Entrance

Close Return Be 0

?

m e e m h

I1/

0

OY

-NNNO

CIoscLi Closed

m

mWo m m

W

7

I?/

-

0

N b m t ee.mw

- ( U N O ~

-

Example: The dotted line shows that the resistance of a 6-inch Standard Elbow is equivalent to approximately 16 feet of 6-inch Standard Pipe. Note: For sudden enlargements or sudden contractions, use the

Standard Tce Through Side Ou

0

7

EX%

m

L

g.&

kKjS:&

?$5'2b$

$22"

22"""E

z!2P

0 0 0 0 0

00000

0 0 0 0 0

0 0 0 0 0

0 0 0

N O -O ( UUNUOJ m w w q q q

W W U J N P

bO,COrDb-

W -

WmNOz

O W b -QNa

qFqqq

q q q ?

qqqq

LL

z m w l n 3

g .a N 0

Q*

0

3

tongSweep Elbow o r 2 run of Standard Tcc From Crane Co. Technical Paper No. 409. Data based on the above chart are satisfactory for most applications; for more detailed data and information refer to pages 3-1 10 to page 3-120 which are based on crane Co. ~echnicalPaper NO.410.

3-121

INGERSOLLRAND


Friction Losses-Valves and Fittings -Viscous Liquids Very little reliable test data on losses through Valves and Fittings for viscous liquids is available. In the absence of meaningful data some engineers assume the flow is turbulent and use the equivalent length method; i.e. where friction losses through valves and fittings are expressed in terms of equivalent length of straight pipe (see pages 3-120 and 3-121). Calculations made on the basis of turbulent flow will give safe results since friction losses for turbulent flow are higher than for laminar (viscous) flow.

Miscellaneous Formulas Discharge of fluid through valves and fittings I

gal per min

=

19.65 d2

This equation may be used for determining the flow in a system if K is the sum of all the resistances in the system including entrance and exit losses. Where: d = pipe diameter-inches hL = friction loss in feet of liquid K = sum of all resistance in the system including entrance and exit losses.

Velocity (fps) =

0.4085 gpm d2(in.)

SECTION IV

PROPERTIES OF

INGERSOLL-RAND


PROPERTIES OF LIQUIDS


Density Information

Properties of Liquids

The DENSITY of a liquid is t h e amount of mass of that liquid (lb, kg, g) contained in a unit of volume (ft", gal., m3, cm" etc.). Thus, the units of density a r e lb/ft< lblgal., kg/m3, glcm" etc.

Page Density information . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-3

Properties of water . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-4 Density-specific gravity data API scales . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-6 Properties of sodium and calcium chloride . . . . . . . . . . . . . . . . . 4-10 Properties of caustic soda . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-11 Baume scales. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-12 Densities of sugar solutions . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-13 Specific gravity of petroleum vs. temperature ............. 4-14 Specific gravity of hydrocarbons. . . . . . . . . . . . . . . . . . . . . . . . . .4-15 Specific gravity of miscellaneous liquids . . . . . . . . . . . . . . . . . . . 4-16 Specific gravities of aqueous solutions. . . . . . . . . . . . . . . . . . . . . 4-17 Specific kravities of refrigerant liquids . . . . . . . . . . . . . . . . . . . . 4-18 Vapor pressure information Vapor pressure of gasolines . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-19 Vapor pressure of hydrocarbons. . . . . . . . . . . . . . . . . . . . . . . . . . 4-20 Vapor pressure of various liquids. . . . . . . . . . . . . . . . . . . . . . . . . 4-21 Vapor pressure of refrigerant liquids . . . . . . . . . . . . . . . . . . . . . 4-22 Viscosity information. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .4-23 Viscosity conversions . . . . . . . . . . . . . . . . . . . . . . . . . . ..4-25 t o 4-28 Viscosity of crankcase oils . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-28 Viscosity of turbine oils . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-29 Viscosity of fuel oils . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-30 Viscosity of petroleum oils vs. temperature ............... 4-31 Viscosity of miscellaneous liquids . . . . . . . . . . . . . . . . . . . . . . . . . 4-32 Viscosity of refrigerant liquids . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-33 Viscosity of sucrose solutions . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-34 Viscosity blending chart . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-35 Petroleum temperature volume relations . . . . . . . . . . . . . . . . . . 4-36 Viscosities and specific gravities of misc. liquids . . . .4-37 t o 4-45 Pump performance with viscous liquids . . . . . . . . . . . . . . . . . . . 4-45 Pump performance corrections charts. . . . . . . . . . . . . 4-47 and 4-48 Pump performance on paper stock . . . . . . . . . . . . . . . . . . . . . . . . 4-49 Slurry information . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .4-50 t o 4-56 4- 2

Because gravity exerts a force called "weight" on a given mass, the t e r m s "weight density" o r gravity of a liquid a r e often used.*

I I

I

, 1

I I

The SPECIFIC GRAVITY of a liquid is its density relative t o that of water; i.e., its density divided by t h a t of water. The water temperature for this purpose is usually 60°F (15.6"C) where its density is 0.9991 g/cm3(Page 4-4). F o r some purposes a water temperature of 39.2"F (4°C) is used

as a base of reference which is its point of maximum density, namely 1.000 g/cm3; for other purposes a water temperature of 68°F (20°C) may be selected a s a base of reference. The base temperature of 60°F (15.6"C)is often specified together with t h a t of t h e liquid whose specific gravity is involved. Thus, 140°F water with a density of 0.9832 glcm3 has a specific gravity a t 140°/60"F of 0.9841 (= 0.983210.9991). I t can be seen t h a t the specified gravity of a liquid is about numerically equal t o its density in g/cm3. Measuring methods have led t o other density units, such a s degrees API or degrees Baume, which a r e related t o specific gravity through the formulas and tables on the following pages.

SPECIFIC WEIGHT a s used in various equations in this data book is t h e weight in lb p e r cu ft. The specific weight of water a t 60°F (15.6%) is 62.3714 lb/ft3; and a t 68°F (20°C) it is 62.3208 lblft? F o r other temperatures proper specific weight values should be used (see page 4-4); also for f u r t h e r discussion refer back to page 2-3. * The

density definition involves strictly mass. Weight and mass are numerically

equal a t earth sea level in the usual English system of units (where lb is properly distinguished as lb,,,, or lb,,,,,.,.). Systems that derive either the mass or force unit in terms of the other via Newton's second law of motion-expressed as F = ma-(such as the International (SI) System) do not have this numerical equality, but also do

not need the gravitational constant go = 32.174 (lb,,l,,/lbf,,,,,) ft/sec2 in calculations involving fluid motion. If the lb,,,s,-lbf,,,,.c, system is used, F = ma must be replaced by 1 F = - ma. Because of this, the factor mlg, (= 0.0311 x m in lb,,,,) per unit volume go is sometimes called mass density, even though the unit of density expressed as lb,,,,, Per unit volume is also a "mass density". See pp. 8-3 to 8-7. Note: g,, is gravitational constant a t sea level-32.174 ftisec'.


Properties of Water at Various Temperatures (Continued)

Properties of Water at Various Temperatures

Temp F

Pressure of saturated vapor lbiln2 abs

Pressure of

Speclf~cvolume f t ' Ib

gal Ib

Density speclftc wt Ib ft'

'glcm

Convers~on factor ft Ib In-

K~nematlc v~scostty cent~stokes

Tempera lure F

C

32 33 34 35

008859 009223 009600 0 09991

0016022 0016021 0016021 0 016020

01199 01198 01198 0 1198

62414 62418 62418 62 420

09998 09999 09999 0 9999

2307 2307 2307 2 307

1 79 1 75 1 72 1 68

32 33 34 35

0 06 11 17

36 37 38 39 40

0 10395 010815 011249 011698 012163

0 016020 0016020 0016019 0016019 0016019

0 1198 01198 01198 01198 01198

62 420 62420 62425 62425 62425

0 9999 09999 10000 10000 10000

2 307 2307 2307 2307 2307

1 66 1 63 1 60 1 56 1 54

36 37 38 39 40

22 28 33 39 44

41 42 43 44 45

012645 013143 013659 014192 014744

0016019 0016019 0016019 0016019 0016020

01198 01198 01198 01198 01198

62426 62426 62426 62426 6242

10000 10000 10000 10000 09999

2307 2307 2307 2307 2307

1 52 1 49 1 47 1 44 1 42

41 42 43 44 45

5 56 61 67 72

46 47 48 49 50

015314 0 15904 016514 017144 017796

0016020 0 016021 0016021 0016022 0016023

01198 0 1198 01198 01198 01199

6242 62 42 6242 6241 6241

09999 0 9999 09999 09998 09998

2307 2 307 2307 2307 2307

1 39 1 37 1 35 1 33 1 31

46 47 48 49 50

78 83 89 94 10

51 52 53 54 55

018469 019165 019883 0 20625 021392

0016023 0016024 0016025 0 016026 0016027

01199 01199 01199 0 1199 01199

6241 6241 6240 62 40 6239

09998 09997 09996 0 9996 09995

2307 2307 2308 2 308 2308

1 28 1 26 1 24 1 22 1 20

51 52 53 54 55

106 111 117 122 128

56 57 58 59 60

022183 0 23000 023843 024713 0 25611

0016028 0 016029 0016031 0016032 0 016033

01199 0 1199 01199 01199 0 1199

6239 62 39 6238 6238 62 37

09994 0 9994 09993 09992 0 9991

2308 2 308 2308 2309 2 509

1 19 1 17 116 1 14 112

56 57 58 59 60

133 139 144 15 156

62 64 66 68 70

0 27494 029497 031626 0 33889 036292

0 016036 0016039 0016043 0 016046 0016050

0 1200 01200 01200 0 1200 01201

62 36 6235 6233 62 32 6231

0 9989 09988 09985 0 9983 09981

2 309 2310 2310 2 311 2311

1 09 1 06 1 03 1 00 0 98

62 64 66 68 70

167 178 189 20 211

75 80 85 90 95

042964 050683 059583 069813 081534

0016060 0016072 0016085 0016099 0016114

01201 01202 01203 01204 01205

6227 6222 6217 6212 6206

09974 09967 09959 09950 09941

2313 2314 2316 2318 2320

0 90 0 85 0 81 0 76 0 72

75 80 85 90 95

23 9 26 7 29 4 32 2 35

100 110 120 130 140

094924 12750 16927 2 2230 28892

0016130 e016165 0016204 0016247 0016293

01207 0 1209 01212 0 1215 01219

6200 61 98 6171 61 56 6138

09931 09910 09886 09860 09832

2323 2328 2333 2 340 2346

0 69 0 61 0 57 0 51 0 47

100 110 120 130 140

37 8 433 48 9 54 4 60

150 160 170 180 190

37184 4 7414 5 9926 7 5110 9 340

0016343 0016395 0016451 0016510 0 016572

01223 0 1226 0 1231 0 1235 0 1240

6119 6099 60 79 60 57 60 34

09802 09771 09737 0 9703 0 9666

2353 2 361 2 369 2 377 2 386

0 44 0 41 0 38 036 033

150 160 170 180 190

65 6 71 1 76 7 822 878

numerlcally equal to speclflc grav~tybasls temperature reference of 39.2"F (4°C) Calculated from data in ASME Steam Tables

' Approximately

Note: For complete Steam Tables see pages 5-7 through 5-24.

saturated Temp F

vapor

Specific volume

Density specific wt.

Conversion factor

Kinematic viscosity

ftllb!inY

centistokes

0.9628 0.9589 0.9580 0.9549 0.9507 0.9464

2.396 2.406

0.31 0.29

0.9420 0.9374 0.9327 0.9279 0.9228

2.449 2.461 2.473 2.486 2.500

*

ft3!lb

gal/lb

Ib/ft3

'gi~m.~

230 240

11.526 14.123 14.696 j7.186 20.779 24.968

0.016637 0.016705 0.016719 0.016775 0.016849 0.016926

0.1245 0.1 250 0.1 251 0.1255 0.1260 0.1 266

60.11 59.86 59.81 59.61 59.35 59.08

250 260 270 280 290

29.825 35.427 41.856 49.200 57.550

0.017006 0.01 7089 0.017175 0.017264 0.01736

0.1272 0.1278 0.1285 0.1291 0.1299

58.80 58.52 58.22 57.92 57.60

200 210 212 ZT(I

lWln2 abs

2.416 2.426 2.437 0.24

Temperature

"F 200 210 212 220 230 240 250 260 270 280 290

' Approximately numerically equal to speciftc gravity basis temperature reference of 39.2"F (4°C) Calculated from data in ASME Steam Tables.

"C

93.3 98.9 100.0 104.4 110 115.6121.1 126.7 132.2 137.8 143.3



Pounds per gallon and specific gravities corresponding to degrees API at 60°F (Continued)

Pounds per gallon and specific gravities corresponding to degrees API at 60°F

Tenths of Degrees

Deg API

---I-API

Tenths of Deqrees

2

3

4

5

42 6

7

8

9

43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60 61 62

63 64 65 66

67 68 69

7o 71 72 73

74

0

1

2

3

4

5

6

7

8

9

6.790 .8155 6.752 ,8109 6.713 ,8063 6.675 ,8017 6.637 ,7972 6.600 -7927 6.563 ,7883 6.526 ,7839 6.490 ,7796 6.455 ,7753 6.420 ,7711 6.385 ,7669 6.350 ,7628 6.316 .7587 6.283 ,7547 6.249 .7507 6.216 ,7467 6.184 ,7428 6.151 -7389 6.119 ,7351 6.087 ,7313 6.056 ,7275 6.025 .7238 5.994 ,7201 5.964 -7165 5.934 7128 5.904 ,7093 5.874 ,7057 5.845 .TO22 5.817 ,6988 5.788 ,6952 5.759 .6919 5.731 ,6886

6.786 .8151 6.748 .81 04 6.709 ,8058 6.671 ,8012 6.633 .7967 6.596 ,7923 6.560 ,7879 6.523 ,7835 6.487 ,7792 6.451 .7749 6.416 ,7707 6.381 ,7665 6.347 ,7624 6.313 ,7583 6.280 ,7543 6.246 -7503 6.213 ,7463 6.180 ,7424 6.148 ,7385 6.116 .7347 6.084 ,7309 6.053 ,7271 6.022 ,7234 5.991 ,7197 5.961 -7161 5.931 .7125 5.901 ,7089 5.871 ,7054 5.842 ,7019 5.814 ,6984 5.785 .6950 5.757 ,6916 5.728 6882

6.782 ,8146 6.744 .81 00 6.705 ,8054 6.667 ,8008 6.630 ,7963 6.592 ,7918 6.556 ,7874 6.520 ,7831 6.484 ,7788 6.448 -7745 6.413 ,7703 6.378 ,7661 6.344 ,7620 6.310 ,7579 6.276 -7539 6.243 ,7499 6.209 ,7459 6.177 ,7420 6.144 .7381 6.113 ,7343 6.081 .7305 6.050 .7268 6.019 ,7230 5.988 -7194 5.958 .7157 5.928 7121 5.898 ,7086 5.868 .7050 5.839 ,7015 5.811 ,6981 5.782 ,6946 5.754 .6913 5.726 ,6879

6.779 ,8142 6.740 ,8095 6.701 ,8049 6.663 ,8003 6.626 -7958 6.589 .7914 6.552 ,7870 6.516 ,7826 6.480 ,7783 6.445 .7741 6.410 -7699 6.375 .7657 6.340 .7616 6.306 ,7575 6.273 .7535 6.240 ,7495 6.206 ,7455 6.174 ,7416 6.141 -7377 6.109 ,7339 6.078 ,7301 6.047 ,7264 6.016 7227 5.985 ,7190 5.955 ,7154 5.925 ,7118 5.895 .7082 5 866 .7047 5836 ,7012 5.808 ,6977 5779 .6943 5.751 .6909 5.723 ,6876

6.775 ,8137 6.736 ,8090 6.697 ,8044 6.660 ,7999 6.622 -7954 6.585 -7909 6.548 .7865 6.512 ,7822 6.476 .7779 6.441 ,7736 6.406 ,7694 6.371 .7653 6.337 -7612 6.303 ,7571 6.270 ,7531 6.236 ,7491 6.203 .7451 6.170 ,7412 6.138 ,7374 6.106 ,7335 6.075 ,7298 6.044 ,7260 6.013 ,7223 5.982 ,7186 5.952 -7150 5.922 ,7114 5.892 7079 5.863 ,7043 5.833 -7008 5.805 -6974 5.776 .6940 5.748 ,6906 5.720 ,6872

6.771 ,8132 6.732 ,8086 6.694 ,8040 6.656 ,7994 6.618 -7949 6.582 ,7905 6.545 ,7861 6.509 -7818 6.473 .7775 6.437 ,7732 6.402 ,7690 6.368 ,7649 6.334 ,7608 6.300 ,7567 6.266 .7527 6.233 .7487 6.199 .7447 6.167 ,7408 6.135 ,7370 6.103 ,7332 6.072 ,7294 6.040 7256 6.010 ,7219 5.979 -7183 5949 ,7146 5.919 -7111 5.889 ,7075 5.860 ,7040 5.831 ,7005 5.802 ,6970 5.773 ,6936 5.745 ,6902 5.718 .6869

