Cenrtifugal Pump Tests-Hydraulic Institute.pdf

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Hl Centrifuga! Pump Tests- 2000

1.6 Test

1.6.2.1

1.6.1

Unless otherwise specified, the rate of flow, head, efficiency, NPSHR and priming time are based on shop tests using water corrected to 20°C (68°F). lf the facility cannot test at rated speed because of limitations in power, electrical frequency or available speed changers, the pump may be tested at between 80% and 120% of rated speed . lt is permissible on pumps greater than 225 kw (300 hp) to test at speeds between 60% and 140% of rated speed.

Scope

This standard is limited to the testing of centrifuga! pumps with clear water. The tests conducted under these standards shall be made and reported by qualified personnel. This standard only applies to tests of the pump unless stated otherwise. The type of test(s) performed, and the auxiliary equipment to be used, should be agreed upon by the purchaser and manufacturer prior to the test. lt is not the intent of this standard to limit or restrict tests to only those described herein. Variations in test procedures may exist without violating the intent of this standard. Exceptions may be taken if agreed upon by the parties involved without sacrificing the validity of the applicable parts of this standard. 1.6.1.1

Objective

Test condltlons

1.6.3 Terminology The following terms are used to designate test parameters or are used in connection with pump testings:

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1.6.3.1

Symbols

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See Table 1.18.

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1.6.3.2

Subscrlpts

1.6.3.3

Specified conditlon polnt

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Specified condition point is synonymous with rated condition point. 1.6.3.4

Rated condltlon polnt

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1.6.2 Types of tests This standard describes the following tests:

1.6.3.5

a)

Normal condition point applies to the rate of flow, head, speed, NPSH and power at which the pump will normally operate. lt may be the same as the rated condition point.

Optional tests as follows when specified :

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Rated condition point applies to the rate of flow, head, speed, NPSH and power of the pump as specified by the purchase order.

Performance test to demonstrate hydraulic and mechanical integrity;

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See Table 1.19.

This standard is intended to provide uniform procedures for hydrostatic, hydraulic, and mechanical performance testing of centrifuga! pumps and recording of the test results. This standard is intended to define test procedures which may be invoked by contractual agreement between a purchaser and manufacturer. lt is not intended to define a manufacturer's standard practice.

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a.

Normal condition point

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'ft.

meter

m

feet

ft

0.3048

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dimensionless millimeter squared/sec dimensionless kilopascal kilowatt cubic meter/hour cubic meter/hour kilogram/cubic meter dimensionless degrees Celsius Newton - meter meter/second non e meter

-

mm 2/s

kPa kW m3/h m3/h kg/m 3

-

oc N-m m/s non e m

dimensionless feet squared/second dimensionless pounds/square inch horsepower cubic feet/second US gallons/minute pound mass/cubic foot dimensionless degrees Fahrenheit pound-feet feet/second non e feet

-

ft2/sec

psi hp ft3/sec gpm lbm/ft3

OF lb-ft ft/sec non e ft

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1.162 92,900 1 6.895 0.7457 101.94 0.2271 16.02 1 (°F-32) x% 1.356 0.3048 1 0.3048

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To calculate the net positive suction head available (NPSHA) to the pump in the field:

At discharge conditions: NPSHA Pd = 4715 psia;

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NPSHA = hatm+h 5 -hvp

td = 360°F

1000 --(Pa - Pvp) + h 5

= (gx p)

Pvp = 172 kPa (from steam tables)

From steam tables, Discharge specific volume .01772 ft 3/lb

y= Specific weight = 947.3 kg/m

Specific volume = 1/specific weight = 1/ythen:

Velocity in the 100-mm inside diameter suction:

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[(P.-P,l~¡)¡¡+,!s)l

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V=

= 3.2

0.1oo2 ~ 3600

= ( 4 ?lS-215)x 144 x

mis

Cl.

cr '< -1

5 3 g rJ>

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Velocity head (hv) = S

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( .01772 + .01800) = 11,570 ft 2 This value should be added to the terms : (hv - hv) and (Zd- Z 5 ) d

S

to obtain the total head.

hv = s

3.22 2 X 9.8 1 = 0.52 m

h5 = h9 + hv + Z 5 S S h 5 = 144.8x (

1000 ) +0.52-0.15 = 16.2m 947.3 X 9.81

6 Copyright© 2000 By Hydraulic lnstitute, All Rights Reserved.

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NPSHA =

1000 (98-172)+16.2 = 8.2m 9.81 X 947.3

Example: (US units) A four-stage boiler feed pump having a 4-inch inside diameter suction and a 3inch inside diameter discharge is rated at a flow rate of 400 gpm against a total head of 900 feet handling water at 240°F, and running at 3550 rpm. The suction gauge reading is 21 psig, the gauge center location is 0.5 feet below impeller inlet datum, and atmospheric pressure is 29 inches Hg. P

atm

= 29" of Hg =

29 x 13·6 = 14.2 psia 12 2.31

NOTE: specific gravity of mercury = 13.58 and

pressure of the liquid in head of liquid pumped, required to prevent more than 3% loss in total head from the first stage of the pump at a specific rate of flow. 1.6.3.13

Power (P)

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367

X (

18000)

1000 x 1.1=1100 gpm max;

250 x 30.5 = 26 kW max; 367 4)

X (

1000 x 1.0=1 000 gpm min;

18000)

Test power at rated total head and rpm =

Pw

(~)

227 x 1.05 = 238 m3/h max;

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(3960)( 18000)

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Test max power at rated total head and rpm =

(1100)(100) = 34.7 hp max;

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(3960)( 18000)

30.5 = 25 .7 kW;

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367(76.9) 100

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Test min power at rated total head and rpm = 30.5 = 22.4 kW;

367(-ªº-) 100

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and:

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(1000)(100) = 31 .6 hp min;

227 x .95 = 216 m 3/h min;

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Test rate of flow range :

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Per Para e, level B at rated total head and rpm.

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Per Para e, level B at rated total head and rpm . Test rate of flow range: 1000 x 1.05 = 1050 gpm max; 1000 x .95 = 950 gpm min;

10 Copyright© 2000 By Hydraulie lnstitute, All Rights Reserved.

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Heat exchanger, if required ---1---.J

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Return lo sump

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Discharge

Figure 1.117 -

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Note: Position of these devices may be reversed in sorne set ups.

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Open or closed tank

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g) Throttling devices may be used for the suction and discharge instruments, such as needle valves or capillary tubes to dampen out the pressure pulsations; h) A means for measuring input power to the pump shall be provided and be suitable for measuring the complete range of power; i) A means for measuring pump speed shall be provided ; j) Test setups intended for NPSH testing shall be provided with a means for lowering the suction pressure to the pump, such as a suction throttle valve (with optional screen or straightening vanes) , variable level sump in an open system, or a closed tank with a mechanism to create a vacuum or pressure;

k) A means for measuring the temperatura of the test liquid shall be provided; 1) The actual dimensions of the suction and discharge pipes where pressure readings are to be taken shall be determinad so that proper velocity head calculations can be made; m) Flow measuring device(s).

1.6.5.6

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Performance test data requirements

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The following data shall be obtained prior to the test run and written for the record to be retained for two years (see sample data sheet on page 14): a)

Record of pump type , size and serial number;

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01 = n = (H1)0.5 = (p1 )0.333 = (NPSHR ) 0.5

OH(s ) Pw = 3960

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n2

02

lf pump output is measured in pounds per square inch, the formula for output power, regardless of the specific weight of the liquid , becomes:

H2

P2

NPSHR2

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Where :

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rate of flow on test;

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rate of flow on installation ;

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speed on test in rpm ;

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1710

Calculation of efficlency

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n2 The pump efficiency expressed in percent is calculated by:

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speed on installation in rpm ;

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= o2 [~:J = 90.8[~~;~] = 75.5 m3 /h

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Power on installation in kW (bhp);

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EC1

Eddy current losses on test in kW (bhp).