6.767 ,8128 6.728 ,8081 6.690 ,8035 6.652 .7990 6.615 ,7945 6.578 ,7901 6.541 ,7857 6.505 ,7813 6.469 ,7770 6.434 .7728 6399 7686 6.365 ,7645 6.330 ,7603 6.296 ,7563 6.263 7523 6.229 ,7483 6.196 ,7443 6.164 ,7405 6.132 .7366 6.100 .7328 6.068 7290 6.037 ,7253 6.007 .7216 5.976 ,7179 5.946 ,7143 5.916 ,7107 5886 ,7071 5 857 7036 5.828 ,7001 5.799 ,6967 5.771 ,6933 5.743 .6899 5.715 ,6866

6.763 .a123 6.724 .a076 6.686 ,8031 6.648 ,7985 6.611 -7941 6.574 ,7896 6.537 ,7852 6.501 ,7809 6.466 -7766 6.430 ,7724 6.396 ,7682 6.360 .7640 6.326 .7599 6293 .7559 6.259 ,7519 6.226 ,7479 6.193 .7440 6.161 .7401 6.129 ,7362 6.097 ,7324 6.065 ,7286 6.034 ,7249 6.004 ,7212 5973 .7175 5.943 7139 5.913 -7013 5.883 ,7068 5.854 .TO33 5.825 ,6998 5.796 ,6964 5.768 ,6929 5.740 ,6896 5.712 .6862

6.759 ,8118 6.720 ,8072 6.682 ,8026 6.645 ,7981 6.607 .7936 6.571 -7892 6.534 .7848 6.498 7805 6.462 .7762 6.427 ,7720 6.392 ,7678 6.357 ,7636 6.323 ,7595 6.290 ,7555 6.256 ,7515 6.223 ,7475 6.190 ,7436 6.158 .7397 6.125 ,7358 6.094 .7320 6.062 ,7283 6.031 ,7245 6.000 ,7208 5.970 ,7172 5.940 ,7136 5.910 ,7100 5.880 .7064 5.851 ,7029 5.823 ,6995 5.793 ,6960 5.765 ,6926 5.737 ,6892 5.709 ,6859

6.756 ,8114 6.716 ,8067 6.679 .a022 6.641 ,7976 6.604 ,7932 6.567 -7887 6.530 -7844 6.494 ,7800 6.459 ,7758 6.423 ,7715 6.389 ,7674 6.354 ,7632 6.320 ,7591 6.287 ,7551 6.253 -7511 6.219 .7471 6.187 ,7432 6.154 ,7393 6.122 -7354 6.090 -7316 6.059 -7279 6.028 -7242 5.997 .7205 5.967 7168 5.937 ,7132 5.907 ,7096 5.877 -7061 5 848 .7026 5.820 ,6991 5791 ,6957 5.762 6923 5734 .6889 5.706 6856

I


INGERSOLL-RAND CAMERON HYDRAULIC DATA Pounds per gallon and specific gravities corresponding to degrees API at 60°F (Continued)

Pounds per gallon and specific gravities corresponding to degrees API at 60°F (Continued)

Tenths of Degrees

2 '7

0

5.703 ,6852 5.676 76 .6819 77 5.649 -6787 5.622 78 ,6754 5.595 79 .6722 5.568 80 ,6690 5.542 81 .6659 5.516 82 .6628 5.491 83 ,6597 5.465 84 ,6566 5.440 85 ,6536 5.415 86 ,6506 87 5.390 ,6476 5.365 88 .6446 5.341 89 ,6417 5.316 90 ,6388 91 5.293 -6360 5.269 92 ,6331 5.245 93 ,6303 94 5.222 ,6275 5.199 95 ,6247 5.176 96 ,6220 5.154 97 ,6193 5.131 98 -6166 99 5.109 ,6139 5.086 100 ,6112 1015.07 ,6086 1025.05 ,6060 103 5.02 ,6034 5.00 104 ,6008 4.98 105 ,5983 4.96 106 -5958 4.94 107 ,5933 75

1

5.701 ,6849 5.673 ,6816 5.646 ,6783 5.619 -6751 5.592 .6719 5.566 ,6687 5.540 ,6656 5.514 ,6625 5.489 .6594 5.462 .6563 5.437 ,6533 5.412 ,6503 5.387 ,6473 5.363 ,6444 5.338 ,6414 5.314 ,6385 5.291 ,6357 5.266 ,6328 5.243 .6300 5.220 ,6272 5.196 ,6244 5.174 ,6217 5.151 ,6190 5.129 ,6163 5.107 ,6136 5.09 ,6110 5.07 ,6083 5.04 ,6058 5.02 ,6032 5.00 ,6006 4.98 ,5981 4.96 ,5955 4.94 ,5930

2 5.698 .6846 5.671 ,6813 5.643 ,6780 5.617 ,6748 5.590 ,6716 5.563 ,6684 5.537 ,6653 5.511 ,6621 5.486 ,6591 5.460 .6560 5.435 .6530 5.410 ,6500 5.385 ,6470 5.361 ,6441 5.336 .641 1 5.312 ,6382 5.288 ,6354 5.264 ,6325 5.241 ,6297 5.217 -6269 5.194 ,6242 5.172 ,6214 5.149 ,6187 5.126 ,6160 5.104 ,6134 5.09 ,6107 5.06 ,6081 5.04 .6055 5.02 6029 5.00 ,6003 4.98 ,5978 4.96 ,5953 4.94 .5928

3 5.695 .6842 5.668 ,6809 5.641 ,6777 5.614 ,6745 5.587 ,6713 5.561 ,6681 5.534 ,6649 5.508 ,6618 5.483 ,6588 5.458 ,6557 5.432 .6527 5.407 ,6497 5.382 ,6467 5.358 ,6438 5.334 ,6409 5.310 .6380 5.286 ,6351 5.262 .6323 5.238 ,6294 5.215 ,6267 5.192 ,6239 5.170 ,6212 5.146 ,6184 5.124 ,6158 5.102 ,6131 5.08 ,6104 5.06 .6078 5.04 ,6052 5.02 ,6026 5.00 ,6001 4.98 5976 4.95 ,5950 4.93 .5925

4 5.693 ,6839 5.665 .6806 5.638 ,6774 5.611 ,6741 5.584 ,6709 5.558 .6678 5.532 ,6646 5.506 ,6615 5.480 -6584 5.455 ,6554 5.430 ,6524 5.405 ,6494 5.380 ,6464 5.356 .6435 5.331 ,6406 5.307 ,6377 5.283 ,6348 5.260 ,6320 5.236 .6292 5.213 ,6264 5.190 ,6236 5.167 ,6209 5.144 ,6182 5.122 ,6155 5.100 .6128 5.08 .6102 5.06 ,6076 5.04 ,6050 5.02 ,6024 4.99 ,5998 4.97 ,5973 4.95 5948 4.93 ,5923

Tenths of Degrees

6

5 5.690 ,6836 5.662 .6803 5.635 .6770 5.608 ,6738 5.582 .6706 5.556 .6675 5.529 .6643 5.503 ,6612 5.477 ,6581 5.453 ,6551 5.427 ,6521 5.402 ,6491 5.377 .6461 5.353 .6432 5.329 ,6403 5.305 ,6374 5.281 ,6345 5.257 ,6317 5.234 ,9289 5.211 .6261 5.187 ,6233 5.164 ,6206 5.142 .6179 5.120 ,6152 5.098 ,6126 5.08 ,6099 5.06 .6073 5.04 ,6047 5.01 ,6021 4.99 ,5996 4.97 .5970 4.95 ,5945 4.93 -5921

5.687 ,6832 5.660 ,6800 5.632 ,6767 5.606 ,6735 5.579 -6703 5.553 ,6671 5.526 ,6640 5.501 -6609 5.475 ,6578 5.450 .6548 5.425 .6518 5.400 ,6488 5.375 ,6458 5.351 ,6429 5.326 .6400 5.302 ,6371 5.278 -6342 5.254 .6314 5.232 ,6286 5.208 ,6258 5.185 .6231 5.162 ,6203 5.140 .6176 5.118 -6150 5.096 .6123 5.08 ,6097 5.05 ,6070 5.03 ,6044 5.01 .6019 4.99 ,5993 4.97 ,5968 4.95 ,5943 4.93 ,5918 1

7 5.685 -6829 5.657 ,6796 5.630 ,6764 5.603 ,6732 5.577 ,6700 5.550 .6668 5.524 ,6637 5.498 ,6606 5.472 ,6575 5.448 ,6545 5.422 ,6515 5.397 ,6485 5.372 .6455 5.348 .6426 5.324 ,6397 5.300 ,6368 5.276 ,6340 5.252 ,6311 5.229 .6283 5.206 ,6256 5.183 ,6228 5.160 ,6201 5.138 ,6174 5.116 ,6147 5.093 ,6120 5.07 ,6094 5.05 ,6068 5.03 ,6042 5.01 ,6016 4.99 ,5991 4.97 ,5965 4.95 ,5940 4.93 ,5916

8 5.682 .6826 5.654 -6793 5.627 .6761 5.600 ,6728 5.574 ,6697 5.548 .6665 5.522 ,6634 5.496 ,6603 5.470 6572 5.445 ,6542 5.420 ,6512 5.395 ,6482 5.370 ,6452 5.346 ,6423 5.321 ,6394 5.297 ,6365 5.274 ,6337 5.250 ,6309 5.227 ,6281 5.204 ,6253 5.180 .6225 5.158 ,6198 5.136 ,6171 5.113 ,6144 5.091 .6118 5.07 .6091 5.05 ,6065 5.03 ,6039 5.01 .6014 4.99 ,5988 4.97 ,5963 4.94 ,5938 4.92 ,5913

9 5.679 6823 5.652 ,6790 5.624 ,6757 5.598 ,6725 5.571 .6693 5545 ,6662 5.519 6631 5.493 .6600 5.467 ,6569 5.443 ,6539 5.417 -6509 5.392 ,6479 5.367 .6449 5.343 ,6420 5.319 ,6391 5.295 ,6362 5.271 ,6334 5.248 ,6306 5.225 .6278 5.201 ,6250 5.179 ,6223 5.156 ,6195 5.133 ,6168 5.111 .6141 5.089 .6115 5.07 6089 5.05 ,6063 5.03 ,6037 5.01 ,6011 4.98 .5986 4.96 ,5960 4.94 -5935 4.92 ,5911

Deg API

108 109 110 111

112 113 114 115 116 117 118 119 120 121 122 123 124 125 126 127 128 129 130 131 132 133 134 I35 136 I37 138 I39

0 4.92 ,5908 4.90 ,5884 4.88 -5859 4.86 .5835 4.84 .5811 4.82 ,5787 4.80 ,5764 4.78 ,5740 4.76 ,5717 4.74 .5694 4.72 5671 4.70 ,5649 4.69 ,5626 4.67 ,5604 4.65 .5582 4.63 ,5560 4.61 ,5538 4.59 ,5517 4.58 5495 4.56 ,5474 4.54 ,5453 4.52 ,5432 4.51 ,5411 4.49 ,5390 4.47 ,5370 4.46 ,5350 4.44 ,5330 4.42 ,5310 4.41 ,5290 4.39 ,5270 4.37 5250 4.36 ,5231

1

4.92 ,5906 4.90 .5881 4.88 ,5857 4.86 ,5833 4.84 ,5909 4.82 ,5785 4.80 .5761 4.78 .5738 4.76 ,5715 4.74 -5692 4.72 ,5669 4.70 ,5646 4.68 ,5624 4.67 ,5602 4.65 ,5580 4.63 ,5558 4.61 ,5536 4.59 ,5514 4.57 ,5493 4.56 ,5472 4.54 ,5451 4.52 ,5430 4.50 ,5409 4.49 ,5388 4.47 ,5368 4.45 -5348 4.44 5328 4.42 5308 4.40 -5288 4.39 5268 4.37 .5249 4.35 ,5229

2

3

4

5

6

7

4.92 ,5903 4.90 ,5879 4.87 ,5854 4.85 ,5830 4.83 5806 4.82 ,5783 4.80 -5759 4.78 ,5736 4.76 ,5713 4.74 .5690 4.72 .5667 4.70 ,5644 4.68 ,5622 4.66 ,5600 4.64 ,5577 4.63 ,5556 4.61 ,5534 4.59 ,5512 4.57 ,5491 4.56 ,5470 4.54 ,5449 4.52 ,5428 4.50 ,5407 4.49 ,5386 4.47 ,5366 4.45 .5346 444 -5326 4.42 .5306 4.40 ,5286 4.39 ,5266 4.37 ,5247 4.35 -5227

4.91 ,5901 4.89 ,5876 4.87 ,5852 4.85 ,5828 4.83 5804 4.81 ,5780 4.79 ,5757 4.77 ,5733 4.76 ,5710 4.74 ,5687 4.72 .5665 4.70 5642 4.68 ,5620 4.66 ,5597 4.64 ,5575 4.62 ,5553 4.61 ,5532 4.59 ,5510 4.57 .5489 4.55 ,5468 4.54 ,5446 4.52 ,5426 4.50 .5405 4.48 ,5384 4.47 ,5364 4.45 .5344 443 .5324 4.42 5304 4.40 ,5284 4.38 ,5264 4.37 ,5245 4.35 5225

4.91 ,5898 4.89 ,5874 4.87 ,5850 4.85 .5825 4.83 ,5802 4.81 ,5778 4.79 ,5754 4.77 ,5731 4.75 ,5708 4.73 ,5685 4.72 .5662 470 .5640 4.68 ,5617 4.66 ,5595 4.64 ,5573 4.62 ,5551 4.61 ,5530 4.59 -5508 4.57 ,5487 4.55 ,5465 4.53 .5444 4.52 .5424 4.50 ,5403 4.48 .5382 4.47 ,5362 4.45 ,5342 4.43 5322 4.42 5302 4.40 .5282 4.38 ,5262 4.37 -5243 4.35 5223

491 .5896 4.89 5871 4.87 -5847 4.85 ,5823 4.83 ,5799 4.81 -5776 4.79 ,5752 4.77 ,5729 4.75 .5706 4.73 ,5683 4.71 ,5660 4.69 ,5637 4.68 ,5615 4.66 ,5593 4.64 ,5571 4.62 ,5549 4.60 .5527 4.59 ,5506 4.57 ,5484 4.55 ,5463 4.53 ,5442 4.51 -5421 4.50 ,5401 4.48 .5380 4.46 ,5360 4.45 ,5340 4.43 ,5320 4.41 .5300 440 .5280 4.38 -5260 436 5241 4.35 ,5221

4.91 ,5893 4.89 ,5869 4.87 ,5845 4.85 ,5821 4.83 ,5797 4.81 ,5773 4.79 .5750 4.77 ,5726 4.75 -5703 4.73 ,5680 4.71 ,5658 4.69 ,5635 4.67 ,5613 4.66 .5591 4.64 ,5569 4.62 ,5547 4.60 .5525 4.58 ,5504 4.57 ,5482 4.55 .5461 4.53 ,5440 4.51 .5419 4.50 ,5399 4.48 ,5378 446 5358 445 ,5338 4.43 ,5318 4.41 ,5298 4.40 ,5278 4.38 ,5258 4.36 .5239 4.35 ,5219

4.91 ,5891 4.89 ,5867 4.86 ,5842 4.84 ,5818 4.82 .5794 481 5771 4.79 ,5747 4.77 .5724 4.75 .5701 4.73 .5678 4.71 .5655 4.69 ,5633 4.67 ,5611 4.65 ,5588 4.64 ,5566 4.62 .5545 4.60 .5523 4.58 ,5502 4.56 ,5480 4.55 ,5459 4.53 ,5438 4.51 ,5417 4.49 .5397 4.48 -5376 4.46 ,5356 4.44 ,5336 443 ,5316 4.41 5296 4.39 .5276 4.38 .5256 4.36 ,5237 4.35 ,5218

Values from 10.0 to 100.0API from tables publ~shedby Amerlcan Petroleum Institute. Values above 100.0API calculated by lngersoll-Rand Co.

8

9

4.90 4.90 ,5886 ,5888 4.88 4.88 ,5862 5864 4.86 4.86 ,5837 .5840 4.84 4.84 ,5813 .5816 4.82 4.82 ,5790 ,5792 4.80 :4.80 ,5768 .5766 4.78 4.78 ,5745 ,5743 4.76 4.76 ,5719 -5722 4.74 4.75 ,5696 ,5699 4.73 4.73 ,5674 .5676 4.71 4.71 ,5651 .5653 4.69 4.69 ,5631 .5628 4.67 4.67 ,5606 ,5608 4.65 4.65 ,5584 ,5586 4.63 4.63 ,5562 .5564 4.61 462 ,5540 5542 4.60 4.60 ,5519 .5521 4.58 4.58 ,5497 .5499 4.56 4.56 -5476 ,5478 4.54 4.54 -5455 ,5457 4.53 4.53 ,5434 .5436 4.51 4.51 ,5413 -5415 4.49 4.49 ,5395 ,5393 4.47 4.48 ,5372 ,5374 4.46 4.46 5354 ,5352 4.44 4.44 5334 .5332 4.42 4.43 ,5314 ,5312 4.41 4.41 .5294 5292 4.39 4.39 5272 5274 4.37 4.38 -5254 .5252 4.36 4.36 ,5235 .5233 4.34 4 34 ,5214 .5216

INGERSOLL-RAND CAMERON HYDRAULIC DATA -

Specific Gravities of Sugar Solutions

United States Standard Baume Scales

Per cent sugar (degrees Balling's or Brix) with corresponding specific gravity and degrees Baume . Temperature 60°F

Relations between Baume degrees and specific gravity Liquids heavier than water Formula-sp

gr =

145 145 . " Baume

Sp Gr 60"-60°F

Baume degrees

Sp Gr 60"-60F

Baume degrees

20 . . . . . 21 . . . . . 22 . . . . . 23 . . . . . 24 . . . .

1.16000 1.16935 1.17886 1. 18852 1.19835

40 . . . 41 . . . . . 42 . . . . . 43 . . . . . 44 . . . . .

1 38095 1.39423 1.40777 1.42157 1.43564

60 . . . 61 . . . 62 . . . . . 63 . . . . . 64 . . . . .

1.70588 1.72619 1.74699 1.76829 1.79012

1.03571 1.04317 1.05072 1 05839 1.06618

25 . . . . . 26 . . . . . 27 . . . . . 28 . . . . . 29 . . . . .

1.20833 1.21849 1.22881 1.23932 1.25000

45 . . . . . 46 . . . . . 47 . . . . . 48 . . . . 49 . . . .

1.45000 1.46465 1.47959 1.49485 1.51042

65 . . . . . 66 . . . . . 67 . . . . . 68 . . . . . 69 . . . .

1.81250 1.83544 1.85897 1 88312 1. 90789

10 . . . . . 11 . . . . 12 . . . . . 13 . . . . . 14 . . . . .

1.07407 1.08209 1.09023 1.09848 1.10687

30 . . . . . 31 . . . . . 32 . . . . . 33 . . . . 34 . . . . .

1.26087 1.27193 1.28319 1.29464 1.30631

50 . . . . . 51 . . . . 52 . . . 53 . . . . . 54 . . . . .

1.52632 1.54255 1.55914 1.57609 1.59341

70 . . . . . 71 . . . . 72 . . . . 73 . . . . . 74 . . . . .

1.93333 1.95946 1.98630 2.01389 2.04225

15 . . . . . 16 . . . . 17 . . . . 18 . . . . . 19 . . . . .

1.11538 1 12403 1.13281 1.14173 1. 15079

35 . . . . . 36 . . . . . 37 . . . . . 38 . . . . . 39 . . . . .

1.31818 1.33028 1.34259 1.35514 1.36792

55 . . . . . 56 . . . . . 57 . . . . 58 . . . . 59 . . . . .

1.61111 1.62921 1.64773 1.66667 1.68605

75 . . . . . 76 . . . . . 77 . . . 78 . . . 79 . . . .

2.07143 2.10145 2.13235 2.16418 2.19697

Sp Gr 60"-60°F

Baurne degrees

.....

1.00000 1.00694 1.01399 1.021 13 1.02837

5 .... 6 ..... 7 .... 8 .... 9 .....

Baume degrees 0 1 2 3 4

..... . . . . ..... .....

Liquids lighter than water Formula

130 + " Baume

-

Sp Gr 60'-60'F

Per cent sugar Balling's or Brix 60°F15.56"C

Specific gravity 6O"16O0F

0 1 2 3 4

Degrees Baume 60°F

Per cent sugar Balling's or Brix 60°F15.56"C

Specific gravity 60"160°F

1.0000 1.0039 1.0078 1.0118 1.0157

0.00 0.56 1.13 1.68 2.24

34 35 36 37 38

5 6 7 8 9

1.0197 1.0238 1.0278 1.0319 1.0360

2.80 3.37 3.93 4.49 5.04

15 16 17 18 19

1.0613 1.0657 1.0700 1.0744 1.0788

20 21 22 23 24

Degrees Baurne 60°F

Per cent sugar Balling's or B r ~ x 60°F15.6"C

Specific gravity 60"/60"F

Degrees Baume 60°F

1.1491 1.1541 1.1591 1.1641 1.1692

18.81 19.36 19.90 20.44 20.98

68 69 70 71 72

1.3384 1.3447 1.3509 1.3573 1.3636

36.67 37.17 37.66 38.17 38.66

39 40 41 42 43

1.1743 1.1794 1.1846 1.1898 1.1950

21.52 22.06 22.60 23.13 23.66

73 74 75 76 77

1.3700 1.3764 1.3829 1.3894 1.3959

39.16 39.65 40.15 40.64 41.12

8.38 8.94 9.49 10.04 10.59

49 50 51 52 53

1.2273 1.2328 1.2384 1.2439 1.2496

26.86 27.38 27.91 28.43 28.96

83 84 85 86 87

1.4359 1.4427 1.4495 1.4564 1.4633

44.02 44.49 44.96 45.44 45.91

1.0833 1.0878 1.0923 1.0968 1.1014

11.15 11.70 12.25 12.80 13.35

54 55 56 57 58

1.2552 1.2609 1.2667 1.2724 1.2782

29.48 30.00 30.53 31.05 31.56

88 89 90 91 92

1.4702 1.4772 1.4842 1.4913 1.4984

46.37 46.84 47.31 47.77 48.23

25 26 27 28 29

1.1060 1.1107 1.1154 1.1201 1.1248

13.90 14.45 15.00 15.54 16.19

59 60 61 62 63

1.2841 1.2900 1.2959 1.3019 1.3079

32.08 32.60 33.1 1 33.63 34.13

93 94 95 96 97

1.5055 1.5126 1.5198 1.5270 1.5343

48.69 49.14 49.59 50.04 59.49

30 31 32 33

1.1296 1.1345 1.1393 1.1442

16.63 17.19 17.73 18.28

64 65 66 67

1.3139 1.3200 1.3261 1.3323

34.64 35.15 35.66 36.16

98 99 100

1.5416 1.5489 1.5563

50.94 51.39 51.93

.

The above table is from the determ~nationsof Dr . F. Plato. and has been adopted as standard by the United States Bureau of Standards.

From Circular No. 59 Bureau of Standards .

INGERSOLLi3AND CAMERON HYDRAULIC DATA

PROPERTIES OF LIQUIDS Specific Gravity of Hydrocarbons

Specific Gravity and Temperature Relations of Petroleum (Approximate)

Specific Gravity-Referred to water at 60°F. Example: oil with sp. gr. of 0.82 at 60°F will have sp. gr. of 0.64 at 500°F. Drawn by IngersoU Rand based on data from Gas Processors & Supphera Assn.

Courtesy of Hydraulic Institute.

A.

PROPERTIES OF LIQUIDS Specific Gravity at 60°F of Aqueous Solutions

""0

I0

20

30

50 60 % by WEIGHT

40

b a w n by Ingersoll-Rand based on data from various chemical handbooks. Drawn by Ingersoll-Rand based on data from various chemical handbooks.

4-16

70

80

90

100

INGERSOLLRAND



Vapor Pressure of Gasolines

Specific Gravity of Refrigerant Liquids I

40

m

m

r

s

a

n

I

a f m

~m

la

IU

lm

rn

"G

Courtesy Ch~cagoBridge & Iron Company To determine the gage working presaure of a vessel to store any natural gasoline: 1. Determine the maximum liquid surface temperature reached or likely to be reached by the liquid during the period of storage. 2. The vertical temperature line interseeta the Reid vapor pressure line for the liquid being considered at a definite point. 3. from the m e determine the initial vapor pressure in pounds absolute at the IeR hand side horizontally from the intersection mentioned in "2." 4. From the initial vapor pressure in pounds absolute subtract 14.7. The result is the gage working pressure of the vessel required to store that Liquid, without evaporation loas. Drawn by Ingersoll-Rand based on data from various refrigerant handbooks.

4-18



Vapor Pressure of Various Liquids

Vapor Pressure of Hydrocarbons TEMPERATURE CELSIUS C '

0

50

100 150 TEMPERATURE OF

200

250 300

400

500

Drawn b) Ingersoll-Rand baqed on data from ranous sources

Drawn by Ingemoll-Rand based on data from various sources

4-20

A

INGERSOLLflAND



Vapor Pressure of Refrigerant Liquids

Viscosity-General

Information

The viscosity of a fluid (liquid or gas) is that property which offers resistance to flow due to the existence of internal friction within the fluid. This resistance to flow, expressed as a coefficient of dynamic (or absolute) viscosity is the force required to move a unit area a unit distance. There are two basic viscosity parameters; i.e. (1) dynamic (or absolute) viscosity; and (2) kinematic viscosity. These two parameters are related since the kinematic viscosity may be obtained by dividing the dynamic viscosity by the mass density. (See note on page 4-3 for definition of mass density.) (1) The unit of dynamic (or absolute) viscosity in the English system is measured in pound seconds per square foot which is numerically identical with the slug per foot second. The unit of dynamic viscosity in metric measure is the dyne-second per square centimeter called the poise, which is numerically identical with the gram per centimeter-second. I t is usually more convenient to express numerical values in centipoises such that 100 centipoises equal one poise. The dimensions of dynamic (or absolute) viscosity are: force

time length2

(2) Since the Darcy-Weisbach and Colebrook relationships (see page 3-3) are based on using a Reynolds number which varies inversely with the kinematic viscosity and which is obtained by dividing the dynamic (absolute) viscosity by the mass density, it is usual practice to use units of kinematic viscosity which have the dimensions of length2 time

-

VAPOR

PRESSURE PSlA

D r a u n b j Ingenoll-Rand b a r d urr data from b a n u u a refngrrant handbooks

4-22

The unit of kinematic viscosity in English measure is the square foot per second. The unit of kinematic viscosity in metric measure is the square centimeter per second called the stoke. I t is usually more convenient to express numerical values in centistokes such that 100 centistokes equal one stoke.

INGERSOLLflAND



When English system units are used in converting from dynamic W

to kinematic viscosity the density C7 (or mass density), rather than 6

the specific gravity must be used where w is the weight in lb/ft3 and g is the acceleration of gravity (32.174 ft/sec2). When the metric system terms centipoises and centistokes are used the density is numerically equal to the specific gravity. The relationship between the dynamic and kinematic viscosity units with their proper dimensions must be carefully considered so that the correct parameters will be used as required in friction loss and other calculations. Various types of instruments are available to determine viscosity, the one most widely used being the Saybolt viscometer which measures the time in seconds required for a liquid to flow from a filled container of specified dimensions through one of two orifices in the bottom of the container. The term SSU (Seconds Saybolt Universal) refers to the time required for the smaller of the two orifices, and the term SSF (Seconds Saybolt Furol) the time required for the larger orifice. The smaller orifice (SSU) being used for the lighter oils and the larger orifice (SSF) for the heavy oils. The efflux time in seconds is converted empirically to kinematic viscosity in other units. The various viscosity relationships and conversions are given on the following pages.

Approximate Viscosity Conversions

INGERSOLLRAND


PROPERTIES OF LIQUIDS Viscosity-Unit

Approximate Viscosity Conversions (Continued) Seconds Saybolt Un~versal SSU

K ~ n e r n a t ~v~scoslty c centlstokes

ft2sec

Seconds Redwood 1 Stand ard

Seconds Saybolt Furol SSF

Seconds Red wood 2 Ad rnlralty

Kinematic Viscosity Degrees Engler

Degrees Barbey

K~ne rnattc cent, stokes

115 96 8 21 718 6 39

5394 647 3 755 2 8631 970 9

See previous page for conversions in SSU, Redwood, etc.

146 175 204 234 263

5 75 4 78 4 11 3 59 319

1078 8 1294 6 1510 3 1726 1 19419

Absolute or Dynamic Viscosity

292 438 584

2 87 1 92 144

2157 6 3236 5 43153

0 002788 0003254 0003717 0004182 0 004647

122 143 163 183 204

1016 1185 1354 1524 1693

111 129 148 166 185

35 1 409 467 526 584

2500 3000 3500 4000 4500

539 4 647 3 755 2 863 1 970 9

0 005806 0 006967 0008129 0 009290 0 01045

254 305 356 408 458

2115 2538 2961 3385 3607

23 1 277 323 369 41 5

730 87 6 102 117 131

5000 6000 7000 8000 9000

10788 1294 6 15103 1726 1 1941 9

001161 001626 001858 002092

509 610 71 2 814 916

4230 5077 5922 6769 761 5

461 553 646 738 830

10000 15000 20000

21576 3236 5 4315 3

002322 0 03483 004645

1018 1526 2035

8461 12692 16923

922

Viscosity relationships =

to o b t a ~ n

by I

ftY!sec ft2!sec sq metersisec sq metersisec centistokes centistokes

259 0 302 3 3453 3885 431 7

259 0 302 3 345 3 388 5 431 7

Kinematic viscosity (centistokes)

Multiply

I

23 9 20 5 180 156 14 4

1200 1400 1600 1800 2000

0 01393

Conversions

I

I

Ibf-sec/ft2 Ibf-sec!ftZ centipoises centipoises centipoises Pascal-sec Pascal-sec I

I

absolute viscosity (centipoises) density (g/crn3)'

centistokes sq rnetersisec ftZ/sec centistokes sq metersisec ft?/sec . ---

centipoises Pascal-sec kg-secisq meter Ibf-seclsq ft' Pascal-sec Ibf-secisq ft centi~oises

' Sometimes absolute viscosity is given in terms of pounds mass. In this casecentipoises x 0.000672 = Ibrnlft sec.

ft2/sec = centistokes x 1.07639 x 10-j Absolute to Kinematic Viscosity

centistokes = ft2!sec x 92903.4 Approximate viscosity conversions ft2!sec (50-100 SSU) ft2/sec (100-350 SSU) ft2!sec (over 350 SSU) centistokes (50-100 SSU) centistokes (100-350 SSU) centistokes (over 350 SSU) centistokes (over 350 SSU) centistokes (over 500 SSF) centistokes (over 300 Redwood #1) centistokes (over 50 Redwood #2) centistokes (over 18 Engler) centistokes (over 20 Storrner) centistokes (over 1.0 Demler # l o ) centistokes (over 1.3 Demler #1) centistokes (over 14 Parlin #20) centistokes (over 230 Ford #4) centistokes ' Usually same as specific gravity

- .00210!SSU SSU x 2.433 x SSU x 2.368 x lo-" .00145/SSU = SSU (taken at 100°F) x 2.3210 x = SSU x 0.226 - 205.3lSSU = SSU x 0.220 147.7iSSU = SSU (taken at 100°F or 37.8%) x 0.21576 = SSU (taken at 210°F or 98.9%) x 0.21426 = SSF (taken at 122°F or 50°C) x 2.120 = Redwood #1 (Standard) x 0.255 = Redwood #2 (Admiralty) x 2.3392 = Engler x 7.389 = Stormer x 2.802 = Demler # I 0 x 31.506 = Demler #1 x 3.151 = Parlin Cup #20 x 61.652 = Ford Cup #4 x 3.753 = 6200 Barbey

= =

centipoises centipoises Ibf-sec/ft2 kg-sec!rn2 Pascal-sec

lldensity (gicm3) 0.00067197/density (Ib/ftJ) 32.174ldensity (IbIftR) 9.80665idensity (kg/rn3) 1000/density (g!crn3)

centistokes ftZ/sec ft2/sec sq rnetersisec centistokes

-

Kinematic to Absolute Viscosity sq meterslsec ft2!sec ftZ/sec centistokes sq meters!sec

0.10197 x density (kg/m3) 0.03108 x density (Ib!ft3) 1488.16 x density (Iblft") 0.001 x density (g/cm3)

centipoises kg-secisq meter Ibf-sec/ft2 centipoises Pascal-sec Pascal-sec


INGERSOLLRAND CAMERON HYDRAULIC DATA Viscosity-Temperature

Viscosity of Fuel Oils

Relations of Petroleum Oils

VISCOSITY SSU 0

Y) C)

N "7

0 a V) L w

" n

3;

""a" 0 0 0 0 0 3

N

-

0 0

w -

ooni

KINEMATIC VISCOSITY.

Drawn by Ingersoll-Rand based on data from Texaco, Inc

4-30

CENTISTOKES

a

3

T

" VISCOSITY

This chart may be used to determine the viscosity of an oil a t any temperature prov~dedits viscosity a t two is known. The lines on this chart show \.~srositlesof representatit? oils. Note: This chart is slrmiar to ASTM tentative standard D341-32T vhlch has a somewhat u i d e r viscosity and range. Courtesy of Texaco. Inc.

INGERSOLLRAND



Viscosity of Refrigerant Liquids

Viscosity of Miscellaneous Liquids

TEMPERATURE CELSIUS -30

-20

-10

0

I0

20

"C 30

40

TEMPERATURE, DEGREES FAHRENHEIT

Drawn by lngrrsollbRand based

oara from ianoue refrigerant nandboilhs.

50

60

70

INGERSOLLRAND



Viscosity of Sucrose Solutions

Viscosity Blending Chart Many liquids designated by such names as asphalt, molasses, oil, varnish, etc., are actually blends or cut-backs and have lower viscosities than the unblended liquids of the same name. On Fig below, let oil, A, have the higher viscosity and oil, B, the lower viscosity. Mark the viscosity of A and B on the right and left hand scales, respectively, and draw a straight line connecting the two as shown. The viscosity of any blend of A and B will be shown by the intersection of the vertical line representing the percentage composition and the line thus drawn. Viscosities of oils A & B must be plotted a t the same temperature.

OIL B 100

90

80

70

60

40

30

PERCENTAGE OF COMPONENT OILS

Draun by Ingeraoll-Hand b a e d an data frum various sugar handbooks.

comes^ of Hydraulic lnstltute

20

10

0



Specific Gravity and Viscosity of Liquids

Petroleum Temperature-volume Relations

Liqu~d Acetaldehyde CH,CHO

Boiling point at atm press

"F

'C

69F 208C

61 68

16 1 20

0788 0 762

59

15

1.W6

Acetlc acld-5% = vlnegar CH,COOH

Speclfic gravlty Temp

based on water = 1 at 60'F

Vlscoslly Temp

. 'F

'C

61 68

16 1 20

centlstokes

SSU

0305 0 295

36

2.85

35

1.34

31 7

10% 50%

. . . . .