Eddy current losses, EC 1, are normally meas ured by manufacturers during development studies. Values from these tests may be used in lieu of measurements during the contractura! performance test.

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since:

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Performance test correction to rated

For purposes of plotting, the rate of flow, head and power shall be corrected from the test values at test speed to the rated speed of the pump. The corrections are made as follows: Rate of flow:

Head:

02 =

n2]2

H2 = [ n1

[~~ J0 1

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Any reduction in specific weight , as caused by an increase in temperatura , results in a directly proportional reduction in output and input power; therefore, the efficiency is not changed. Reduced viscosity of water at increased temperatura will have an influence on efficiency. For pumps in the lower range of specific speed typically below 1750 (1500) , such as high pressure, multi-stage boiler feed pumps and large, single-stage hot water circulating pumps, reduced viscosity will :

11ot = 1- (0.2)( .868 ) , 11ot = .826 = 82.6%

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11ot = 1- ( 1-11 t )(vo V t) x , t

increase the interna! leakage losses;

11 ot = 1 - ( 1 - .80)( .00000185) 0.1 .0000076 •

reduce disc friction losses;

11ot = 1- (0.2)( .868 ),

reduce hydraulic skin friction or flow losses.

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11ot

= .826 = 82.6%

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Pressure Gauge

(1)

Dampening Valve

Thermometer Control Valve for Throttling Suction

Dampening Device

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Flow Meter if Located in Discharge

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Constant Level

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Straightening Vanes Booster Pump may be lnstalled if additional suction pressure is required

Return to sump

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Discharge

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Discharge Control Valve, or '---Adjustable Spring Loaded Back Pressure Valve or Adjustable Choke Valve Heat exchanger, if required

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Note: Position of these devices may be reversed in sorne setups.

Suppression type NPSH test with constant level sump 19

Copyright© 2000 By Hydraulic lnstitute, All Rights Reserved .

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Hl Centrifuga! Pump Tests- 2000

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a.

of straight pipe to straighten flow. This arrangement dissipates the turbulence produced by the throttle valve and makes possible an accurate reading of suction pressure at the pump inlet. This simple arrangement usually is satisfactory for NPSHR greater than 3 meters (1 O feet), although the turbulence at the throttle valve tends to accelerate the release of dissolved air or gas from the liquid which takes place as the pressure on the liquid is reduced. A test made with this arrangement usually indicates higher NPSHR than that which can be expected with deaerated liquid. In the second arrangement, Figure 1.120, the pump is supplied from a sump in which the liquid level can be varied to establish the desired NPSH. This arrangement provides an actual suction lift and hence more nearly duplicates operating conditions of pumps on water service. Care should be taken to preven! vortexing as liquid level is varied. The priming connection should be installed above the eye of the impeller either in the suction pipe or on the pump.

3

release of air or gas. This arrangement more nearly duplicates service conditions where a pump takes its supply from a closed vessel at or near its vapor pressure. lt is also acceptable to test with a closed loop without the closed tan k on the suction side.

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In each of these arrangements, water shall be used as the test liquid. Aeration shall be minimizad by taking the following precautions:

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submerged return lines;

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6 reservoir sized for long retention time to allow air to escape; inlet line properly located to preven! vortexing ; reservoir baffles to isolate inlet from return line; tight pipe joints and stuffing boxes to guard against air leakage into the system.

1.6.6.3

NPSHR test procedure

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In the third arrangement, Figure 1.121, the pump is supplied from a closed tank in which the level is held constan! and the NPSHA is adjusted by varying the air or gas pressure over the liquid, by varying the temperatura of the liquid, or by varying both . This third arrangement tends to strip the liquid of dissolved air or gas. lt gives a more accurate measurement of the pump performance uninfluenced by the

The cavitation characteristics of a pump can be determinad by one of the following procedures:

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Using one of the test arrangements shown, the pump is run at constan! rate of flow and speed with the suction condition varied to produce cavitation . Plots of head shall be made for various NPSH values.

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Gas Pressure

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Priming connection

Discharge

Remainder of system same as Figure 1.117 } or 1.119

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Distributor

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Figure 1.120- Level control NPSH test with deep sump supply

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Water level variance Optional baffle: spacing between suction and discharge pipes is to be equal lo or greater !han 6 times the sum of the nominal pipe diameters. When spacing mus! be reduced, a baffle as shown is required .

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Heating or Cooling Coil

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Flow

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Suction

Discharge

Figure 1.121- Vacuum and/or heat control NPSH test with closed loop

20 Copyright© 2000 By Hydraulic lnstitute, All Rights Reserved.

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As NPSHA is reduced, a point is reached where the curves break away from a straight-line trend, indicating a condition under which the performance of the pump may be impaired. The degree of impairment will depend upon the specific speed, size and service of the pump. Figure 1.122 shows results typical of a test for NPSH at flow rates both greater and less than normal. The 3% drop in head is the standard to determine NPSHR . Another technique for determining the NPSH characteristics is to hold the speed and suction head (h 5 ) constant and to vary the rate of flow. For any given suction head, the pump head may be plotted against rate of flow. A series of such tests will result in a family of curves, as shown in Figure 1.123. Where the curve for any suction head (h 5 ) breaks away from the envelope by 3%, NPSHR is established.

NPSHR characteristics. The relationship between model results and predicted full-size characteristics is described in Section 1.6.13. Accurate determination of the cavitation point requires careful control of all factors which influence the operation of the pump. A mínimum of five test points bracketing the point of change shall be taken, and the data plotted to determine when the performance breaks away from that with excess NPSHA. Any change in performance, either a deficiency at a given rate of flow, or change in sound or vibration, may be an indication of cavitation. But because of the difficulty in determining just when the change starts, a drop in head of 3%, which is the standard value in determining NPSHR, is accepted as evidence that cavitation is present. The 3% head drop is based on the first stage head for multi-stage pumps.

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When it is impractical to conduct a test to the above criteria on large pumps due to size, rate of flow or facility NPSHA, a model test may be used to determine

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NPSHR values

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The NPSHA value required to properly establish the non-cavitating performance of a pump should be determined from prior full-scale or model tests of the specific pump in question. if no such prior test results are available, a recommended NPSHA value of twice the predicted NPSHR, for rated flow rates greater than 85% of the best efficiency point, oran NPSHA value of at least two and a half times the NPSHR, for rated flow rates below 85% of the best efficiency point, is recommended for maximum assurance. lt should be noted that the average pump will give full performance at NPSHA values only 1.3 times the NPSHR value at flow rates above 85% of the best efficiency point and 1.7 times the NPSHR value at flow rates below 85% of the best efficiency point. Accordingly, the test performed at constant rate of flow, as shown in Figure 1.124, should begin with the non-cavitating performance NPSHA value established above, or greater.