80%. .

59

Conc.-glacial 118C Acetlc a c ~ danhydr~de

0 88 Acetone CH,COCH, Alcohol ally1 .

. . . ..

butyl-n

. . . . . .

methyl (wood) CH,OH . .

.

133F 50 5C

68

20

0 792

68 77

20 25

0 41

207F 97.2C

68

20

0.855

68 104

20 40

1.60 0.90 cp

31 8

68 158

20 70

0.81 0.78

68 158

20 70

3.64 1.17

38 31 5

68

20

0 79

59 32

15 0

0 74 1.04

60

156

10-

77 100

25 378

215-1510 75-367

1M-7M 350-1700

60

156

10-

77 100

25 378

33-216 19-75

155-1000 90-350

243F 117C

151F 64.7C

PERCENT INCREASE IN VOLUME ABOVE 60 F. Asphalt emuls~ons Fed # 1

Fed #2

Courtesy of Hydraulic Institute.

4-36

v

VI

Based o n materai from the Hydraulic lnstlture with a d d ~ t ~ o nby s ~ngerso~l- and



Specific Gravity and Viscosity of Liquids (Continued)

Specific Gravity and Viscosity of Liquids (Continued) -

L~qu~d

Carbon tetrachlor~de CCI,

SAE lOW

Carbon dlsulphide CS

SAE 20W

Castor oil

Bo~lng point at atm press

S p e c t t c gravlty Temp F

VISCOSlly Temp

based o n watet - 1 at 60'F

C

F

C 20 376

0 612 0 53

0 20

0 33 0 298

170F 76 7C

68

20

1 594

68 100

115F 46 2C

32 68

0 20

1293 1 263

32 68

68 104

20 40

0 96 0 95

100 130

378 54 4

centistokes

259-325 98-130

SAE 20

SSU

1200-1500 450-600

SAE 30 SAE 40

Automot~vegear 011s SAE 75W

Il

SAE 80W SAE 85W SAE 90 24 Baume

SAE I 4 0

40" API

35 6 API 32 6 API Salt Creek Decane-n

60 130 343F 173C

D~ethyleneglycol

156 544

0843 082

60 130

156 54 4

68

20

0 73

0 100

1 7 8 378

60

156

112

70

211

60

15 6

82- 95

122 160

50 711

77 61 2 36 1 001 32

45 6 34 31 1497

25-0 Carbol~ca c ~ d(phenol)

360F 182 2C

65

18 3

1 08

65 194

183 90

1183 126cp

65

5D Ethyl acetate CH,COOC,H, Dowtherm

494 3'

25'12

1

8%" 1 056

1

;

8 6 6 rnax 352max

1 8" 1

400 max 165max

INGERSOLLRAND



-


Liquid Ethyl bromide C H Br

S p e c ~ f i cgravty Bo~l~ng pont based Temp at o n water atm F - 1 at 60 F C press


V~scos~ty Temp F

C

cent~stokes

lOlF 77 2C

59

15

1 45

68

20

0 27

Ethylene bromlde

269F 131 7C

68

20

2 18

68

20

0 787

Ethylene c h l o r ~ d e

183F 837C

68

20

1 246

68

20

0 668

60

156

1125

70

211

80"o

68

20

1 186

68

Conc

60

156

1221

68 77

Freon -11

70

21 1

149

-12

70

21 1

133

- 21

70

21 1

68

SSU

SSU at 100°F 178

88 4

20

14

31 7

20 25

1 48 157cp

31 7

70

21 1

0 21

70

21 1

0 27

137

70

21 1

145

31 7

20

1159

68 77

20 25

145 149cp

31 7

60

156

82- 95

70 100

21 1 378

2 3 9 - 4 28 -2 69

34-40 32-35

2

60

156

82- 95

70 100

21 1 37 8

3 0-74 2 11-4 28

36-50 33-40

6

60

156

82- 95

122 160

50 71 1

97 4-660 37 5-172

450-3M 175-780

60

156

089

211 37 8

139 74

Ethylene glycol

Furfurol Fuel 011s 1

Gas 011s

161 7C

70 100

Glycer~ne 1oooo 50'0 water Glucose

--

113

5 29

73 50

Lard

60

156

096

100 130

378 544

621 343

Lard 011

60

156

91-93

109 130

378 544

41-475 234-271

190-220 112 128

60

156

92-94

100 130

378 544

305 1894

143 93

60

156

1357

70 100

211 378

Linseed

011

Heptane-n Mercury

6751F 356 9C

0 118 0 11

287 160


INGERSOLLRAND



A flrst

B second

NltroDenzene

68

20

0 99

32 68

0 20

Propylene glycol

68

20

1 038

70

21 1

Quenching 311 (~YPIC~I

60

156

86- 89

P r o p ~ o n cac d

286F

1 52cp 113

52

100-120


31 5

24 1

20 5 - 2 5





fresh

74 B r x

76 B r x

Centrifugal pump performance with viscous liquids Since pump performance characteristic curves are basis water, corrections (per charts in *Fig 4-2 and 4-3) must be applied when handling viscous liquids. The following two examples will illustrate the use of these charts. Example A-performance RT-2

Given: Characteristic curve (Fig 4-1) page 4-46 for pump handling water a t normal temperature (see page 4-46,4-47 and 4-48).

RT-4

Problem : Determine the approximate performance curve for oil having a specific gravity of 0.90 and viscosity of 1000 SSU (216 centistokes).

RT-6

1

RT-8

RT-10

Toluene

1231F 1106C

Trlelhylene glycol Turpent~ne

Varn~sh spar

correction:

320F

E?

0866

1 125

60

156

86- 87

60

156

09

4168 0 38cp

21 1

185 7

100 130

37 8 54 4

866-95 2 39 9 - 4 4 3

100

20 378

313 143

400-440 185-205 1425 650

From water curve in Fig 4-1 note that capacity at best efficiency point (1.0 x Q,) is 750 gpm. Tabulate gpm for 0.6 x Q,, 0.8 x Q,, 1.0 x Q, and 1.20 x Q, for water as in table following Fig 4-1; read heads and efficiencies from the water curve a t these values of gpm and tabulate as shown. Entering the chart (Fig 4-3) at 750 gpm go vertically to the head in feet (100') and horizontally to 1000 SSU and vertically to the correction factors, reading one value for C g and C, and four values for C, and tabulate as shown. Multiplying the tabulated water values by these factors will give the corrected values for operation with the viscous liquid. Corrected head and efficiency curves may be plotted using these points; approximate brake horsepower and curve *NOTE: Figures 4-1 to 4-3 appear on pages 4-46 to 4-48.

INGERSOLLRAND CAMERON HYDRAULIC DATA can be determined by use of the formula:

PROPERTIES OF LIQUIDS Viscosity Corrections for Small Pumps (Continued) Between 10 to 100 GPM

capacity (viscous) x head (viscous) sp gr Estimated bhp (viscous) = 3960 x Efficiency (viscous)

CAPACITY-GPM

Fig. 4-1 Sample performance chart

Courtesy of Hydraulic I n s t ~ t u t r .

Sample Calculations

Fig. 4-2 Performance correction chart. (Correction factors apply to Best Efficiency Point only) of Hydraulic Institute.

INGERSOLLRAND


CAMERON HYDRAULIC DATA Example B -selecting

Viscosity Corrections for Large Pumps (Continued) Above 100 GPM

a pump:

Selecting a pump for viscous liquids is the reverse of correcting for water performance; i.e. take the desired design conditions and divide by the applicable correction factors to obtain the equivalent design conditions on water. For example: select a pump to deliver 750 gprn at 100 ft when handling a liquid having a viscosity of 1000 SSU and specific gravity of 0.90 a t pumping temperature. Enter chart a t 750 gpm and follow the same procedure as in Example A except for this calculation use C, from curve marked 1.0 x Q, (capacity a t best efficiency point-bep) Equivalent water conditions obtained by dividing the viscous conditions by the above correction factors will be 790 gpm and 108.7 ft. If the pump selected for these equivalent water conditions has a water efficiency of 81% the viscous efficiency will be 0.64 x 0.81 or about 52%. Estimated bhp

=

750 x 100 x 0.90 3960 x 0.52

=

32.8

Note: Correction charts are approximate and apply only to Centrifugal pumps of conventional design with open or closed impellers and adequate suction head to force liquid into impeIler; not good for axial or mixed flow pumps or non-uniform liquids. Correction factors for flows 100 gprn and below (Fig. 4-2) are basis (bep). For a more detailed discussion of these correction factors reference should be made to the Hydraulic Institute Standards.

Pump performance on stock (for friction loss see page 3-88)

r

Fig. 4-3 Performance correction chart Courtesy of Hydraulic Institute.

Since pump performance curves are based on tests with water a t normal temperatures (60°F to 70"F), there will be a reduction in head, capacity and efficiency when handling stock, and corrections (depending on consistency) must be applied to the water performance. These corrections (applied to the head and capacity at the best efficiency point (bep) will be approximately 0.725 for 6% stock; 0.825 for 5.5%; 0.90 for 5.0%; 0.94 for 4.5%; 0.98 for 4.0%; and 1.0 for 3.5% and less. The brake horsepower (bhp) of a pump delivering stock a t the corrected head and capacity will be approximately the same as if it were delivering water at the bep. Therefore, the approximate efficiency of the pump on stock can be det,ermined by calculating its hydraulic horsepower at the corrected head and capacity and dividing by the bhp. Pumps handling stock with entrained air must be given special consideration (consult with manufacturer).



Sediment Terminology -.

Slurry Information The abrasive nature of some slurries is clearly a consideration in selecting and designing slurry pumps. Excessive wear of wetted pump parts due to abrasion has limited operational life in some instances to two weeks. Abrasive wear is inconclusive and difficult to predict even though many studies on wear testers have been performed. Abrasive considerations are the abrading mineral itself, abrasive hardness, particle velocity, density, directions, sharpness, shape, size and corrosiveness.

Scale of Particle Sizes

Tyler screen mesh per inch

U.S. standard mesh per inch

Inches

Microns

Very Coarse Gravel Coarse Gravel Medium Gravel Fine Gravel Very Fine Gravel Very Coarse Sand Coarse Sand Medium Sand Fine Sand Very Fine Sand Coarse Silt Medium Silt ~ i n silt e Very Fine Silt Coarse Clay Medium Clay Fine Clay

Pump components exposed to abrasion, i.e. impellers, casings and suction covers, are made from abrasion resistant materials such as Ni-hard and rubber. Experience has shown that for abrasive handling pumps, the pump RPM should be kept as low as possible. A guideline in showing the effect of RPM on wear is the relation that wear will vary approximately as the cube of the RPM-wear CY RPM3. Hence since RPM is related to pump developed pressure, high head applications will wear much more rapidly than lower heads. Also, it can generally be seen that pump part hardness is inversely proportional to abrasive wear-wear a l/BHN;* and wear also varies directly with particle concentration- wear a C , . Both synthetic and natural rubbers are used in slurry pumps for their superior abrasion and corrosion resistance. Their abrasion resistance exceeds Ni-hard or other metals when the particles are small and round. Sharp and hard solids with high energy are unsuitable for rubber application because they can cut the rubber material. The dampening effect of rubber is low for impact angles greater than 20". Also, rubber is generally unsuitable for applications with heads over 150' and where particle size exceeds ?4 inch. Wear resistant metals such as Ni-hard are used on more coarse and harder slurries. MetalIRubber Slurry Pump Selection Criteria

Use Metal-lined Plc~np: Solids greater than '/4 in. PH greater than 4.5 Abrasive service above 100 f t head Temperatures to 250°F Hydrocarbon based slurries * Bnnell hardness number 4-50

Use Rxbber-lined P ~ o ~ t p : Solids less than ?4 in. PH less than 6.0 Abrasive service below 100 ft head Non-abrasive service below 100 ftlsec-impeller peripheral speed Temperatures below 150°F

Class

Mohs Scale of Hardness, Modified (Trans. Am. Electrochem Society, 1933) Mineral or Mater~al Talc Gypsum, Kaolin Clay, Anthracite Calc Spar, Gray Cast Iron Fluor Spar Apatite Orthoclase or Periclase Vitreous Pure Silica Quartz, Stellite Topaz Garnet Fused Zirconia, Tantalum Carbide Fused Alumina, Tungsten Carbide Silicon Carbide Boron Carbide Diamond

Mohs Hardness 1 2 3 4 5

Soft to Medium

6 7 8 9 10 11 12 13 14 15

Medium to Hard

Hard to Very Hard

Hardness of Common Minerals Soft

Medium

Hard

Very Hard

Asbestos Rock Gypsum Rock Slate Talc Soft Limestone

Limestone Dolomite Sandstone Coal

Granite Quartzite Iron Ore Trap Rock Gravel

Iron Ore (taconite) Granite Granite Gravel

PROPERTIES OF LIQUIDS SIurry rheology, viscosity Terms: Rheology-study of deformation and flow of substances. Fluid-a substance which undergoes continuous deformation when subjected to shear stress. Consistency (apparent viscosity)-a slurry's resistance to deformation when subjected to shear stress. This term is applied to differentiate from absolute viscosity which is used in conjunction with Newtonian fluids. Kinematic viscosity-absolute viscosity (consistency) divided by the mass density* of the fluid. Fluidity -inverse of viscosity. Plasticity-property of a fluid which requires a definite yield stress to produce a continuous flow. Rigidity-consistency of a plastic fluid in terms of stress beyond the yield. Newtonian fluid-a fluid whose viscosity is constant and is independent of shear rate, and where shear rate is linearly proportional to shear stress. (water, oil, etc). Non-Newtonian (complex) fluid-a fluid whose consistency is a function of shear stress, and the shear rate-shear stress relationship is non-linear. For either Newtonian or Non-Newtonian fluids, viscosity (or consistency is the rate of shear (flow) per unit shearing stress (force causing flow). T = p dvldy Tangential Shearing Stress (force) Viscosity (consistency) dvldy = Shear rate (velocity gradient) T =

=

Types of Non-Newtonian fluids: Bingham-plastic fluids-a fluid where no flow occurs until a definite yield point is reached. This yield stress is necessary to overcome static friction of the fluid particles. Most slurry mixtures used in pipeline transportation exhibit Bingham plastic characteristics. Pseudo-plastic fluids-substances with no definite yield stress which exhibit a decrease in consistency with increasing shear rate. Dilatant (inverted plastic) fluids-a fluid which exhibits an increase *

mass density

=

weight

-

acceleration of gravity

a

in consistency with increasing shear rate. These fluids h ve the property of increasing their volume when stirred. Examples are starch in water, quicksands and beach sands. Thixotropic fluids-a fluid which exhibits a decrease in consistency with time to a minimum value a t any shear rate. I t will break down when stirred but rebuild itself after a given time. Examples are drilling muds, gypsum in water, paint. Typical flow diagrams (rheogram) for various fluids:

NOTE: Shear stress is proportional to pressure or total head; shear rate is proportional to velocity or flow. Useful formulas for solids and slurries: S, = Specific gravity of liquid S, = Specific gravity of solids S, = Specific gravity of slurry mixture C, = Percent solid concentration by volume C, = Percent solid concentration by weight

INGERSOLL-RAND



As a very approximate guide for slurries with particle sizes under 50 microns, a minimum velocity in the range of 4 to 7 ft. per second second is required, provided this velocity gives turbulent conditions. For larger particle size slurries (over 150 microns) and volume concentrations up to 15 percent, a rough guide for minimum velocity is 14 times the square root of pipe diameter (ft.), (Durand's equation). There is no general method or formula to determine the critical velocity of all slurry combinations, therefore, if a precise critical velocity is required, results should be obtained by experimentation.

Slurry Head Correction-Pipe Friction Loss For a given solid throughput and pipe diameter, the lowest pressure loss is obtained at the transition between laminar and turbulent flow. Although this minimum pressure loss is also the most economical running point (power per pound of solids), the operating velocity must be kept above this critical carrying velocity.

Percentage by Volume or by Weight C, or C,

From Centrifugal Pumps by A. J . Stepanoff uith permission of John Wiley & Sons.

Critical Carrying Velocity of Slurries in Pipes

As with critical carrying velocities, many extensive studies have been done with pressure gradients of solid mixtures. Again, a general purpose formula for all slurries is impractical to predict. However, certain guidelines can be followed.

As a slurry is conveyed by turbulent flow in a pipe, particles have a tendency to settle. The critical velocity of a slurry flow in a pipe is that velocity below which particles start forming a sliding bed on the bottom of the pipe which will cause the flow to become unstable and the pipe will eventually clog. General slurry pipeline practice is to design the pipe velocity to exceed the critical velocity by a t least 30 percent.

When the slurry contains particles under 150 microns and the concentration of these particles is low, and the fluid velocity is high enough to ensure uniform particle distribution in the pipe-under these circumstances, the slurry behaves as a "Newtonian liquid and

This velocity will depend upon pipe diameter, solids concentration and the properties of the fluid and solid particles. Extended studies have been done on critical speeds of slurry mixtures. One typical study done by Durand with sand-water suspensions gives the relationship: V, = F,[SgD(S, -

Critical Carrying

Where D = inside pipe diameter-ft S, = specific gravity of solids V, = critical carrying velocity-ftlsec g = acceleration of gravity-ftlsec2 F,= an experimental coefficient dependent upon grain size and concentration and approximate equals 1.34 above .05 in. particle size. NOTE: That this coefficient is for sand-water mixtures to 15 percent concentration by weight. In general slurry pipeline practice, to prevent settlement in the pipeline, hydraulic conditions should ensure turbulent flow.

Pressure Loss

Velocity

I

* For Newton~anLiquid definition eee page 1-5

t h e pressure loss is t h e same a s the water friction loss which can be calculated from the friction loss charts in a previous section. (Pages 3-3 to 3-48) Friction loss is also dependent on pipe roughness. In slurry pipeline design, a rough pipe design will yield a higher pressure loss capability. Using a "C"* factor pipe of 100 will result in a pressure loss capability about 100% greater than design with a clean-steel pipe, however "C"* values of 140 are not uncommon with certain types of slurries. Although slurry-pipe friction can be higher than water or Newtonian fluids, many slurries have negligible head correction and can be treated with a correction very nearly the same as clear water. Avoid large corrections, unless tested, since overcapacity can cause pump problems. In calculating and/or estimating pipe friction losses for slurries, it has been common practice, for many years, to use the Hazen and Williams empirical formula discussed on pages 3-7 and 3-8. This formula is convenient to use and experience has shown, that with t h e selection of the proper friction factor "C" will produce reliable results. Both t h e Darcy a n d Hazen-Williams formulas can be used for slurry pumping with appropriate experience correction factors. The Hazen-Williams formula is more convenient in that "C" values can be associated with given slurries and extrapolated from the friction factor tables, using corrections for various "C" factors shown on page 3-8. With reference to pump performance, most slurries have little affect on performance except for density; allowance, however, should be made for pump wear to maintain plant production.

* Friction

4-56

factor in Hazen and Williams formula. "C" of 140 is for new steel pipe.

SECTION V

STEAM DATA

5- 1

INGERSOLLRAND


q$

STEAM DATA

2.2

Steam Data Notes


Steam Data Page Notes on Steam . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 5-3 Enthalpy and Entropy-Definition . . . . . . . . . . . . . . . . . . . . . 5-4 Mollier Diagram . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 5-5 Pressure-enthalpy chart . . . . . . . . . . . . . . . . . . . . . . . . . . . . 5-6 Steam Tables: Temperature Data (to 705.47"F) . . . . . . . . . . . . . . . . . . . . . . . . . . . 5-7 Pressure Data (in Hg Abs) . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .5-14 Pressure Data (mm Hg Abs) . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 5-17 Pressure Data (to 3208.2 psia) . . . . . . . . . . . . . . . . . . . . . . . . . . . . 5-19 Superheated Steam Data . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .5-21 Theoretical Steam Rates for Steam Turbines . . . . . . . . . . . . . . . . . 5-25 Approximate Turbine Efficiencies . . . . . . . . . . . . . . . . . . . . . . . . . . . 5-30 Vapor Flow Formulas . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .5-32 Pressure Drop in Steam Piping . . . . . . . . . . . . . . . . . . . . . . . . . . . . .5-34 Low Pressure Steam Flow . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .5-38 Pressure Drop in Steam Fittings . . . . . . . . . . . . . . . . . . . . . . . . . . . .5-39 Psychometric Chart. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .5-40 Boiler Feed Flow Data . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .3-42 .

1

I

Steam is the term usually applied to the vapor-phase of water when this phase is reached by boiling water. The term vapor describes the gaseous state of any substance, below its critical condition, from which it can be reduced to a liquid by compression. But water vapor is usually thought of only in a mixture with air, while the word steam has a much broader meaning. In a certain range of (low) pressures, the terms steam and water vapor are used interchangeably. "Boiling point" is the temperature at which a liquid boils-that is, changes rapidly and violently into vapor, (or steam, if the liquid is water), through the application of heat. When the pressure exerted upon the liquid is 760 mm Hg or 14.696 lb per sq in abs., the boiling point of water is 212°F or 100°C. The temperature a t which water boils varies, however, with the pressure; water may actually boil at freezing temperature (32°F) provided the pressure is held down to .0885 lb per sq in; on the other hand its maximum boiling temperature (the critical temperature), is approximately 705"F, under a pressure of some 3200 lb per sq in. Steam, or water vapor, is invisible. Only through partial condensation does it appear as a mist. Steam may exist either in saturated form, while in contact with water, or as superheated steam, after separation from the water from which it was generated and further heating. Saturated steam may be dry or wet; in the latter case it carries free moisture and the amount of moisture determines the "quality" of the steam. The exhaust from a steam turbine or engine is usually wet steam. The temperature of dry-or wet saturated steam a t a given pressure is the same and is determined entirely by the absolute pressure. If the pressure is maintained, the temperature will remain constant as condensation proceeds. Removal of heat produces condensation. Superheated steam behaves like a gas; when compressed, its temperature rises; when heated at constant pressure its volume increases, when heated at constant volume its pressure rises, etc. Its condition is usually indicated by the "degrees of superheat" above the saturation temperature, and by its pressure. 1cu ft of water, evaporated at 212°F and 14.696 lb per sq in absolute Pressure, becomes 1606 cu ft of dry-saturated steam.

1 cu ft of steam weighs 0.03731 lb, and 1 lb of steam occupies 26.80 cu ft, at a pressure of 14.696 lb per sq in absolute and a temperature of 212°F. 5- 3

INGERSOLLRAND


1 cu ft of dry air weighs 0.08073 lb, and 1 lb of dry air occupies 12.387 cu ft a t pressure of 14.696 lb per sq in absolute and a temperature of 32°F

The amount of heat required to transform a liquid into its vapor, the temperature remaining constant, is called the latent heat of vaporization. The value of the latent heat varies with the pressure under which the liquid is caused to vaporize. The latent heat of vaporization of water to steam is 970.3 Btu per lb at atmospheric pressure. The Btu (British thermal unit) is equivalent to 778.0 ft-lb, which is the heat energy required to raise the temperature of 1 lb of water 1°F in the range from 32 to 212°F. In the metric system use is made of the term calorie (cal) or gram-calorie which is the heat required to raise the temperature of 1 gram of water 1°C within the range 0 to 100°C. The lulogram-calorie or large calorie is 1000 gramcalories. In modern practice the Joule is used as a measure of energy. I t is equivalent to 0.7376 ft-lb. The output of a steam generating plant is often expressed in pounds of steam delivered per hour. Since the steam output may vary in temperature and pressure, the boiler capacity is more completely expressed as the heat transferred in Btu per hour. Boiler capacity is usually expressed as kilo Btu (kB)/hour which is 1000 Btu/hour, or mega Btu (mB)ihour which is 1,000,000 Btulhour. An older expression of boiler capacity is boiler horsepower. It is equivalent to 34.5 lb of water evaporated per hr a t standard atmospheric pressure and 212°F. It is equivalent to 33,475 Btulhr. *ENTHALPY-(Heat Content) is the sum of the internal and external energies of a substance. *ENTROPY-is a measure of the unavailability of energy in a substance. *For more details reference to MARKS Handbook is suggested.

8;

STEAM DATA Mollier Diagram for Steam

INGERSOLLUAND

STEAM DATA


Pressure-enthalpy Chart for Steam

Properties of Saturated Steam-Temperature

Table

I Vacuum

Btullb

Absolute Pressure

75 76 77 78 79

0875 0 904 0935 0 966 0 999

22 22 23 24 25

22 97 75 54 37

0 42964 0 44420 045919 047461 0 49049

29 29 28 28 28

047 017 986 955 923

740 3 7174 695 2 673 9 653 2

43 44 45 46 47

045 043 042 040 038

1051 2 1050 7 1050 1 1049 5 1049 0

1094 3 10947 1095 1 1095 6 1096 0

Tables on pages 5-7 to 5-10 reproduced by permlsslon from ASME Steam Tables' 1967 by Amer~can Soclety of Mechanical EnL~neersAll rlghls reserved Hg and vacuum In ~nchesHg calculated by Ingersoll-Rand Absolute pressures In ~nchesHg rn~ll~meters

Courtesy of B a k k Wilmx.

5-6

INGERSOLLRAND CAMERON HYDRAULIC DATA Properties of Saturated Steam-Temperature

A b s o l u t e Pressure Temp

F

~nHg

m m Hg

Ib/ln2

Vacuum i n Hg ref t o 29.921 ~n b a r , at

32F

Table (cont.)

STEAM DATA Properties of Saturated Steam -Temperature

Table (cont.)

Total heat o r e n t h a l p y Spec~f~c Btuilb volume sat v a p steam water evap ft3/lbm

v,

h,

ha

h,

Tables on pages 5-7 to 5-10 reproduced by permlsslon from ASME Steam TablesG 1967 by Amer~can Soc~etyof Mechan~calEng~neersAll r ~ g h t sresewed Absolute pressures In lnches Hg, m~ll~meters Hg, and vacuum In lnches Hg calculated by Ingersoll-Rand

Tables on pages 5-7 to 5-10 reproduced by permlsslon from ASME Steam Tables' 1967 by Amer~can

Society of Mechan~calEng~neersAll r~ghtsreserved Absolute pressures In lnches Hg mllllmeters Hg and vacuum In lnches Hg calculated by Ingersoll-Rand

INGERSOLLRAND



STEAM DATA

Table (cont.) Properties of Saturated Steam-Temperature

Vacuum I n Hg ref to Absolute Pressure Temp F

~n Hg

mrn Hg

Ib/ln2

29.921

bar. at 32F

tn

Speclflc volume sat vap ft3/lbm

v,

Table (cont.)

Total heat or enthalpy Btullb water hf

evap hk

steam h,

Tables on pages 5-7 to 5 10 reproduced by permlsslon from ASME Steam Tables' 1967 by Amer~can SOClely 01 Mechanical Engineers All rlghts reserved Absolute pressures In Inches Hg m~lllmetersh g and vacuum in inches Hg calculated by Ingersoll-Rand

Tables o n pages 5-11 to 5-13 reproduced by perrnlsslon from ASME Steam Tables' 1967 by The Amer~can Society of Mechan~calEng~neersAll rlghts reserved

STEAM DATA

INGERSOLLRAND CAMERON HYDRAULIC DATA -


-

Table (cont.)


Table (cont.)

Tables on pages 5-1 1 to 5-13 reproduced by permlsslon from ASME Steam Tables' 1967 hy The Amer~can Socely of Mechanlca Englneers all rlghts reserved Any pressure may be expresqed In a number of d~fferent units by uslng the following formulas 1 standard atmosphere = 14 696 lblsq In absolute 1 slandard atmosphere 29 9213 Inches Hg (at 32 F-0 Ci 1 standard atmosphere - 34 00 it water (at 75 F-23 9 C ) 1 standard atmosphere 76 cm or 760 mm Hg (at 0 C-32 F 1 pound per sauare lnch 2 036 ~nchesHg (a1 32 F-0 C i 1 pound per square nch 27 763 nches water (at 75 F-23 9 C ) 1 ~ n c hHg (at 32 F) 491 pounds per square nch 1 ~ n c hHg 25 4 m ( m e t e r s Hg 1 k q cm 14 223 1b sq In 1 pound per sq In = 6 895 k~lopascals

Tables on pages 5-11 to 5-13 reproduced by permission from ASME Steam Tables S 0 ~ 1 e tof y Mechan~calEnglneers All rlghts reserved

5-12

' 1967 by The Amer~can

conversion

INGERSOLLUAND

Properties of Saturated Steam-Pressure; Absolute pressure ~n H g

Properties of Saturated Steam-Pressure;

In Hg Abs

Temp F

Sp vol cu i t Ib

Absolute pressure ~nH g

Temp F

Sp vol cu f l lb

50 51 52 53 54 55 56 57 58 59

58 80 59 35 59 90 60 43 6096 6148 6200 6249 62 99 63 47

1256 5 1233 6 12109 1189 5 11683 11484 11286 11102 1091 9 1074 6

1 00 1 01 1 02 1 03 1 04 1 05 1 06 1 07 1 08 1 09

79 03 79 33 79 64 79 94 8023 8 0 52 8 0 81 8110 81 39 81 67

652 3 646 4 640 4 634 4 628 7 623 1 617 5 6120 606 7 601 4

60 61 62 63 64 65 66 67 68 69

63 96 64 43 64 90 65 35 65 81 66 26 66 70 67 13 67 56 67 99

1057 3 1041 0 1024 9 1009 7 994 7 980 3 966 3 952 5 939 4 926 3

110 111 112 113 114 115 116 117 1 18 119

81 82 82 82 83 83 83 83 84 84

70 71 72 73 74 75 76 77 78 79

6840 68 82 69 23 69 63 70 03 70 43 70 81 71 20 71 58 7196

9140 901 7 889 9 8784 867 1 856 1 845 5 835 1 825 0 8151

1 20 1 21 1 22 1 23 1 24 1 25 1 26 1 27 1 28 129

84 65 84 91 8517 85 43 85 68 85 93 86 18 86 43 8668 8692

549 3 544 9 5407 536 6 532 5 528 4 524 5 520 6 5167 5129

2039 19768 19179 1863 0 18109 1761 6 17153 1671 1 1629 9 15900

80 81 82 83 84 85 86 87 88 89

72 72 73 73 73 74 74 74 75 75

33 70 06 42 78 13 48 83 17 51

805 6 796 2 786 9 778 0 7692 760 7 752 4 744 1 736 2 728 4

1 30 1 31 1 32 1 33 1 34 1 35 1 36 1 37 1 38 1 39

87 17 87 41 87 65 87 89 88 12 88 3 6 88 59 88 83 8906 89 28

509 2 505 6 502 0 498 4 494 9 491 5 488 1 484 7 4813 478 1

1553 0 15170 14820 1449 9 14185 1388 4 1360 0 1332 3 1306 2 1280 9

90 91 92 93 94 95 96 97 98 99

75 85 76 18 76 51 76 83 7715 77 47 77 79 78 1 1 78 42 78 73

720 7 713 2 705 9 698 7 6917 684 8 678 1 671 4 6650 658 7

1 40 141 142 1 43 1 44 1 45 1 46 1 47 1 48 1 49

89 51 89 74 89 97 9019 9041 90 6 3 90 85 91 07 91 29 91 50

474 9 471 7 468 5 4654 4624 459 4 456 4 453 5 450 6 447 8

Sp vol cu f l Ib

05 06 07 08 09

543 9 03 12 11 14 8 3 17 24

11200 9400 8300 7250 6500

10 11 12 13 14

19 44 21 42 23 25 24 94 26 53

5860 5320 4960 4520 4210

15 16 17 18

28 0 0 2939 3072 31 9 6

3950 3730 3500 3310

1803 19 20 21 22 23 24 25 26 27 28 29

32 00 3328 34 56 35 78 36 96 38 0 9 3 9 18 40 23 41 23 42 22 43 17 44 08

3306 3147 2997 2861 2736 2624 2520 2424 2336 2253 2177 2106

30 31 32 33 34 35 36 37 38 39

44 9 6 45 8 3 4667 47 48 48 28 49 05 4980 50 53 51 25 51 96

40 41 42 43 44 45 46 47 48 49

52 64 5331 5398 54 6 2 55 25 5588 56 48 57 0 8 57 6 6 58 24

In Hg Abs

(Continued)

Absolute pressure ~n Hg

Temp F

STEAM DATA


95 23 51 78 06 33 60 87 13 39

596 591 586 581 576 571 567 562 558 553

Absolute pressure ~n H g

Temp F

Sp vol cu It lb


Temp F

Sp vol cu It Ib

Absolute pressure n Hg

Temp F

Sp vol cu ft Ib

2 93 2 94 2 95 2 96 2 97 2 98 2 99

114 11 11423 11435 11446 11458 11470 11482 11494

2368 2360 2353 2345 2338 2330 2322

2 2 2 3 5 8 1 5 1 7

Sp VOI for temp below 3 2 F are apDrox!mate Values from 0 5 to 18 In Hg reproduced by permission from Chemlcal Englneers Handbook by John H Perry publlshed by McGraw-HIII Book Co Inc Values from 1803 to 29 92 In Ha calculated araDhlcallv bv Inaersoll-Rand Co bv Dermlsslon of the authors and publlsher from data In " ~ h e r r i o d ~ n a m~~Yco i e r t l e sbl team" by Keenan a n d ~ e y e s .