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Figure 1.122 -

NPSH test with rate of flow held constant

NPSHR values 3% reduction in total head

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1h 1,, 2 1h3 1hJ h5 1

When testing with water, an accurate temperatura measurement usually is sufficient to establish the vapor pressure, but the degree of aeration of the water may have a considerable influence on performance. Consistent results are more readily obtained when the water is deaerated. Cases may arise in which the limitations of the factory test facilities may preclude the securing of sufficient NPSHA to produce the installation NPSHA. In such cases, the NPSHR can be obtained by an increase in the pump speed with a corresponding increase in pumping head and flow rate instead of by a reduction in NPSH available:

Rate of flow Figure 1.123- NPSH test with suction head held constant

a) Correction to specified speed for net positiva suction head (NPSH):

21 Copyright© 2000 By Hydraulic lnstitute, All Rights Reservad.

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2)2 NPSH1 ,

lf the manufacturer can demonstrate that, with a given pump under particular conditions, an exponent different than the square of the speed exists, such exponent may be recognized and used accordingly.

n NPSH2 = ( n

1

02

=

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1.6.6.4

NPSHR test suctlon condltlons

Where:

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NPSH1 = Net positive suction head at test speed; NPSH2 = Net positive suction head at specified speed ;

n1 =Test speed in rpm ;

The total suction head is to be determined as specified in Section 1.6.3.12.4. The NPSHA on the test stand shall exceed the NPSHR of the pump with sufficient margin throughout the operating range to ensure that it will have no effect on the pump performance. See Section 1.6.3.12.1O for a description of NPSHA.

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n2 = Specified speed in rpm ;

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0 1 = Test rate of flow;

0 2 = Rate of flow at specified speed; b) NPSH law.

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The affinity relationships define the manner in which head , rate of flow, input power, and NPSHR vary in a centrifuga! or axial flow pump with respect to speed changes. lf a pump operates at or near its cavitation limit, other factors also have an effect, and the limiting NPSHR value may vary other than as the square of the speed. Sorne of these factors are: thermodynamic effect on the vapor pressure of the liquid, change in surface tension, and test differences due to the relative air content of the liquid.

For pumps in free-surface systems, the approach must be free of obstructions. The flow towards the pumps must be uniform and free of eddies and vortices. lntake structures should be designed as described in the ANSI/HI 9.8-1998, Pump lntake Design. 1.6.6.5

NPSHR test records

Complete written or computer records of all data relevant to the NPSHR tests shall be kept by the test facility and available to the purchaser for a minimum of two years (see sample data sheet on page 14).

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This information should include:

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Specified NPSHR and NPSHA;

b)

Height of suction gauge, above or below the datum line;

e)

lnside diameter of pipe at location of suction pressure tap ;

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At rates of flow 85% 2.5 x NPSH R

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or less of BEP

d) Observed data (each run);

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2 x NPSHR

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NPSHA

NPSH test at constan! rate of flow Recommended NPSHA range for NPSHR test when no previous data on pumps full performance is available.

Figure 1.124 -

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At rates of flow

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NPSH test with flow rate held constant

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shaft speed;

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discharge pressure;

-

rate of flow.

e) Type of test setup;

22 Copyright© 2000 By Hydraulic lnstitute, All Rights Reserved.

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Hl Centrifuga! Pump Tests- 2000 f) Type of flow meter and calibration; g) Type, number and calibration of pressure gauges;

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d) Oil temperature, when oil sump is used.

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Mechanical test operating condltlons

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Note any abnormal observation (noise, vibration, etc.);

The mechanical test shall be conducted under the following operating conditions:

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ldentification of materials at liquid end of pump;

j) Type and serial number of pump and driver; k)

a) Shaft speed- as required to meet rated conditions as specified in the customer's order. Facility 60 or 50 hertz speeds may be used when customers hertz are not available, or as agreed to by customer.

Date of test; b)

1) ldentity of personnel in charge.

1.6.6.6

Rate of flow - the rated rate of flow for which the pump is sold, or as adjusted to a speed other than contract by Section 1.6.5.8.8.

Report of NPSHR test

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Ambient air temperature.

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Mechanical test objective 1.6.7.4.1

To demonstrate the satisfactory mechanical operation of a pump, at the rated conditions, including: vibration levels; lack of leakage from shaft seals, gaskets, and lubricated areas; and free running operation of rotating parts. When specified, bearing temperature stabilization will be recorded.

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d} Liquid temperature - at ambient condition.

1.6.7.4 1.6.7.1

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e) Suction pressure- as available from the test facility. All parties to the test shall be furnished a copy of the NPSHR curve or curves as described in Section 1.6.6.3.

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Vibration

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Vibration instruments can be either hand held or rigidly attached to the pump. The sensor(s) shall be velocity type designed to read the nominal RMS velocity without filtering to specific vibration frequencies. Readings can be taken manually or with recording instruments.

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These tests do not apply to submersible pumps as described in ANSI/H 1 1.1-1.2-2000 Figures 1.7 and 1.8 . References to shaft seal do not apply to sealless pumps.

1.6.7.2

Mechanical test setup

The test setup shall conform to the requirements of Section 1.6.5.5 where applicable, and the test liquid shall be clear water. In addition, instrumentation shall be added to measure the following:

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Temperature instruments can be any recognized temperature sensor such as pyrometers, thermometers, thermocouples and the like. They shall be capable of measuring the metal temperature on the outside of the housing of both bearings, and may be hand held or rigidly attached to the bearing housing. The top center over the bearing is usually the location of the highest temperature. Where temperature sensors are built into the pump, they shall be used instead of sensors on the bearing housing. lf built-in, they must be at a location where temperature is of interest.

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The pump rate of flow and suction pressure shall be set per Section 1.6.7.3. The pump shall be operated for a minimum of 1O minutes, and the following observations made and data recorded: a)

Leakage from shaft seals, gaskets, mechanical seal piping, and bearing housing(s).

23 Copyright© 2000 By Hydraulic lnstitute, All Rights Reserved.

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Vibration leve! at both inboard and outboard bearings, in two directions perpendicular to the shaft plus the axial direction. Only the nominal RMS velocity values need be recorded . Refer to the latest Hl Standard for acceptable values.

e) Bearing temperatures at both inboard and outboard bearings shall be recorded. When specified, the pump shall be operated until the bearing temperature stabilizes. See ANSI/HI 1.4-2000, Centrifuga/ Pumps, Section 1.4.5.2.3, for the temperature stabilization procedure. d)

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Rubbing of rotating parts shall be checked for by listening for unusual or excessive noise, and observing the coast down of the pump when power is cut off. Torque readings or other changes in similar instrument readings can also indicate rubbing . Liquid temperature and ambient air temperature shall be taken manually or with recording instruments .

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piping, bearing housing, etc. Minor leakage at pump suction and discharge flanges shall not be cause for rejection since these joints are disconnected and reconnected in the field .

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Mechanical test acceptance levels Leakage from the pump as observed at the following:

The mechanical performance is considered acceptable when each of the following is achieved:

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Vibration levels on both bearings in any direction do not exceed the allowable limits specified in or as specified on the order document.

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b) Temperature of both bearings' housing surface does not exceed the pump manufacturer's standard for the product as established prior to test. e) Mechanical seals may have an initial small leakage, but shall have no visible leakage when running at test operating conditions for a minimum of 1O minutes. When shut down, there shall be no visible leakage from seals for five minutes with the test suction pressure applied. The purpose of this test is to ensure that the entire seal (cartridge) has been properly installed. Soft packing shall have no more than 12 drops per minute leakage for a 25-mm (1-inch) shaft up to 3500 rpm . For larger shafts or higher test speeds and pressures, allowable leakage shall be increased proportionately with shaft diameter speed and pressure or as agreed to by the purchaser. There shall be no visible leakage through pressure containment parts, gaskets, seal recirculation

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Any flow measuring system may be used for measuring pump rate of flow. However, it must be installed so that the entire flow passing through the pump also passes through the instrument section so that the instrument can measure rate of flow with an accuracy of ± 1.5% at BEP.