1 92 1 93 2 2 2 2

46 47 48 49

Values from 05 to 18 In Hg reproduced by permlsslon from Chemlcal Englneers Handbook by John H Perry publlshed by McGraw-HIII Book Co Inc Values from 1803 to 29 9 2 In Hg calculated graphically by Ingersoll-Rand Co by permlsslon of the authors and publlsher from data In Thermodynam~cProperties of Steam by Keenan and Keyes

INGERSOLLRAND



In Hg Abs


(Continued) Absolute pressure ~n Hg

400 4 10

Temp F

12542 12633

SP vol cu ntlb

1767 1726


1100 1150

Temp F

1655 1674

Sp vol cuftllb

68 4 65 6

STEAM DATA

Absolute pressure ~nHg

2900 2992

Absolute pressure mm Hg Temp 'F

2104 2120

Sp vol cuft/lb

276 268

Values from 05 to 0 1803 In Hg reproduced by permlssion from Chem~calEng~neersHandbook by John H Perry, published by McGraw-HIII Book Co , Inc Values from 0 1803 to 29 92 In Hg calculated graph~callyby lngersoll Rand Co by permlsslon of the authors and publ~sherfrom data In Thermodynam~cProperties of Steam by Keenan and Keyes For correction of observed vacuum and barometer to standard condition see pages 7-5 to 7-10

Absolute pressure mm Hg

mm Hg Abs

Sp vol cu ft Ib

Absolute pressure mm H g

Temp F

Sp vol cu f t lb

7 8 55 7 9 15 79 74 8 0 33 8090 8 1 46 8 2 02 8 2 56 8310 8 3 63

662 3 6500 638 2 626 8 6158 605 3 594 9 585 2 5756 566 5

50 0 50 5 51 0 51 5 52 0 52 5 53 0 53 5 54 0 54 5

10061 100 94 101 27 10160 101 92 102 24 102 56 10288 10319 10350

3444 341 2 338 0 3349 331 9 328 9 326 0 323 1 3202 3175

30 0 30 5 31 0 31 5 32 0 32 5 33 0 33 5 34 0 34 5

8 4 16 8467 8 5 19 8 5 68 8 6 18 8 6 66 8715 8 7 62 80 0 9 88 55

557 5 5490 540 5 532 4 524 6 516 9 5095 502 4 495 4 4886

55 0 55 5 56 0 56 5 57 0 57 5 58 0 58 5 59 0 59 5

10381 104 12 10441 104 72 105 02 10531 10561 105 9 0 10619 106 47

3148 312 1 3095 306 9 304 4 301 9 299 5 297 1 2947 292 4

1576 1 1504 7 1439 8 1380 1 1326 0 1275 8 1229 5 1186 2 11461 11086

35 0 35 5 36 0 36 5 37 0 37 5 38 0 38 5 39 0 39 5

89 01 8 9 46 89 91 90 34 90 78 91 21 91 63 92 0 5 92 47 92 88

482 0 475 6 469 3 463 3 4574 451 7 446 1 440 6 4353 430 0

60 0 60 5 61 0 61 5 62 0 62 5 63 0 63 5 64 0 64 5

106 76 107 0 5 107 33 10761 107 88 10816 108 43 10871 108 9 8 109 24

290 1 2878 2856 2834 281 2 2791 277 0 2749 272 9 270 9

63 50 64 44 65 3 5 66 24 6710 67 94 68 76 69 56 70 34 7111

1073 6 1040 7 1009 8 980 8 9535 927 7 903 3 880 4 858 5 8375

40 0 40 5 41 0 41 5 42 0 42 5 43 0 43 5 44 0 44 5

93 29 93 69 94 09 9448 94 87 95 26 95 64 9611 96 39 96 76

425 0 420 0 415 1 4104 4058 401 4 397 0 3927 388 4 384 2

65 0 65 5 66 0 66 5 67 0 67 5 68 0 68 5 69 0 69 5

109 51 109 77 11004 11030 11056 110 82 11107 11 1 33 11158 11183

269 0 267 1 2652 2633 2614 2596 2578 256 0 2543 2526

71 85 7 2 59 73 31 7401 74 69 75 36 76 03 76 67 77 31 77 94

817 8 798 9 780 9 7636 747 3 731 7 716 4 702 1 688 3 674 9

97 13 9 7 49 97 85 98 21 98 56 9891 99 26 99 60 99 94 10028

380 3 376 4 3726 3688 365 1 3614 357 9 354 4 351 0 3477

70 0 70 5 71 0 71 5 72 0 72 5 73 0 73 5 74 0 74 5

11208 11233 11258 11282 11306 11331 11355 11379 11403 1'4 26

2509 2492 2475 2459 2443 2427 2411 2396 2381 236 6

Temp F

Sp v o cu f l Ib

15 20 25 30 35 40 45

8 73 14 5 0 1909 22 91 26 19 29 05 31 62

9700 7300 5920 4950 4250 3780 3380

25 25 26 26 27 27 28 28 29 29

0 5 0 5 0 5 0 5 0 5

4 579 50 55 60 65 70 75 80 85 90 95

32 0 0 34 17 36 55 38 7 7 40 8 2 42 75 44 55 46 25 47 8 6 49 37 50 8 3

3306 3042 2779 2558 2372 2211 2070 4 1946 8 1838 0 1741 8 1654 4

10 0 10 5 11 0 11 5 120 12 5 13 0 13 5 140 14 5

52 21 53 5 5 54 8 2 5605 57 22 58 36 59 45 6051 6154 6254

15 0 15 5 16 0 16 5 170 17 5 18 0 18 5 190 19 5 20 0 20 5 21 0 21 5 22 0 22 5 23 0 23 5 24 0 24 5

45 45 46 46 47 47 48 46 49 49

0 5 0 5 0 5 0 5 0 5

Temp F

Sp vol for temp below 32'F are approximate. Values from 1.5 to 4.579 mm Hg calculated from data n Chemlcal Engineers Handbook by John H Perry. published by McGraw-Hill Book Co., Inc. Values lrom 4 579 to 760 mm Hg calculated graph~callyby Ingersoll-Rand Co. by permlssion of the authors and publisher from data In 'Thermodynamic Properties of Steam by Keenan and Keyes

INGERSOLLRAND

Properties of Saturated Steam-Pressure; Absolute pressure m m Hg

T:mp F

Sp vol cuftllb

STEAM DATA


Absolute pressure mmHg

Temp F

Sp vol cu ftllb

Properties of Saturated Steam-Pressure

mm Hg Abs (cont.) Absolute pressure mm Hg

Temp 'F

Sp vol cu ftllb

Spec~flcvolume 11 Ibm Abs press Ib ~n

Temp F

Enthaipy btullbm

Water

Steam

Water

V,

V.

h,

Steam h,

Table

Entropy btu Ibm x F Water

Steam

5

5,

Abs press lb ~n

Values from 1 5 l o 4 579 mm Hg calculated from data In Chemlcal Eng~neersHandbook by John H Perry published by McGraw-HIII Book Co , Inc Values from 4 579 to 760 mm Hg calculated graph~callyby Ingersoll-Rand Co by permlsslon of the authors and publisher from data In Thermodynam~cproperties of Steam by Keenan and Keyes

I I I I I I I Tables on pages 5-19 to 5-20 reproduced by permlsslon from ASME Steam Tables Amer~canSoclety of Mechanical Engineers All rlghts reserved

I

1967 by The

INGERSOLLRAND


Properties of Saturated Steam-Pressure

Table (cont.)

Tables on pages 5-19 to 5-20 reproduced by permission from ASME Steam Tables Amerlcan Soclely of Mechan~calEng~neers All rlghfs reserved

STEAM DATA Properties of Superheated Steam

1967 by The

Tables o n pages 5.21 t o 5 2 4 reproduced from ASME Steam Tables' 1967 by The Amerlcan Soc~etyof Mechan~calEngineers All rlghts reserved +Sh = superheat v = speclflc volume ~nff3'lb, h = total heat In Btuilb, s = entropy In 6tui"FIlb

INGERSOLLRAND


STEAM DATA

Properties of Superheated Steam (cont.)

Properties of Superheated Steam (cont.) Abs press b ln(sat temp-F)

4000

Tables on pages 5 2 1 to 5 2 4 reproduced from ASME Steam Tables ' 1967 by The Amerlcan Soclety of Mechan~calEng~neersAll rlghts reserved 'sh = Superheat v = spec~flcvolume In ft3/lb h = total heat In Btullb s = entropy In BtuPFllb

Temperature-degrees Sat water

v h s

Sat steam

1

Fahrenheit

I

700

800

0 1052 11743 12754

900

1000

1200

1400

1500

0 1463 13116 13807

0 1752 14036 14461

02210 15522 15417

02601 16857 16177

02783 17506 16516

Tables on pages 5-21 to 5 2 4 reproduced from ASME Steam Tablesc 1967 by The Amer~canSoc~etyof Mechan~calEng~neersAll rlghts Reserved 'sh = superheat v = s p e c ~ f ~volume c In ft311b, h = total heat In Btujlb, s = entropy In BluPFllb

INGERSOLLRAND


STEAM DATA

Properties of Superheated Steam (cont.)

Theoretical Steam Rates, Condensing for Engines and Turbines Ib per hp-hr Exhaust pressure-in 3.0 ln~tial temp "F

2.5

2.0

1.5

1.0

150 Ib gage 365.8"F saturated steam

7.67 7.42 7.18 6.95 6.72

7.45 7.22 6.98 6.76 6.53

I

'2: 6.98

": ". 6.72

6.38

6.55 6.34

6.31 6.1 1

6.00 5.82

I

I

I

1

7.39

1

7.21

1

7.01

1

I

6.76

1

2.5

2.0

1.5

1.0

250 Ib gage 406°F saturated steam

1

300 Ib gage 421.7"F saturated steam 421.7

3.0



I

Hg abs

I

I

I

400 Ib gage 448.1°F saturated steam 6.47

Tables on pages 5-21 to 5-24 reproduced from ASME Steam Tables 1967 by The Amer~canSoclety of Mechancal Engneers All r ~ g h t sreserved 'sh = superheat v = s p e c ~ f ~volume c In ft311b h = total heat In Btuilb s = entropy In Btu1"Filb

750 800 850

5.94 5.76 5.57

5.81 5.63 5.45

5.66 5.49 5.32

5.48 5.31 5.15

5.25 5.09 4.94 I


goo 950

1

5.02 4.86

1

-

- -

4.93 4.78

1

4.82 4.67

1

4.69 4.55

/

I

I

I


4.52 4.39

INGERSOLLRAND

STEAM DATA


Theoretical Steam Rates, Condensing for Engines and Turbines

Theoretical Steam Rates, Non-Condensing for Engines and Turbines-lb per hp-hr

Ib per hp-hr

150 Ib gage, 3653°F saturated steam

Exhaust pressure-ln 3.0

lnitial temp "F 700 750 800 850 900 950 1000

2.5

2.0

5.41 5.21 5.04 4.88 4.73 4.59 4.45

5.28 5.10 4.93 4.78 4.63 4.49 4.36

4.97 4.80 4.65 4.50 4.37 4.24 4.12

5.15 4.97 4.81 4.65 4.52 4.38 4.26

2.0

1.5

365.8

1.0


1000 Ib gage 546.4"F saturated steam 5.51 5.31 5.14 4.97 4.81 4.67 4.52

2.5

3.0

1.0

1.5

lnitial temperature, "F

Hg abs

....

....

....

....

....

5.27 5.08 4.91 4.76 4.61 5.47

5.17 4.99 4.83 4.67 4.53 4.39

5.07 4.89 4.73 4.58 4.44 4.31

4.94 4.77 4.61 4.47 4.33 4.21

4.77 4.62 5.46 4.33 4.20 4.08

400

450

700

750

800

234

284

334

384

434

12.5 13.9 15.3 16.6

12.0 13.3 14.6 15.8

11.5 12.7 13.8 15.0

11.0 12.1 13.2 14.3

10.5 11.5 12.6 13.7

10.0 11.0 12.1 13.1

19.0 20.5 22.1 23.8

18.0 19.4 20.9 22.5

17.1 18.4 19.2 21.3

16.2 17.5 18.8 20.2

15.5 16.7 18.0 19.3

14.8 15.9 17.2 18.5

14.1 15.3 16.4 17.7

27.1 29.3 31.6 36.8

25.6 27.7 29.7 34.6

24.2 26.0 28.0 32.6

23.0 24.7 26.5 30.9

21.8 23.5 25.2 29.3

20.8 22.3 24.0 28.0

19.9 21.4 22.9 26.8

19.0 20.5 22.0 25.6

43.2 51.2 ....

40.5 48.1

38.2 45.3

....

....

36.2 42.9 51.7

34.3 40.8 49.2

32.8 38.8 47.0

31.4 37.2 44.9

30.1 35.6 43.0

650

700

750

800

0

34.2

84.2

134

184

0 5 10 15

14.4 16.2 17.9 19.6

14.1 15.7 17.4 19.1

13.6 15.1 16.7 18.3

13.1 14.6 16.0 17.5

20 25 30 35

21.3 23.2 25.0 27.1

20.8 22.6 24.4 26.4

19.9 21.6 23.3 25.2

40 45 50 60

29.3 31.7 34.3 40.2

28.5 30.8 33.3 39.0

70 80 90

47.3

45.8 .... ....

....

....

200 Ib gage, 387.8"F saturated steam



387.8


lnitial superheat, "F 0

12.1

62.1

112

162

600

650

Ib per hp-hr

-

550

Initial superheat, F

Theoretical Steam Rates, Non-Condensing

Exhaust press l blsq in gage

500

Exhaust press lblsq In Sage

212

262

312

362

412

400

450

500

550

600

Exhaust press lblsq in gage

0

12.2

62.2

112

162

212

262

312

262

412

0 5 10 15

13.1 14.4 15.7 17.0

13.0 14.3 15.6 16.9

12.5 13.7 15.0 16.2

12.0 13.2 14.3 15.5

11.5 12.7 13.8 14.9

11.1 12.1 13.2 14.1

10.6 11.6 12.5 13.5

10.2 11.1 12.0 12.8

9.7 10.6 11.4 12.2

9.3 10.1 10.9 11.7

20 25 30 35

18.3 19.6 20.9 22.3

18.1 19.4 20.8 22.1

17.4 18.6 19.9 22.1

16.6 17.8 19.0 20.2

15.9 17.0 18.0 19.1

15.1 16.1 17.1 18.1

14.4 15.3 16.2 17.2

13.7 14.6 15.4 16.3

13.1 13.9 14.7 15.6

12.5 13.3 14.1 15.0

40 50 60 70 80 90 100 110

23.8 26.8 30.1 34.0 38.3 43.5 49.6 ....

23.6 26.5 29.9 33.8 38.0 43.1 49.2

22.5 25.3 28.5 32.0 36.1 40.9 46.5

21.4 24.1 27.0 30.2 33.9 38.3 43.3 49.4

20.3 22.7 25.4 28.4 31.9 35.9 40.7 46.5

19.2 21.4 24.1 26.9 30.2 34.0 38.5 44.1

18.2 20.4 22.8 25.5 28.6 32.3 36.6 41.8

17.3 19.4 21.7 24.3 27.3 30.7 34.8 39.8

16.5 18.5 20.7 23.2 26.0 29.3 33.3 38.0

15.8 17.7 19.8 22.2 24.9 28.1 31.8 36.5

Initial superheat, O F

....

....


STEAM DATA

Theoretical Steam Rates, Non-Condensing for Engines and Turbines

Theoretical Steam Rates, Non-Condensing (Continued) for Engines and Turbines

250 Ib gage, 406.0°F saturated steam

400 Ib gage, 448.1°F saturated steam

lnitial temperature, "F 406 Exhaust press lblsq in gage 0 5 10 15

450

500

550

600

650

700

lnitial temperature. "F 750

800

448.1

850

500

550

650

700

800

850

900

302

352

402

452

750

o

44

94

144

194

244

294

344

394

444

12.1 13.3 14.4 15.4

11.7 12.8 13.9 14.9

11.3 12.3 13.3 14.3

10.9 11.8 12.8 13.7

10.4 11.4 12.3 13.1

10.0 10.9 11.7 12.5

9.6 10.4 11.2 11.9

9.2 10.0 10.7 11.4

8.8 9.6 10.2 10.9

8.5 9.2 9.8 10.4

0 5 10 20

10.6 11.5 12.2 13.7

10.2 11.0 11.7 13.0

9.8 10.5 11.2 12.5

9.4 10.1 10.8 11.9

9.0 9.7 10.3 11.4

8.7 9.3 9.9 10.9

8.4 8.9 9.5 10.4

8.0 8.6 9.1 10.0

7.7 8.2 8.7 9.6

7.4 7.9 8.4 9.2

30 40 50 60

15.0 16.3 17.6 18.9

14.3 15.6 16.8 18.0

13.7 14.8 16.0 17.2

13.1 14.1 15.2 16.3

12.5 13.5 14.5 15.5

11.9 12.8 13.8 14.7

11.4 12.2 13.1 14.0

10.8 11.7 12.5 13.3

10.4 11.2 11.9 12.8

9.9 10.7 11.4 12.2

80 100 120 140

21.7 24.7 27.9 31.6

20.6 23.4 26.5 29.9

19.6 22.2 25.0 28.1

18.5 20.9 23.5 26.4

17.5 19.7 22.2 24.9

16.6 18.7 21.0 23.6

15.8 17.8 20.0 22.4

15.1 17.0 19.1 21.4

14.4 16.2 18.2 20.5

13.8 15.6 17.5 19.6

160 180 200

35.8 40.7 46.6

33.8 38.4 43.7

31.7 35.8 40.6

29.7 33.5 38.1

28.0 31.7 36.0

26.5 30.0 34.1

25.2 28.5 32.4

24.1 27.2 30.9

23.0 26.0 29.6

22.1 25.0 28.4

900

950

1000

Initial superheat, "F

Initial superheat, "F 0

51.9

102

152

202

252

300 I b gage, 421.PF saturated steam


lnitial temperature, "F 421.7 Exhaust press l blsq in gage

600

Exhaust press lblsq i n gage

450

500

550

600

650

700

lnitial temperature, "F 750

800

850

Initial superheat, "F 0

28.3

78.3

128

178

228

278

328

378

428

0 5 10 15

11.5 12.5 13.5 14.4

11.2 12.2 13.2 14.0

10.8 11.7 12.6 13.4

10.4 11.3 12.1 12.9

10.0 10.8 11.6 12.3

9.6 10.4 11.1 11.8

9.2 10.0 10.6 11.3

8.9 9.6 10.2 10.8

8.5 9.1 9.7 10.3

8.2 8.8 9.3 9.9

20 30 40 50

15.3 17.0 18.7 20.5

14.9 16.5 18.3 20.0

14.3 15.8 17.4 19.1

13.7 15.1 16.6 18.1

13.1 14.4 15.8 17.3

12.5 13.7 15.0 16.3

11.9 13.1 14.3 15.5

11.3 12.5 13.6 14.8

10.8 11.9 13.0 14.1

10.4 11.4 12.4 13.5

60 80 100 120

22.4 26.5 31.2 36.6

21.8 25.7 30.2 35.6

20.7 24.5 28.7 33.5

19.7 23.1 27.0 31.5

18.7 21.8 25.4 29.7

17.7 20.6 24.1 28.1

16.8 19.6 22.8 26.8

16.0 18.7 21.8 25.5

15.3 17.9 20.8 24.4

14.6 17.1 19.9 23.3

140 160 180

43.5 52.3

42.2 50.4

39.7 47.2

37.1 44.1

....