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Rate of flow instruments are classified into two functional groups. One group primarily measures batch quantity; the other primarily measures rate of flow.

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Measurement of rate of flow by volume is done by measuring the change in volume of a tank or reservoir during a measured period of time. The tank or reservoir can be located on the inlet or discharge side of the pump, and all flow into or out of the tank or reservoir must pass through the pump. In establishing reservoir volume by linear measurements, considerations shall be given to the geometric regularity (flatness, parallelism , roundness, etc.) of the reservoir surfaces, dimensional changes due to

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thermal expansion or contraction, or deflection resulting from hydrostatic pressure of the liquid.

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Liquid levels shall be measured by means such as hook gauges, floats and vertical or inclined gauge glasses.

The pipe for one diameter preceding the upstream pressure taps shall be free from tubercles or other surtace imperfections which would establish a local disturbance in line with these openings. The pressure tap opening shall be flush with the interior of the pipe or meter element as appropriate and shall be free of burrs (see Figures 1.126 and 1.127).

In sorne locations and under sorne circumstances, evaporation and loss of liquid by spray may be significant and may be greater than the effects of thermal expansion or contraction. Allowance for such loss must be made, or the loss prevented.

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Measurement of rate of flow by head meters is done by introducing a reduced area in the flow stream which results in a reduction in gauge head as the velocity is increased. The gauge head differential is measured and used to determine the rate of flow. The meters discussed in Sections 1.6.9.4.1, 1.6.9.4.2 and 1.6.9.4.3 use this principie.

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Abrasion, 9.1-9.5: 11 severe, 9.1-9.5: 15 Abrasion resistant cast irons, 9.1-9.5: 19 Acceleration head, 6.1-6.5: 25-27, 8.1-8.5: 12 Acceleration pressure, 6.1-6.5: 25-27, 8.1-8.5: 12 Accessory equipment, 3.1-3.5: 41-44 Accumulator, 9.1-9.5: 3 Acoustical calibration, 9.1-9.5: 50 Actuating mechanism See Valve gear Additives in liquid, 9.6.1: 4 Adhesivas, 9.1-9.5: 26 Adjustment factors for alternate designs, 3.1-3.5: 42t. Affinity laws, 1.6: 16, 11.6: 28 Air entrainment, 4.1-4.6: 20 Air gap, 4.1-4.6: 7, 5.1-5.6: 12 Airborne noise, 3.1-3.5: 28 Airborne sound measurement, 9.1-9.5: 50 6 dB drop-off, 9.1-9.5: 50 acoustical calibration, 9.1-9.5: 50 averaging of readings, 9.1-9.5: 52 A-weighted sound level, 9.1-9.5: 50, 51, 52 background sound level and corrections, 9.1-9.5: 52, 54 f. calculation and interpretation of readings, 9.1-9.5: 52 caution (extraneous noise), 9.1-9.5: 51 data presentation, 9.1-9.5: 52 graphic plot, 9.1-9.5: 52 instrumentation, 9.1-9.5: 50 measurements and technique, 9.1-9.5: 51 microphone locations, 9.1-9.5: 50, 51 ,54f.-60f. microphone system, 9.1-9.5: 50 octave-band analyzer, 9.1-9.5: 50 octave-band sound pressure levels, 9.1-9.5: 50, 51, 52 operation of pumping equipment, 9.1-9.5: 50 primary microphone location, 9.1-9.5: 51 recorders, 9.1-9.5: 50 reference sound source, 9.1-9.5: 50 sound level meter, 9.1-9.5: 50 test data tabulation, 9.1-9.5: 52 test environment, 9.1-9.5: 50 test reports, 9.1-9.5: 52, 53f.

Alarm limit (defined), 9.6.5: 2 Alignment, 3.1-3.5: 36, 37f. and elevated temperaturas, 3.1-3.5: 38 Alignment (horizontal pumps) angular, 1.4: 3, 3f. and coupling guard, 1.4: 5 dial indicator method, 1.4: 4, 4f. final, 1.4: 6 of full pump, 1.4: 6 of gear type couplings, 1.4: 4, 5f. laser method, 1.4: 4 leveling pump and driver, 1.4: 2 misalignment causes, 1.4: 13 parallel, 1.4: 3, 3f. shaft and coupling, 1.4: 3 of spacer type couplings, 1.4: 5, 5f. of special couplings, 1.4: 5 straightedge method, 1.4: 3 and thermal expansion, 1.4: 7 of v-belt drive, 1.4: 5 Alignment (vertical pumps), 1.4: 9 misalignment causes, 1.4: 13 All bronze pumps, 9.1-9.5: 16, 17 All iron pumps, 9.1-9.5: 16, 17 All stainless steel pumps, 9.1-9.5: 16, 17 Alleviator, 9.1-9.5: 3 Allowable operating range, 1.1-1.2: 58,2.1-2.2:22 Allowable operating region, 9.6.3: 1 centrifuga! pumps, 9.6.3: 5, 5f., 6f., ?f. factors affecting, 9.6.3: 1 large boiler feed pumps, 9.6.3: 8 vertical turbine pumps, 9.6.3: 8, 8t. Alnico, 4.1-4.6: 8, 5.1-5.6: 14 Aluminum and aluminum alloys, 9.1-9.5: 22 Aluminum bronze, 9.1-9.5: 21 American National Metric Council, 9.1-9.5: 7 American Society for Testing and Materials, 9.1-9.5: 11 Angular misalignment, 3.1-3.5: 36, 37, 37f., 38 ANSI/ASME 873.1M, 9.6.2: 1, 3, 4, 5t., 6t., ?t. 1.5x1-8 CF8M (Type 316) pump combinad axis deflection evaluation, 9.6.2: 25 derating loads, 9.6.2: 22 individual nozzle load evaluation, 9.6.2: 22

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Bearing failure mode causes and indicators, 9.6.5: 18, 21t. Bearing life, 9.6.3: 2 Bearing lubrication comparison of stabilization temperatura with manufacturer's standards, 1.4: 12 measurement of operating temperatura, 1.4: 11 , 12f. rolling element bearings, 1.4: 11 sleeve and tilting pad bearings, 1.4: 11 sleeve bearings, 1.4: 12 temperatura vs. time, 1.4: 12 Bearing materials, 4.1-4.6: 15 Bearing wear monitoring, 9.6.5: 14 acoustic detection, 9.6.5: 15 bearing materials and characteristics, 9.6.5: 14 carbon bearing wear characteristics, 9.6.5: 14 contact detection, 9.6.5: 15 contact or continuity switch, 9.6.5: 15 controllimits, 9.6.5: 15 frequency. 9.6.5: 15 indicators, 9.6.5: 24 means, 9.6.5: 14 power monitor, 9.6.5: 15 silicon carbide bearing wear characteristics, 9.6.5: 14 temperatura pro be, 9.6.5: 15 vibration sensor, 9.6.5: 15 wear detection methods, 9.6.5: 14 Bearings adjusted rating life , 1.3: 74, 75 axial load, 1.3: 74 basic dynamic radial load rating , 1.3: 74 basic rating life, 1.3: 74 dynamic equivalent radial load, 1.3: 7 4 externa! , 5.1-5.6: 19 grease, 1.3: 65 housing closures, 1.3: 70 impeller mounted between, 1.3: 58 , 72f. impeller overhung from, 1.3: 58, 70, 71f. interna!, 5.1-5.6: 18 labyrinths, 1.3: 70 life, 1.3: 74 lubrication, 1.3: 65-67 oil lubrication , 1.3: 65 operating temperatura, 1.3: 75 product lubrication, 1.3: 66t.. 67 radial load , 1.3: 74 rating life , 1.3: 74 reference and source material, 5.1-5.6: 38 reliability , 1.3: 74 rolling element, 1.3: 64, 64t. sleeve, 1.3: 64 types, 1.3: 64 BEP See Best efficiency point

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11.6: 3 Body, 3.1-3.5: 4, 9.1-9.5: 3 Boiler circulating pumps, 1.3: 1O Boiler feed booster pumps, 1.3: 9 Boiler feed pumps, 1.3: 8 Bolt-proof load, 5.1-5.6: 15 Booster service, 1.3: 1, 2.3: 1 Bowl assembly efficiency, 2.1-2.2: 23, 2.6: 7 calculation, 2.6: 16 Bowl assembly input power, 2.1-2.2: 23, 2.6: 7 Bowl assembly output power, 2.6: 7 Bowl assembly performance test, 2.6: 11 , 11f. Bowl assembly total head, 2.1-2.2: 22, 2.6: 6 calculation , 2.6: 15 measurement, 2.6: 29f., 29

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Brass leaded red, 9.1-9.5: 20 yellow, 9.1-9.5: 20 Bronze all bronze pumps, 9.1-9.5: 16, 17 aluminum, 9.1-9.5: 21 leaded nickel bronze, 9.1-9.5: 21 silicone, 9.1-9.5: 20 specific composition bronze pumps, 9.1-9.5: 16, 17 tin , 9.1-9.5: 20 Bronze fitted pumps, 9.1-9.5: 16, 17 Building services pumping systems, 9.6.1: 9 Bull ring packing, 6.1-6.5: 63, 63f. Burst disc (rupture), 9.1-9.5: 3 Bushings, 1.4: 6 Bypass, 1.4: 13 Bypass piping, 9.1-9.5: 3

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Direct acting (steam) pump materials, 9.1-9.5: 18 Direct acting (steam) pumps defined, 8.1-8.5: 1 double-acting pump, 8.1-8.5: 1 duplex pump, 8.1-8.5: 2 horizontal pump, 8.1-8.5: 1 inspection, 8.1-8.5: 22 nomenclatura, 8.1-8.5: 3 piston pump, 8.1-8.5: 1f., 2 simplex pump, 8.1-8.5: 2, 2f. types, 8.1-8.5: 1, 1f. typical services, 8.1-8.5: 12 vertical pump, 8.1-8.5: 1 Direction of rotation , 3.1-3.5: 5 Dirty liquids, 5.1-5.6: 24 Discharge, 3.1-3.5: 33 insufficient, 2.4: 15 lack of, 2.4: 15 Discharge flow, 5.1-5.6: 36 Discharge piping , 2.4: 4, 6.1-6.5: 45, 46f. See also Piping , Suction piping air release valves , 2.4: 5 lining up, 2.4: 3 reducers , 2.4: 4f., 5 siphons, 2.4: 6 supports, anchors, and joints, 2.4: 4 valves , 2.4: 5, 6f. Discharge port, 3.1-3.5: 4, 9.1-9.5: 4 Discharge pressure, 8.1-8.5: 7 Discharge recirculation , 1.3: 43 Discharge valve position, 1.4: 12 Disk couplings, 1.3: 68 Displacement, 3.1-3.5: 14, 3.6: 2, 6.1-6.5: 20, 8.1-8.5: 7 Displacement type meters, 6.6: 13 Dissolved gases, 3.1-3.5: 19, 21f. Double suction pump specific speed , 1.3: 32, 35f., 36f. Double volute casing See Dual volute casing Double-acting pump, 6.1-6.5: 1, 2f., 3f. Dowelling , 1.4: 13 Draining, 5.1-5.6: 18 Drains, 8.1-8.5: 23 Orive (steam) cylinder, 8.1-8.5: 4 Orive (steam) end , 8.1-8.5: 3, 5f. lubrication , 8.1-8.5: 15, 23 Orive (steam) piston, 8.1-8.5: 4 Orive characteristics , 4.1-4.6: 17 Orive shaft, 1.3: 67 Orive specification , 3.1-3.5: 24 Driven component liner, 5.1-5.6: 14 Driver mounting , 3.1-3.5: 34 Driver sizing, 5.1-5.6: 25 Drivers, 1.3: 76, 2.3: 45 deceleration devices , 1.3: 77 , 2.3: 45 electric motors, 1.3: 77, 2.3: 45

engines, 1.3: 77 gears, 2.3: 45 magnetic, 1.3: 77 mounting and alignment, 2.4: 6 non-reversa ratchets, 2.3: 46 pre-lubrication, 2.4: 8 pump-to-driver shafting, 2.3: 46 steam turbina , 1.3: 77 thrust bearings, 2.3: 46 variable speed, 1.3: 77, 2.3: 45 Dry critica! speed, 9.6.4: 2 Dry vacuum test, 1.6: 25 Dual volute casing, 1.3: 58 , 59f., 76 K versus rate of flow , 1.3: 58, 59f. Ductile iron, 9.1-9.5: 18 Duplex pump, 6.1-6.5: 2 Duplex stainless steels, 9.1-9.5: 20 Duplicate performance pump, 1.1-1.2: 25 , 2.1-2.2: 3 Duplicate pump, 2.1-2.2: 3 Duty cycle, 3.1-3.5: 24 Dynamic analysis report, 9.6.4: 4, 5 Dynamic balance , 5.1-5.6: 20 Dynamic balancing , 1.1-1.2: 61 Dynamometers, 1.6: 30, 3.6: 18, 9.1-9.5: 3 calibration, 1.6: 31

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neodymium, 5.1-5.6: 14 outer magnet ring, 5.1-5.6: 14 pole (N-S), 5.1-5.6: 14 precautions, 5.1-5.6: 32 rows of magnets, 5.1-5.6: 14 samarium cobalt, 5.1-5.6: 14 separately coupled, 5.1-5.6: 2, 7f. shipping precautions, 5.1-5.6: 32 slip, 5.1-5.6: 14 vertical submerged, 5.1-5.6: 2, 9f. Magnetic drives, 1.3: 77 Magnetic Material Producers Association, 4.1-4.6: 23 Magnetic materials, 4.1-4.6: 8 Magnetic slip, 4.1-4.6: 9 Magnets, 5.1-5.6: 14 assembly, 4.1-4.6: 12 assembly caution, 4.1-4.6: 21 cautions, 4.1-4.6: 19, 21,22 component temperature, 5.1-5.6: 26 demagnetization, 4.1-4.6: 20 handling cautions, 4.1-4.6: 22 humidity effects, 4.1-4.6: 21 installation and safety considerations, 4.1-4.6: 19 permanent, 4.1-4.6: 8 shipping, 4.1-4.6: 19 temperature limits, 4.1-4.6: 20, 5.1-5.6: 26 Main drive (steam) slide valve, 8.1-8.5: 4 Main drive (steam) valves, 8.1-8.5: 4, 6f. setting (duplex pumps), 8.1-8.5: 22 setting (simplex pumps), 8.1-8.5: 23 Maintenance, 2.4: 14, 4.1-4.6: 21-22, 5.1-5.6:32, 35 access, 1.4: 1, 2.4: 2 canned motor, 5.1-5.6: 35 close running fits, 5.1-5.6: 35 examination of wear patterns, 5.1-5.6: 36 excessive power consumption, 1.4: 16 inspections, 5.1-5.6: 35 insufficient discharge flow or pressure, 1.4: 16 little or no discharge flow, 1.4: 16 loss of suction, 1.4: 16 magnet assembly, 5.1-5.6: 35 mechanical seals, 3.1-3.5: 46 noise, 1.4: 15 packing, 3.1-3.5: 46 parts replacements , 2.4: 14 preventive, 3.1-3.5: 45 spare parts, 3.1-3.5: 46 troubleshooting, 1.4: 15, 2.4: 15 wear plates, 1.4: 15 wear rings, 1.4: 15, 2.4: 14 Maintenance inspection, 9.6.5: 12 characteristics to consider, 9.6.5: 12 coupling flexible elements inspection, 9.6.5: 12 erosion inspection, 9.6.5: 13 frequency, 9.6.5: 13