....

35.0 41.6 50.5

33.1 39.4 47.7

31.4 37.3 45.3

30.1 35.6 43.1

28.7 34.2 41.3

27.4 32.6 39.6

....

....

575 Exhaust press Iblsq in gage

600

650

700

750

800

850

lnitial superheat, "F

Pages 5-25 to 5-29 calculated from "Theoretical Steam Rate Tables" by J. H. Keenan and F. G. Keyes, published by American Society of Mechanical Engineers.


STEAM DATA -

- -

Corrections to Rankine Cycle Efficiency Curves Superheat Corrections

Approximate Turbine Efficiency*-Rankine Cycle 3600 rprn

Single-stage

-

Type of turbine

Add or subtract to or from RCE

Correction method Superheat

/Y 1

I0 psigl I /

g

I

CONDENSING

-600 p s i r

Y

5a 40,200

1

FOR A P P R O X I M A T I O N S O N L Y

I

I

300 400

l

2" Hg Abs, Exhaust - loo0 F Superheat 3600 RPM l

I

I

I

600 800 I000 1500 2000 TURBINE HORSEPOWER

Non-condensing

Condensing

Multiply

Multiply

0.963 1.000 1.012 1.015

0.977 1.000 1.018 1.034

add 0.6

0°F 100°F 200°F 300°F W

Multi-stage

Non-condensing

-

Subtract 0.6 Subtract 1.2

Speed Correction Multiplier for Speeds Other Than 3600 rpm Multi-stage Turbines Only

I

Non-condensing

3000 4000 5000 D-1343

Condensing

RPM

3000

5000

7500

10,000

3600

5000

7500

10,000

BHP 500 1000 2000 3000 5000

1.000 1.000 1.000 1.000 1.000

1.030 1.013 1.001 0.997 0.994

1.036 1.006 0.980 0.968 0.959

1.018 0.982 0.940 0.920 0.902

1.000 1.000 1.000 1.000 1.000

1.000 1.000 1.000 1.000 1.000

1.000 1.000 1.000 0.984 0.955

1.000 1.000 0.957 0.929 0.895

EFFICIENCY Page 5-30 gives approximate Rankine cycle efficiencies (RCE) for single-stage and multi-stage turbines at various ratings and steam pressures. These data may be used only for rough estimating. There is considerable variance between manufacturers for a given rating and condition, some offering a higher efficiency, some lower, depending upon how the conditions match a particular size or design.

I

100

200

300 400

600 800 1000

1500 2000

TURBINE HORSEPOWER

3000 4000 5000 D-1344

Theoretical Steam Rate Formulas TSR

=

Steam flou (Ibihrl =

I

I

2545 AH

'

TSR x hp corrected efhc~encg

100 -.

where the back pressure is in psig."

TSR = theoret~calsteam rate-lblhp-hr AH

*

=

difference ~n enthalpy between inlet and exhaust steam ( ~ e n t r o p s )

Corrections for superheat and speed on next page.

Although very large turbines a r e used for certain types of drives, a limit of 5000 hp has been chosen for these data since it was felt this encompassed the majority of drives where such data would be used. I t is to be expected that larger units would have higher efficiencies. F o r example, a 25,000 hp, 3600 rpm turbine a t 600 psig, 750°F and 5" H g abs. exhaust, would have an efficiency of about 82%. "Single-stage turbines often operate a t some back pressure. The curves a r e based on 5 psig back pressure. For back pressures to 50 psig multiply RCE from t h e curves by a correction factor equal to: 0-25 (backhressure - 5) corr. Factor = 1 +

I

8

Condensing turbines show a small increase in RCE for higher absolute exhaust pressure (lower vacuums), but it is not slgmficant for the purpose of . . these curves.

CAMERON HYDRAULIC DATA Gas o r Vapor Flow For flow problenls involving gas or vapor the Darcy formulae are: dV - 6.32 W - 2273.5 Qp - 378.9 q p R = Dvp = - - - dz 32.174 u 12 v (l z (1z

STEAM DATA The Darcy formula can not be applied indiscriminately to vapor or gas flow because it does not take into account the affect compressibility has on velocity and density. 1. When h,, is less than 10% of upstream pressure, reasonable accuracy is obtained. Base p and V on either upstream or downstream conditions. 2. When h , is between 10 and 4 0 9 of upstream pressure, reasonable accuracy is obtained by using p and V based on an average of upstream and downstream conditions. 3. When h , is over 404 of upstream pressure divide the total length into shorter sections and add the pressure drops for each section.

FRICTION O F STEAM IN PIPES Use of tables and charts, pages 5-34 to 5-37 and 5-39 Symbols D = internal pipe dia-ft d = internal pipe dia-in f = frlction factor (page 3-11) g = acceleration due to gravity -32,174 ftlsecL h, = pressure drop -inches of water h, = pressure drop-psi L length of pipe-ft p = density a t temp and press of flow conditions-lb/fti q = flow-cfm-ftilmin Q = flow-cfs-ft3/sec R = Reynolds number s, = specific gravity of gas (air = 1) u = absolute viscosity = Ibf-sec/ft2 V = velocity of flow-(ftlsec) v = kinematic viscosity (ftL!sec) W = flow-lb!hr w = specific volume-ft

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-

h N

N

o 0 0 0 0 ~ h ~ - - -

s2

I

'

I

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!

I

I

Welded and Seamless Wrought Steel Pipe

I Size

1

II 1 - 1t

~ c t ~ e d ~lle no

I

I

'tk: lnches

1

~nches

1

rnches

1

I C~rcurnlerence ~xternal

/

nches

1

1

I

lnches

e

I

Transverse area a

l e a l

1

SO

~n

Internal 30

in

1

Lenqth o l p f p e per sq 11 ot surface area External surface

I

feel

1 1

Internal surtace feet

/

1 1

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1/

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5elecled from ANSI B 36 1 0 1975 X Extra strong XX Double extra strong S Standard Allowable worklnq pressures based on Grade B pipe l e n s ~ l estrength 60 000 psl 35000 psl ybeld polnt Allowable w o r k ~ n gpressures at 400 F are 86 3"" of those at 100 F Allowable worklng pressures of Grade A ptpe al 100 F are 8 0 " ~o f Grade B plpe at 100 F Water hammer factors should be used l o reduce allowablp w o r k ~ n gpressure by the amount of flow n gal p r r

N2

Allowable

(P ~d1.r hammer

P

INGERSOLLRAND


Steel Pipe Flanges

CAST IRONAND STEEL PIPE FLANGESAND FLANGE FITTINGS

American National Standard (cont.)

Steel Pipe Flanges

Length thru hub In Nom~nal pipe size

Outs~de

Flanae thlcc-

1 1 1 1 z r1 l

a

f )

Threaded

welding

1

Lapped

I

Wneck eld~ng

Nom~nal

American National Standard (cont.) Length thru hub In

PIP^

Flange ratlng

sue

DSI

Outs~de flanage d~a ~n

Flange thck ness (mln) ~n

D~arneter bolt c~rcle

Threaded sl~p-on socket weldlna

Lapped

Weld~ng neck

From ANSl B 16 5 Sllp-on w e l d ~ n gnot In 2500 Ib ratlng and only In 1% to 2'4 slzes for 1500 b ratlng and 1% to 3 In sues for 150 l b ratlng Socket w e l d ~ n anot n 400 900 and 2500 Ib ratlnqs and only In 1'2 to 2II2 ssles for 1500 l b ratlng and 'h to 3 slzes In 300 Ib rn tig Threaded In 1500 Ib r a t ~ n gfrom 1,2 to 12 In slzes only

From ANSl 8 16 5 Sltp-on weldtng not n 2500 Ib ratlng and only n 1'4 to 2'12 slzes for 1500 Ib rallng and 11/2 to 3 In sues f o r 150 Ib r a t ~ n a Socket weld~Ggnot In 400 900 and 2500 Ib ratlngs and only ~n 'I2 to 21 ' 2 slzes f o r 1500 Ib r a t ~ n gand 1 2 to 3 slzes In 300 Ib r a t ~ n g Threaded In 1500 b r a t ~ n gfrom 'I2 to 12 In slzes only

Flange Ratings-150 Ib. Table G-150 PN20 Pressure-TemperatureRatings Gage pressures in bar

1 Bar

c

1 4 5 p s I (pressure) F-32) (temperature)

o 5556 (

Flange Ratings-300 Ib. Table G-300 PN50 Pressure-Temperature Ratings Gage pressures in bar

_Allays ~

Fe $

Carbon 400 Alloy 405 600 414497 4 0 3 4 8 7 36 1 46 1 3 3 6 4 4 0

Temp C

U 1The9~ ratlng? are at 540 'C max

I

L

service temperature

NOTES' 1 Ratings shown apply la other malerlal groups where column dlv~d~ng lhnes have been omltt~d 2 Provls!ons of Sectlo" 2 apply to all ratings 3 S r r Temperature Notes far all Mater~alGroups

1 Bar C

14 5 p s l (pressure) 0 5556 1 F 3 2 ) (temperature1

~ Cr ~

Mo ~

Alloy Alloy

800 497 4 8 8 454 4 3 0

I32

I kelI Temper N t At loys

ature

517

38

517 51 5 SO2

50 100 150

c

-

~

Flange Ratings-400 Ib. Table G-400 PN68 Pressure-TemperatureRatings Gage pressures in bar

E -l l ~ r -o 1 r1 1 1 2 1 1 7 1 1 4 Malerl~ls Carbon

17

I 5

19

110

113

114

21

22

23

24

25

27-31 Cr

26

Fe

Mo 2CrType 1 Cu 304L 1 'nMo Types N l C r 1'1Cr 2'dCr 5Cr 9Cr Type Type Type Type 347 Type Type Cb '2Mo Ma h M o 1Mo IiMn 1Ma 304 316 316L 321 348 309 310 20Cb 552 618 662662551 662662 690 567 6 3 8 6 9 0 6 9 0 6 9 0 543 604 638642533640645 690 556635690682683 552 508 545 563 460 553 580 687 515 621 687 650 654 480 522 484 5 1 3 4 1 6 5 0 0 5 4 0 669 503 599669618622 C

Temp C 291038 50 100 150

681690 668690 618687 601669

638 631 601 586

200 250 300 350

584 650 556618 516 566 493536

569 541 503 480

488 463 431 412

J75 400 425 450

48 6 51 1 460460 383 383 26 1 2 6 7

47 1 432 36 4 26 4

41 2 404 34 4 26 1

475 500 525 550

18 1 11 7 69 43t

-

51 7 48 8 468

650 618

460 4 6 8 419 451

201 2 5 1 2 7 0 2 9 2 2 0 6 3 0 1 1 4 3 t 186 170 2 1 8 156 226 166

575 600 625 650 675

606 598 593 590 56 6 53 6

650 618

589 574 560

3

2

113 78 45 4 3

156 102 88 ~

117 87 60 ~

437 407 387 374

476 445 422 406

383 356 337 321

458 427 407 391

512 483 459 439

493 468 446 426

370 366 362 358

396 388 382 374

315 309 303 297

386 382 380 376

429 424 420 410

418 410 400 392

80 62 49 37 27

34- 35

N, Cu Cr Nickel Alloys Fe 400 Alloy Alloy 200 405 600 331 552662 331 537649 481 6 1 4 331 447587 331 NI

331 33 1 731

440 43 7 437 43 7

567 549 532 51 7

36

37

38

NI

Fe NI Nlc Cr Mo kel Ternpcr ature Alloy Alloy A1 82 loys C 800 38 690 662 50 690 650 100 687 605 150 573 669 553 53 5 529 52 2

437509514 48 8 43 0 46 8 42 2

650 61 8 566 53 6

200 250 300 350

517

375 400 425 450

z;:

:;: i??

475 500 595 550

344344338344 333 333 291 315

318344 291 333

150 268 321 9 6 223 286 6 6 174 7 4 7 4 9 ~ 103 168

700 725 750 775 800

32

304 264 211 1 ~6 6 131 1 0 2 83 64 50 40

133 103 78 61 47

321 286 237 1~5 4 115

248 194 152 1 0~7 93

293 258 222 188 151

575 600 625 650 675

90 70 54 42 35

75 58 45 34 26

116 82 58 42 29

700 725 750 775 800

t T h e ~ erallngs arc at 540 C max servlce temperature NOTES .-

1 Rat~ngsshown aclf,lyla other materlal qroups where column dlvldlng llnesare ornlned 2 Prons~onsof Sectlo" 2 apply to all rallngs 3 See Temperature Notes fur 1 1 1 Malertal Groups 1 Bar

C

14 5 p s 8 lprrssurcl 0 5556 ( F 32) (ternperntrlrr!

-

Flange Ratings-600 Ib.

TableG-600 PNlOO Pressure-TemperatureRatings Gage pressures in bar ---

Marl Grorrp Mat~r~a~s Carbon

Type 304 993 957 818 72 7

lype lype lype 316 316L 321 993 827 993 963 799 960 844 690 830 77 0 62 5 75 0

341 348 993 968 869 81 0

655 611 581 561

713 668 633 608

768 724 689 658

NOTES: 1 Halln~s shown apply 10 other maler~algroups wherecolumn dtvbdlng hnes are omllted 2 P r o v l s l o n ~of Scctlon 2 apply l o all ratings 3 See Temperature Notes for all Matertal Groups 1 Bar

C

14 5 p il (p!?ssnr~.l 0 5556 I ' F 32) (temperature)

574 534 505 481

687 641 611 587

lype 309

:

Typ~ 310 20Cb 82 8 814 76 2 721

669 639

N k Alloy 200 49 7 497 49 7 497

1 1 !lays1

:

N, Nlc MO kel Temper 400 Alloy Alloy Alloy A1 ature 405 600 800 B2 "C 82 8 9 9 3 99 3 103 4 38 8 0 6 974 976 1034 50 72 1 92 1 90 7 1031 100 671 880 860 1004 1SU

Flange Ratings-900 Ib. Table G-900 W 1 5 0 Pressure-Temperature Ratings Gage pressures in bar

NOTES 1 Rat~ngsshown apply to other mater~algroups where column dlvidlng llnes are omlned 2 Prov~s~ons of Sectton 2 apply l o all rallngs 3 See Temperature Notes for all MaterialGroups

1 Bar C

14 5 p s I (pressure) 0 5556 ( F 321 (temperature1

Flange Ratings-1500 Ib. Table G-1500 PN250 PressureTernperature Ratings Gage pressuresin bar

NOTES I Ratings shown apply to other mater~algroups where column dlvldlnq lhnesare omlned 2 Provrs~ons of Sect~on2 apply to all ratings 3 See Trmp~ratureNates for all Material Groups

1 Bar C

14 5 p s I (pressure) 0 5556 1 F 321 ltemperaturel

.

1

A

/

9

SECTION Vlll

-

MISCELLANEOUS DATA

-

INGERSOLLRAND

MISCELLANEOUS


Decimal and Millimeter Equivalents

1 1 q;:. 1 Fract~on

Dec~mal equlvalent

of tractional inches

1 1 e?qL:iFract~on

Dec~mal equlva lent

of tractlonal lnches

CONTENTS OF SECTION 8 Miscellaneous Data Decimal and Millimeter Equivalents

. . . . . . . . . . . . . . . . . . . .

Page . 8-3

Arithmetical and Geometrical Formulas . . . . . . . . . . . . . . . . . . 8-3 Approximate Altitude and Barometer Reading

. . . . . . . . . . . . .

8-4

Barometer Reading Corrections . . . . . . . . . . . . . . . . . . . . . 8-5 to 8-9 Weight and Dimensions of Copper Tubing and Pipe

. . . . . . . . .

8-10

Volume in Partially Filled Horizontal Tanks

. . . . . . . . . . . . . . 8-11 Capacities of Cylinders and Tanks . . . . . . . . . . . . . . . . . . . . . . 8-12

Displacement Per Stroke of Plungers

8-13 Areas of Circles . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 8-14 Hardness Conversion n b l e

. . . . . . . . . . . . . . . . . . .

. . . . . . . . . . . . . . . . . . . . . . . . . . . 8-15

Use of Gages and U Tubes . . . . . . . . . . . . . . . . . . . . . . . 8-16 to 8-20 Pump Data Sheet for Material Selection Pump Materials

. . . . . . . . . . . . . . . . .

. . . . . . . . . . . . . . . . . . . . . . . . . . . . .