13 Copyright© 2002 By Hydraulic lnstitute, All Rights Reserved.

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Overhung impeller pumps (continued) separately coupled single stage-centerline mounted-pump on base plate, 1.1-1.2: 42fo separately coupled single stage-centerline supportAPI 610, 1.1-1.2: 12fo separately coupled single stage-frame mounted, 1.1-1.2: 10fo separately coupled single stage-frame mountedANSI 873 01, 1.1-1.2: 13fo separately coupled single stage-frame mountedlined pump, 1.1-1.2: 11fo separately coupled single stage-frame mountedmixed flow, 1.1-1.2: 21fo separately coupled single stage-frame mountedself-priming, 1.1-1.2: 24fo separately coupled single stage-in-line-flexible coupling, 1.1-1.2: 8f o separately coupled single stage-in-line-rigid coupling, 1.1-1.2: 9fo separately coupled single stage-wet pit volute, 1.1-1.2: 14f. separately coupled-single stage-frame mounted (vertically mounted), 1.1-1.2: 47fo separately coupled-single stage-frame mountedpump on base plate, 1.1-1.2: 40f. p See Pressure P See Power Pmot See Submersible motor input power Pp See Pump input power Pw See Pump output power Pace See Acceleration pressure Pb See Barometric pressure Pba See Bowl assembly input power Pd See Discharge pressure Pd See Outlet pressure Pd See Total discharge pressure Pd See Working pressure p1 See Friction loss pressure p9 See Gauge pressure PH See Total differential pressure Pmot See Electric driver input power Pmot See Electric motor input power Pmot See Total input power Pp See Pump input power Ps See lnlet pressure Ps See Suction pressure Ps See Total suction pressure Pv See Velocity pressure Pw See Pump output power Pwba See Bowl assembly output power Pz See Elevation pressure Pacemakers (precautions), 5.1-5.6: 32 Pacemakers and magnets, 4.1-4.6: 19 Packed stuffing-box, 1.3: 69, 69f o, 70f o

Packing, 3.1-3.5: 5, 46, 9.1-9.5: 4 allowance for expansion, 8.1-8.5: 16 basis of recommendations, 8.1-8.5: 17 canvas, 8.1-8.5: 17 chemical, 8.1-8.5: 17 clearance, 8.1-8.5: 18 drip, 8.1-8.5: 17 fitting, 8.1-8.5: 18, 18fo gland adjustment, 8.1-8.5: 16 hydraulic packing, 8.1-8.5: 17 installation, 8.1-8.5: 15 lubrication, 8.1-8.5: 17 molded ring, 8.1-8.5: 17 soaking, 8.1-8.5: 18 swelling, 8.1-8.5: 18 Packing box, 9.1-9.5: 4 Packing gland, 9.1-9.5: 4 Paper stock, 1.3: 15 See also Pulp and paper applications Parallel misalignment, 3.1-3.5: 36, 37, 37fo Parallel operation, 1.4: 14, 2.4: 12 Parallel operation and rate of flow, 2.3: 17, 17fo Parasitic losses, 5.1-5.6: 12 Partially suspended solids, 9.1-9.5: 5 Particles, 4.1-4.6: 14 Parts, 2.1-2.2: 3, 6fo-12fo alphabeticallisting, 2.1-2.2: 14t.-18t. maintenance review, 4.1-4.6: 21 names of, 4.1-4.6: 5t.-6t. Parts replacements, 2.4: 14 PATs See Pumps as turbines Percent accumulation, 3.1-3.5: 5 Percent overpressure, 3.1-3.5: 5 Percent regulation, 3.1-3.5: 5 Percent solids by volume, 6.1-6.5: 27, 9.1-9.5: 5 Percent solids by weight, 6.1-6.5: 27, 9.1-9.5: 5 Performance and selection criteria, 1.3: 21 Performance test, 1.6: 9, 2.6: 1, 9, 6.6: 1 acceptable deviation of dependent test quantities from specified values, 3.6: 7 acceptable deviation of independent test quantities from specified values, 3.6: 6 acceptable instrument fluctuation , 6.6: 6 acceptance, 3.6: 6, 6.6: 5 acceptance criteria, 2.6: 9 acceptance levels, 1.6: 9 acceptance tolerances, 1.6: 9, 2.6: 9 acceptance values, 6.6: 6 accuracy, 3.6: 7 bowl assembly, 2.6: 11, 11fo calculation of bowl assembly efficiency, 2.6: 16 calculation of bowl assembly total head, 2.6: 15 calculation of efficiency, 2.6: 15, 6.6: 9 calculation of inlet or suction pressure, 6.6: 9 calculation of input power, 6.6: 9

18 Copyright© 2002 By Hydraulic lnstitute, All Rights Reservedo

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calculation of outlet or discharge pressure, 6.6: 9 calculation of output power, 6.6: 9 calculation of overall efficiency, 2.6: 16 calculation of pump efficiency, 2.6: 16 calculation of pump input power, 2.6: 15 calculation of total differential pressure, 6.6: 9 calculation of total discharge head, 2.6: 13 calculation of total head, 2.6: 15 calculations, 1.6: 15, 3.6: 11, 6.6: 9 calculations of pump output power, 2.6: 15 calculations of total suction head, 2.6: 13 calibration interval for instruments, 1.6: 11, 12t. correcting for solids in suspension, 2.6: 18 correcting for specific weight variations, 2.6: 18 correcting for speed variations, 2.6: 17 correcting for viscosity variations, 2.6: 18 correction for solids in suspension, 1.6: 19 correction for temperature variations, 1.6: 18 correction for viscosity, 6.6: 1O correction for viscosity variations, 1.6: 19 correction to rated speed, 1.6: 17, 6.6: 10 data requirements, 1.6: 13, 2.6: 13, 14f. data sheet, 6.6: 7, 8f. differential pressure formulas, 3.6: 11 efficiency calculation, 1.6: 16 efficiency formulas, 3.6: 11 fluctuation, 3.6: 7 fluctuation and accuracy, 2.6: 11 t. at increased speed, 1.6: 17, 2.6: 17 inlet conditions, 3.6: 8 input power calculation, 1.6: 15 input power formulas, 3.6: 11 instrument calibration interval, 2.6: 9, 1Ot. instrument fluctuation and accuracy, 2.6: 1O instrumentation, 1.6: 11, 2.6: 9, 3.6: 7, 20, 21 t., 6.6:6 instrumentation accuracy, 1.6: 11 instrumentation fluctuation, 1.6: 11 key conditions, 3.6: 8 Level A acceptance, 3.6: 6 level A acceptance, 1.6: 9 Leve! B acceptance, 3.6: 6 level B acceptance, 1.6: 9 liquid conditions, 3.6: 9 at non-rated conditions, 2.6: 16-18 open or closed tan k, 1.6: 13f. at other than rated speed, 1.6: 16 outlet pressure, 3.6: 9 output power calculation, 1.6: 15 output power formulas, 3.6: 11 plotting of results, 3.6: 12, 12f. plotting results, 1.6: 16, 16f., 2.6: 16, 16f., 6.6: 9, 10f. power correction {formula), 3.6: 11, 12f. procedure, 3.6: 9, 6.6: 7

pump (closed loop), 2.6: 11, 12f. pump (closed suction), 2.6: 11, 12f. pump (general), 2.6: 12 rate of flow correction (formula), 3.6: 11 records, 1.6: 15, 2.6: 13, 3.6: 1O, 6.6: 9 at reduced speed, 1.6: 16, 2.6: 16 report, 1.6: 19, 2.6: 18, 6.6: 1O sample data sheet, 1.6: 14 setup, 1.6: 11, 2.6: 11-81., 6.6: 6, 71. for specific weight variations, 1.6: 18 speed, 3.6: 9 with suction lift, 1.6: 11 f. tabulation sheet, 3.6: 1Ot. and temperature variations, 2.6: 17 terminology, 6.6: 1-5 total discharge head calculation, 1.6: 15 total head calculation, 1.6: 15 total suction head calculation, 1.6: 15 Type 1, 3.6: 10, 6.6: 6 Type 11, 3.6: 10, 6.6: 6 Type 111, 6.6: 6 Type 111 and IV, 3.6: 7, 11 Type 111 and IV reports, 3.6: 12, 14f. witnessing, 1.6: 9, 2.6: 9, 3.6: 6 witnessing of, 6.6: 5 Performance. See also Submersible pump performance test calculation based on change in pump impeller diameter, 11.6: 29 calculation based on change in pump speed, 11.6: 29 calculation of ranges based on leve! A and leve! B acceptance criteria tolerances, 11.6: 31 Peripheral velocity, 9.6.1: 2 Permeability (magnetic), 4.1-4.6: 9 Permeance, 4.1-4.6: 9 Petroleum process pumps, 9.6.1: 6 Phenolic piston rings, 8.1-8.5: 19 application, 8.1-8.5: 19 clearance, 8.1-8.5: 20 forms, 8.1-8.5: 20 maximum concentration of chemicals, 8.1-8.5: 19t. Pilot-operated relief valve, 9.1-9.5: 4 Pipe dope, 8.1-8.5: 15 Pipe tape, 8.1-8.5: 15 Pipeline pumps, 9.6.1: 1O Piping, 2.3: 45, 3.1-3.5: 38,5.1-5.6: 33 See also Discharge piping, Suction piping hydraulic resonance, 2.4: 13 inlet, 3.1-3.5: 39 jacket, 3.1-3.5: 39 nozzle loads and criteria {limiting torces and moments), 3.1-3.5: 39, 40t., 42t. outlet, 3.1-3.5: 39 pipe-to-pump alignment, 3.1-3.5: 39f., 39

19 Copyright© 2002 By Hydraulic lnstitute, All Rights Reserved.

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Set pressure, 3.1-3.5: 4 Settling slurry, 6.1-6.5: 28, 9.1-9.5: 6 Settling velocity, 6.1-6.5: 28, 9.1-9.5: 6 Severity level, 9.6.5: 1-2 Sewage pumps, 1.3: 14 Shaft breakage mode causes and indicators, 9.6.5: 19t. Shaft deflection, 1.3: 70 Shaft fatigue failure, 9.6.3: 3 Shaft position monitoring, 9.6.5: 11 frequency, 9.6.5: 11 indicators, 9.6.5: 24 proximity probes, 9.6.5: 11 Shaft seal life, 9.6.3: 2 Shaft seals alternativa, 1.3: 70 mechanical seals, 1.3: 68, 69f. packed stuffing-box, 1.3: 69, 69f. Shafting, 2.3: 43 pump-to-driver, 2.3: 46 Shear pin relief valve , 9.1-9.5: 4 Shear rate, 3.1-3.5: 19 Shear stress, 3.1-3.5: 19 Shipment inspection, 3.1-3.5: 33 Shipping of magnets, 4.1-4.6: 19 Short-term storage, 1.4: 1 Shut off, 1.1-1.2: 58, 1.6: 1, 2.6: 1, 11.6: 3 Shutdown, 1.3: 22 , 3.1-3.5: 45 Shut-down analysis, 2.3: 15 Shutdown limit (defined), 9.6.5: 2 Shutoff, 2.1-2.2: 22 Silicon bronze, 9.1-9.5: 20 Silicon carbide, 5.1-5.6: 13 Simplex pump, 6.1-6.5: 2f., 2, 3f. Single plane balancing, 1.1-1.2: 60 Single suction pump specific speed, 1.3: 32, 33f., 34f. Single volute casing, 1.3: 58, 58f., 76 K versus rate of flow, 1.3: 58, 59f. Single-acting pump, 6.1-6.5: 1f., 1, 2f. Site preparation, 2.4: 1 foundation bolts, 1.4: 1, 2f. foundation requi rements, 1.4: 1 location of unit, 1.4: 2 maintenance access, 1.4: 1 protection against elements and environment, 1.4: 1 suction and discharge pipes, 1.4: 2 Sleeve bearings, 1.3: 64, 9.1-9.5: 4 Slip, 3.1-3.5: 14,3.6: 2, 5.1-5.6: 14,6.1-6.5: 20, 6.6: 4, 8.1-8.5: 7 hydraulic, 4.1-4.6: 10 magnetic, 4.1-4.6: 9 and slurries, 3.1-3.5: 26 and viscosity, 3.1-3.5: 23 Sluice gates, 9.8: 60

Slurries, 2.3: 36, 3.1-3.5: 24 apparent viscosity vs. shear rate, 3.1-3.5: 25, 26f. carrier liquids, 3.1-3.5: 24 characteristics, 3.1-3.5: 24 clearance provision for particle size, 3.1-3.5: 26 concentration of solids in, 3.1-3.5: 25 and construction materials, 2.3: 36 construction materials for, 3.1-3.5: 27 corrosion effect on wear, 3.1-3.5: 27 flow velocity, 3.1-3.5: 26 hardness of solids in, 3.1-3.5: 25, 25f. non-settling, 2.3: 36, 38f. operating sequences, 3.1-3.5: 27 and performance changas, 2.3: 36, 37f., 3.1-3.5: 26, 26f. pressure relief provision, 3.1-3.5: 27 pump design for, 3.1-3.5: 27 and rotativa speed, 2.3: 38 sealing against, 3.1-3.5: 27 settling, 2.3: 36, 38f. settling characteristics, 3.1-3.5: 25 shear rate effect on friction power, 3.1-3.5: 26 shear rate effect on slip, 3.1-3.5: 26 size of solids in, 3.1-3.5: 25 speed effect on wear, 3.1-3.5: 27 speed effects, 3.1-3.5: 26 testing and modeling for, 3.1-3.5: 27 wear, 3.1-3.5: 27 Slurry, 6.1-6.5: 27,9.1-9.5: 6 Slurry application terms, 9.1-9.5: 5 Slurry service, 1.3: 17-19 materials of construction for slurry pumps, 1.3: 17 non-settling slurries, 1.3: 17, 19f. relationship between concentration and specific gravity for aqueous slurries, 1.3: 17, 18f. rotational speed of slurry pumps, 1.3: 19 settling slurries, 1.3: 17, 19f. Slurry service pumps, 9.6.1: 9 Slush pump, 9.1-9.5: 4 Smothering gland, 9.1-9.5: 5 SO See Shut off Soft start drivers, 6.1-6.5: 37 Solids/abrasives in liquid, 9.6.1: 4 Soluble chloride, 9.1-9.5: 11 Sound level meters, 9.1-9.5: 50 Source material, 5.1-5.6: 38 Spacer type couplings, 3.1-3.5: 37 Spare parts, 1.1-1.2: 27, 3.1-3.5: 46 Specific composition bronze pumps, 9.1-9.5: 16, 17 Specific gravity, 3.1-3.5: 23,3.6: 6, 4.1-4.6: 14, 9.6.1: 2 Specific heat, 4.1-4.6: 14 Specific speed, 1.1-1.2: 2, 3f., 59,2.1-2.2:2 Specific weight, 3.6: 6