8-21

8-22 thru 8-28

Arithmetical and Geometrical Formulas : Circumference of Circle = 3.1416 x dia = 6.2832 x radius Area of Circle = ,7854 x (dial2 = 3.1416 x (radiusI2 Area of Sphere = 3.1416 x (dial2 Volume of Sphere = 0.5236 x (dial3 Area of triangle = 0.5 x base x height Area of a trapezoid = 0.5 x sum of the two parallel sides x height Area of a square, a rectangle or parallelogram = base x height Volume of a pyramid = area of base x 1.3 height Volume of a cone = 0.2618 x (dia of baseI2 x height Volume of a cylinder = 0.7854 x height x dia2

MISCELLANEOUS


Barometer Corrections

Approximate Atmospheric Pressures and Barometer Readings at Different Altitudes

Miscellaneous Mm of mercury

Atmospheric pressure Ibiin2

Equivalent head of water (75'F) Feet

787.9 773.9 760.0 746.3 733.1

15.2 15.0 14.7 14.4 14.2

35.2 34.7 34.0 33.4 32.8

Barometer Alt~tude Feet

Meters

Inches of mercury

-1000 -500 0 500 1000

-304.8 -152.4 0 152.4 304.8

31.02 30.47 29.921 29.38 28.86

Boiling point of water "F

"C

213.8 212.9 212.0 211.1 210.2

101.0 100.5 100.0 99.5 99.0

i

Other barometer corrections include those for latitude, altitude and difference in elevation between barometer and datum plane. These are given on the following page. Table I , 111. IV and V apply to mercurial barometers. Table V applies to aneroid barometers. Table I1 applies to small-bore, single-tube mercury columns. U-tubes and manometers, in which both legs have approximately the same bore, and lal-ge-bore, single-tube columns do not require capillarity correction. The temperature correction from Table I applies to any mercury colunin when brass scales calibrated in inches a t 62°F and a density factor for mercury based on 32°F are used. Tables I11 and I V apply to all mercury columns in which a density factor based on 45" latitude and sea level altitude is used. The corrections are small and are usually ignored or taken into account by uslng a density factor based on the latitude and altitude of the datum point. In general, aneroid barometers a r e not satisfactory for accurate testing. If one is used, it should be compensated for temperature and frequently calibrated against a standard mercurial barometer, as a violent knock or shaking may introduce a substantial error.

Example of use of Tables 111, IV and V. Assume a barometer reading of 20.013" Hg a t 70°F'. 1000 ft altitude, 45" latitude a n d 30 ft above t h e datum plane for which a reading is desired. Barometer reading . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 29.013" Latitude correction (Table 111) . . . . . . . . . . . . . . . . . . . . . . . . . . . - .048" Altitude correction (Table IV) . . . . . . . . . . . . . . . . . . . . . . . . . . . . - .002" Elevation correction (Table V) ( . 3 x .102) . . . . . . . . . . . . . . . . . + .031" Temperature correction (Table I) . . . . . . . . . . . . . . . . . . . . . . . . . - ,019" Corrected barometer (to 3TF, 970 ft altitude, and 45" latitude) . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 28.885"

Temp hg co1

F

Correction for Relative Expansion of Mercury and Brass Scale to 32°F Standard

Correction of Small Bore Single-tube Mercury Columns for Capillarity

Table I

Table II

Observed i e a d ~ n gof the barometer In lnches

25

I

MISCELLANEOUS


INGERSOLLUAND

25 5

26

26 5

27

27 5

28

28 5

29

29 5

C o r r e c t o n to be subtracted from oaserved readlng

Helght of men~scus-~nches 30

1

30 5

31 0

ID tube lnches

.01

.02

03

04

.05

.06

.08

07

Correction to be added to hg column read~ng-lnches

(From Smithson~anPhyslcal Tables-1933)

Explanation of Correction Tables for Mercurial Barometers Table I-Examples

of use

Reading of barometer a t 75°F . . . . . . . . . . . . . . . . . . . . . . . . . . . 29.964" Temperature correction (Table I) . . . . . . . . . . . . . . . . . . . . . . . . - . 126" Barometer corrected to 32°F . . . . . . . . . . . . . . . . . . . . . . . . . . . . 29.838" Reading of Mercury column a t 97°F . . . . . . . . . . . . . . . . . . . . . . 28.120" Temperature correction (Table I) . . . . . . . . . . . . . . . . . . . . . . . . - . 173" Vacuum corrected to 32°F. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 27.947" Absolute pressure (29.838 - 27.947) . . . . . . . . . . . . . . . . . . . . . .

Table 11-Example

Condensed frorr c r c u l a r F U S W e a t i e r B ~ , e a u

1.891"

of ITse

Suppose above mercury column had a single tube of 51:32' bore and the estimated height of meniscus was .03" Correction for capillarlty (Table 11) . . . . . . . . . . . . . . . . . . . . . .

1

.102"

Vacuum corrected for capillarity (27.947 + ,102) . . . . . . . . . . . 28.049" Absolute pressure (29.838 - 28.049) . . . . . . . . . . . . . . . . . . . . . . 1.73Y1' NOTE:-Xl\vays read the top of the meniscus and arid the capillarity correction to this vacuum column reading. There is no correction on double tube mercury columns or manometer?. 8-7

INGERSOLLRAND


MISCELLANEOUS

Correction of Mercurial Barometer for Latitude in Inches Hg to Reduce to 45' Latitude

Correction of Mercurial Barometer for Altitude

To be added to barometer reading for latitudes above 4 5 . To be subtracted from barometer reading for latitudes below 45

Table IV

Inches Hg to be subtracted from barometer reading

Table Ill R e a d n g o f tile barometer n n c n e s

Alt~tude ft

Read~ngof barometer, ~nches

. 26

25

30

29

28

27

,

1

31

Elevation Correction for Barometer In inches Hg per 100 ft difference i n elevation. To be added to barometer reading when barometer is above datum plane. To be subtracted from barometer reading when barometer is below datum plane. Table V Temperature. "F Alt~tude ft

0

10

20

30

40

50

60

70

80

90

INGERSOLLRAND CAMERON HYDRAULIC DATA Weights and Dimensions of Copper and Brass Pipe and Tubes

MISCELLANEOUS Volume of Horizontal Tanks in Gallons per Foot of Length

Copper t u b ~ n g Copper and brass p l p e Regular fit Type K

Type

L

Type M Welghf per It Ib

Nom ~nal slze n

In Out slde slde d ~ a m diam in in

Wt per ft Ib

In Side dlarn in

Wt per ft Ib

In side dlarn in

Wt per 11 lb

Out side dlarn In

In side dam in

405 540 675 840

281 375 494 625

67'0

85".

100°c

Cop per

Copper

Copper

250 375 500 625 750 875

186 311 402 527 652 745

085 134 269 344 418 641

200 315 430 545 666 785

068 126 198 284 362 454

20 325 450 569 690 811

068 106 144 203 263 328

1050

822

124

127

130

1

1 125

4

1375 1625 2125 2625

995 1245 1481 1959 2 435

839 104 136 206 292

1 025 1 265 1505 1985 2 465

653 882 114 175 2 48

1055 1291 1571 2009 2 495

464 681 940 146 2 03

1315 1660 1900 2375 2875

1062 1368 1600 2062 2 500

174 2 56 304 402 5 83

1 79 2 63 313 414 6 00

183 2 69 320 423 6 14

3 3'2 4 4' 2

3 125 3625 4125

2 907 3385 3857

4 00 512 651

2 945 3425 3905

3 33 429 538

2 981 3459 3935

2 68 358 466

3 500 4000 4500 5000

3 062 3500 4000 4500

8 31 1085 1229 1374

8 56 1111266 1415

8 75 1141 1294 1446

5 6

5 125 6125

4 805 5741

967 1387

4 875 5845

7 61 1020

4 907 5881

6 66 891

8 125

7 583

2590

7 725

19 29

7 785

16 46

5 563 6625 7 625 8625

1 5 40 1844 23 92 3005

15 85 1399 24 6 3 3095

16 21 1941 25 17 31 6 3

'6

' r 48

' z '8

1'2 2 2'2

7

8

1

5 063 6125 7 062 8 000

246 437 612 91 1

I

253 450 630 938

259 460 643 957

Volume ln tank (gals)' Cos H

=

2(0 5

-

-

7 4805

portlon f l l e d ) D

.

-D- H &(st"

-

720

-

2

"1 ( 0 5

-

portlon rllled)'

tank d a (fll vol of full tank (gals)

' Applies to tanks up to 50". illled When tank f r o m full tank

IS

i'

-

lengln

7 4805&

$1"

8,

\ 1

cos+#

' length

over 50'0 fllled calculate p o r t o n r o t Illled and subtract

MISCELLANEOUS

INGERSOLLRAND CAMERON HYDRAULIC DATA and Tanks

Capacities-Cylinders

1

"i Z 1

z

e w e a m m m o O

N

--

~

O

oom

$

I

- N n e m

w c m m o N

---

N

~

~

N

~

-

o - ~ m m

b

m m w m e N - m m o - m v r -

0 0 - n m

U

Z

N

~

- - N N N

1

0 N 0 0 m o o w n o me

N

m o m e w - W O W N - - N N D

o m ~ o wN m w m g 0 o u w m o n o m a r m m o z o

- O N - U o w m o m

W 0 W 0 e e - m w u n e e m w

~

o

~

r-oowo - - - N

~

N

O

O

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no m w m m a m - o m - 7 N N N

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w r - o n e ~ ~ N N N n D O

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wr-m-m or-eon v w o e o m m N N m hO m ~ u h m ~ m m - ~ m r m N O O - - - N N N N O O f e f m m aP-S

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1

Stroke lengths in inches

w e e m o o o o w o o m 0 ~ m m mN ~ O 0 O m ~mW- ~ e h ~e 0 Om

O O W N

1

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w e w w

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1

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w c m m o

Displacement per Stroke-In U.S. Gallons For Various Diameter Plungers

m e m n D O -

1 / N q w onn

Plunger diam in lnches

1

1

2

2'2

3

32

4

8125 875 9375 1000 1 0625

00224 00261 00299 00340 00383

00336 00392 00448 00510 00574

00448 00522 00598 00680 00770

00560 00652 00748 00850 00959

00672 00783 00897 01020 01151

00785 00914 01046 01190 01343

00896 01044 01196 01360 01535

01120 01305 01495 0170 01915

01345 01565 01795 0204 02298

01570 01830 02093 0238 02681

01792 02090 02329 0272 03064

1 125 11875 1250 13125 1 375

0043 004'9 00532 00586 00643

00645 00718 00797 00879 00965

0086 00957 0106 01172 0129

01076 01196 0133 01465 0161

0129 01435 0159 01758 0193

01506 01674 0186 02051 0225

01721 01916 0213 02344 0257

0215 02395 0266 02930 0322

0258 G2874 0319 03516 0386

0301 03353 0372 04102 0451

0344 03832 0425 04688 0514

14375 1 500 15625 1625 16875 1750

00703 00765 00830 00898 00968 01041

01054 01 148 01245 01348 01452 01561

01405 0153 01660 01798 01936 02082

01756 0191 02075 0225 02420 02610

02108 02295 02490 0270 02904 0312

02459 0268 02905 0314 03389 0364

02810 0306 03320 0360 03873 0417

03513 0383 04150 0450 04841 0521

04216 0458 04980 0538 05809 0624

04920 0536 05810 0628 06777 0728

05621 0612 06640 0718 07745 0832

18125 1875 10375 2000 20625

01117 01196 01276 01360 01446

01675 01794 01914 0241 02169

02234 0239 02552 0272 02892

02792 0299 03190 0340 03615

03351 0359 03828 0408 04338

03909 0418 04466 0477 05061

04468 0478 05104 0544 0578C

05585 0598 06380 0680 07230

06702 0718 07656 0817 08676

07819 0837 08932 0953 10122

08936 0957 10208 1088 11568

2 125 21875 2250 2 3125 2375

01536 01627 01720 01818 01917

0230 02440 0258 02727 0287

0307 03254 0344 03646 0383

0384 04067 0430 04545 0478

0461 04881 0516 05454 0575

0537 05694 0602 06363 0671

0614 06508 0688 07272 0767

0768 08135 0860 09090 0958

0922 09762 1033 10908 1148

1075 11389 1205 12726 1340

1228 13016 1376 14528 1532

2 500 2 625 2 750 2875 3 000

02125 02347 02573 0281C 0306C

0319 0352 0386 0421 0459

0425 0469 0514 0562 0612

0532 0587 0643 0702 0765

0637 0704 0772 0843 0918

0744 0822 0900 0983 1071

0850 0939 1029 1124 1224

1063 1173 1287 1405 1530

1274 1409 1544 1686 1836

1468 1643 1802 1967 2142

1700 1878 2058 2248 2448

3125 3 250 3375 3500 3625

03320 03590 03872 04165 04470

0498 0538 0581 0624 0670

0664 0718 0714 0833 0894

0830 0897 0968 1042 1117

0996 1077 1162 1249 1341

1162 1256 1355 1458 1565

1328 1436 1549 1666 1768

1660 1795 1936 2083 2235

1992 2154 2323 2499 2682

2324 2513 2710 2916 3129

2656 2872 3097 3332 3576

3 750 3875 4000 4125 4250

04780 05110 0542 0578 0614

0717 0766 0813 0867 0921

0956 1022 1084 1156 1228

1195 1277 1'360 1445 1535

1434 1533 1626 1734 1842

1673 1788 1897 2023 2149

1912 2044 2168 2312 2456

2390 2555 2710 2890 3070

2868 3066 3252 3468 3684

3346 3577 3794 4046 4298

3824 4088 4336 4624 4912

4375 4 500 4 625 4 750 4 875

06508 06885 07273 07672 0808

0976 1033 1091 1151 1212

1302 1378 1454 1534 1616

1627 1722 1818 1918 2020

1952 2066 2182 2302 2424

2278 2410 2543 2685 2828

2603 2755 2909 3069 3232

3254 3444 3636 3836 4040

3905 4131 4364 4603 4848

4556 4820 5091 5370 5656

5207 5508 5818 6138 6464

5000 5 250 5 500 5790 6 000

0850 09371 10286 11242 12241

1275 1405 13.2 1666 1836

1700 1871 2057 2248 2448

2125 2343 2571 2810 3061

2550 2811 3086 3372 3672

2975 3279 3600 3934 4284

3400 3748 4114 4496 4896

4250 4685 5143 5621 6121

5100 5622 6171 6745 7345

5950 6560 7200 7869 8569

680C 7497 8228 8993 9793

6 250 6500 6750 7000 7 250

13282 14366 15492 16660 17872

1992 2155 232A 2499 2681

2656 2873 3098 3333 3576

3321 3593 3873 4'66 4468

3984 4310 4647 4996 5361

4645 5028 5422 5631 6255

5313 5746 6197 6666 7148

6641 7183 7746 8333 8935

7969 8620 9295 9998 10723

9297 10056 10845 11662 1 2510

1 0625 11493 12393 13328 1 4297

7500 7750 8 000 8 500 9 000

19125 20423 21760 24566 2745C

2867 3063 3264 3685 4131

3825 4084 4352 -913 5508

4i81 5106 5440 6 41 6885

5737 6127 6538 '370 8262

6694 7145 7616 8598 9639

7650 a169 a704 9826 1 1016

9562 10212 1 0880 1 2283 1 3-70

11475 12254 13056 1 4738 1 6525

13387 1 4297 1 5232 1 7196 1 9278

15300 16337 1 7408 19653 2 2033

Dlsplacemenl

Plunger area 23 1

. stroke

5

6

7

8


INGERSOLLRAND

Standard Hardness Conversion Tables for Steel Br~nell

Dia

Rockwell

Areas of Circles Diameters in Inches and Areas in Square Inches* Area

Dia

_

Area

I

Dia

/

Area

-

173 782 176 715 179 673, 182 655 185 h b l 188 692 191 748 194 Q28 197 933 201 062 204 216 207 395 210 59s 213.825 217 077 2?0 354 223 655 226 981 230 3 3 1 233 i 0 6 237 105 240 529 243 97; 247 45 250 94E 251 47 258 016 ? b l 5s; 265 153 "6s 803 ? i ? 44s ?ib I17 2i9 El1 ? \ 3 52'3 237 272 291 04 494 832 29'; 613 30'2 45'1 :306 355 310 445 114 16 3?? ObJ 330 064 336 164 346 361 354 657 303.051 371 543 380 134 3 5 1 S22 397 609 406 494 415 4 7 i 424 555 433 737 443 015 452 3'4 401 Sb4

* Also appller

to

I i - I Dia

Area

Dia

471 436 481 107 490 875 500 742 510 i 0 6 520 769 530 93 541 19 551 547 562 003 572 557 563 209 593 959 604 807 615 754 6?6 798 637 941 649 182 660 521 671 959 683 494 $95 128 106 86 718 69 730 618 742 645 754 i 6 9 i b 6 992 i i 9 313 i 9 1 712 hO4 25 b l b 865 629 579 842 391 655 301 b63 709 b b l 415 694 62 907 922 921 '323 934 E?? 445 42 9h? 115 975 909 9b9 9 1003 79 1017 678 1032 065 1046 349 1060 i ? ? 1075 ? I 3 I089 i 9 2 1104 409 1119 244 1134 I 1 8 1149 oas 1164 159 1179 327 1194 593

*ih

D ~ a m o n dCone Penetrator 1

C Scale 150 kg load

D Scale 100 kg load

A Scale 60 kg load

68 67 66 65 64

76 9 76 1 75.4 74 5 73.8

85.6 85 0 84 5 83.9 83 4

10 mrn Standard Ball 3000 kg load

-

-

V~ckers Diamond Pyrarn~d

940 900 865 832 800

any cnns!strn?

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