25 Copyright© 2002 By Hydraulic lnstitute, All Rights Reservad .

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Hllndex of Complete Set: 2002 Release Suction, 3.1-3.5: 33 loss of, 2.4: 16, 5.1-5.6: 37 pressure, 5.1-5.6: 15 Suction and discharge pipes, 1.4: 2 expansion joints and couplings, 1.4: 7 flat faced flanges, 1.4: 7 pipe support and anchors, 1.4: 7 requirements, 1.4: 7, 8 Suction conditions, 1.1-1.2:58,1.3: 57,2.1-2.2: 22, 2.3: 18, 6.1-6.5: 24, 8.1-8.5: 10 Suction energy, 9.6.1: 1O, 5 determination, 9.6.1: 3, 3f. factors, 9.6.1: 2 Suction energy leve! , 9.6.1: 1 Suction nozzle, 9.1-9.5: 5 Suction piping, 2.4: 4 See also Discharge piping, Piping eccentric reducers , 2.4: 4, 4f. elbows, 2.4: 5 reducers , 2.4: 4, 4f. , 5 requirements, 2.4: 4 strainers, 2.4: 5 supports, anchors, and joints, 2.4: 4 tanks, 2.4: 5 valves , 2.4: 5 Suction port. 3.1-3.5: 4, 9.1-9.5: 3 Suction pressure, 1.1-1.2: 60 , 8.1-8.5: 7 Suction pumps, 1.1-1.2: 4f. datum elevations, 1.1-1.2: 55f. submersible, 1.1-1.2: 5f. Suction recirculation, 1.3: 43, 9.6.3: 5 centrifuga! pumps, 9.6.3: 5, 5f., 6f., ?f. large boiler feed pumps, 9.6.3: 8 vertical turbine pumps, 9.6.3: 8, 8t. Suction specific speed, 1.1-1.2: 3f., 3, 1.3: 32 , 33f., 34f. , 35f., 36f. , 2.3:32, 9.6.1: 1, 9.6.3: 5 Suction system relationships, 6.1-6.5: 41, 42f., 43f. Suction tanks, 9.8: 9 minimum submergence, 9.8: 10, 10f., 111. multiple inlets or outlets, 9.8: 11 NPSH considerations, 9.8: 11 simultaneous inflow and outflow, 9.8: 11 Sump volume calculating , 9.8: 54 decreasing by pump alternation , 9.8: 57 minimum sequence, 9.8: 55 operational sequences, 9.8: 55, 56f. pump and system head curves, 9.8: 55, 56f. Surface vortices required submergence for minimizing, 9.8: 29, 33f., 34f. Swirl , 9.8: 1 in the suction pipe, 9.8: 27 meters, 9.8: 27, 27f. SWL See Static water leve!

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Symbols, 1.1-1.2: 56t. , 1.3: 1, 2t., 1.6: 2t. , 2.1-2.2: 19, 20t. , 2.3: 1' 2t., 3t. , 2.6: 2t. , 3.1-3.5: 15t., 3.6: 3t., 6.1-6.5: 21t. , 6.6: 1, 2t. , 8.1-8.5: Bt. , 9.8:38 Synchronous drive, 4.1-4.6: 10 Synchronous magnet coupling, 4.1-4.6: 11 System piping, 2.3: 45 System preparation, 2.4: 9 filling, 1.4: 1O flushing , 1.4: 1O pre-filling, 1.4: 11 priming, 1.4: 1O System pressure limitation , 1.3: 22, 2.3: 14 System ratings, 4.1-4.6: 17 System requirements, 1.3: 21 double suction pump specific speed , 1.3: 32, 35f. , 36f. effects of handling viscous liquids, 1.3: 23, 24f., 25f. , 26f., 27f. net positive suction head, 1.3: 38-42 NPSH margin considerations , 1.3: 39 NPSH reduction, 1.3: 39, 40f., 411. NPSH reduction for liquids other than hydrocarbons orwater, 1.3: 40f., 41f., 42 NPSH requirements for pumps handling hydrocarbon liquids and water at elevated temperaturas, 1.3: 39, 40f., 411. NPSHA corrections for temperatura and elevation , 1.3: 38 pump selection for a given head, rate of flow, and viscosity, 1.3: 28 pump versus system curve, 1.3: 21, 211. reverse runaway speed, 1.3: 22 shut-down, 1.3: 22 single suction pump specific speed, 1.3: 32, 33f. , 34f. starting with closed discharge valve, 1.3: 22 starting with open discharge valve , 1.3: 22 start-up, 1.3: 22 suction specific speed, 1.3: 32, 33f., 34f., 35f., 36f. system pressure limitation, 1.3: 22 torque curves, 1.3: 23, 23f. viscous liquid calculations, 1.3: 30t. , 31 , 32t. viscous liquid performance correction chart limitations, 1.3: 23 viscous liquid performance curves, 1.3: 30f., 30, 31 f. viscous liquid performance when water performance is known, 1.3: 29, 30f., 311. viscous liquid symbols and definitions , 1.3: 28 water hammer, 1.3: 22 t See Temperatura Tachometers, 1.6:31 , 6.6: 18,9.1-9.5:5 TAEH See Total available exhaust head Tail rod, 6.6: 3

28 Copyright© 2002 By Hydraulic lnstitute, All Rights Reserved.

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Volute pumps calculation for radial thrust, 1.3: 58 calculation of axial thrust for enclosed impellers, 1.3: 60- 63 circular casings, 1.3: 60, 60f. dual volute casing, 1.3: 58, 59f. K versus rate of flow (double volute casing), 1.3: 58, 59f. K versus rate of flow (single volute casing) , 1.3: 58, 59f. single volute casing, 1.3: 58, 58f. Vortices , 9.8: 1 free surface, 9.8: 1, 26, 26f. required submergence for minimizing surface vortices , 9.8: 29 , 33f., 34f. submerged , 9.8: 1 sub-surface, 9.8: 26f. , 27

Wells, 2.4: 2, 2f. checking, 2.4: 2 draw-down, 2.4: 11 Wet critica! speed, 9.6.4: 2 Wet pit pumps, 2.3: 1 Wet pit, short setting or close-coupled (lineshaft) pumps, 2.1-2.2: 1, 9f. Wet pit volute pumps, 1.1-1.2: 14f. total suction head, 1.1-1.2: 57 Wet wells (solids-bearing liquids), 9.8: 15 cleaning procedures, 9.8: 17 confined inlets, 9.8: 16 trench-type, 9.8: 16f. vertical transitions, 9.8: 16 wet well volume, 9.8: 17 Winding temperature test, 5.1-5.6: 40 Working pressure, 1.1-1.2: 60, 2.1-2.2: 23

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