Text

Rev 1 to Calculation ENSM720719FK, Centrifugal Charging Pump (Ccp) Npsh.
	ML17335A155
Person / Time
Site:	Cook
Issue date:	07/19/1972
From:	Kuo F; INDIANA MICHIGAN POWER CO.
To:	;
Shared Package
ML17335A147	List: ML17335A146; ML17335A148; ML17335A149; ML17335A150; ML17335A152; ML17335A153; ML17335A154; ML17335A155; ML17335A156; ML17335A157; ML17335A185;
References
	ENSM720719FK, ENSM720719FK-R01, ENSM720719FK-R1, NUDOCS 9808100113
	Download: ML17335A155 (34)
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NUCI.KARENGINEERING DEPARTMENT Calculation Cover Sheet Cook Nuclear Plant SafetyRelatedMechanicalSystems Sheet 1 of II~

INDIANAMICHIGANPOWER COMPANY CALCULATIONNO. ENSM720719FK UNIT NO. 1 SAFETYRELATED YES g NO Q CALCULATEDBY: F. Kuo 7/19/72 DATE SYSTEM VERIFIED BY:

TITLE DATE 9CP/RFC/MM/PM/PR/CR/TM/NO. $ 3/;4 APPROVED BY:

FILE LOCATION j / '~iv/ i~r I I I/E.~

CALCULATIONDESCRIPTION:

This calculation determines the NPSH to unit METHOD OF VERIFICATION:

cason for Change 1

ALTERNATE CALCULATION B'

REVISION Calculated Date

~

cast centrifugal charging pump (CCP) from thc volume control Iy Vcrificd Bv r~ gv'E~

5gm REVIEW Date Approved B

tank (VCT)

Date 1 Correct NPSH calc using absolute terms J.'ak 7/1/98 instead of a candu ate format ggV Sion /

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Table of Contents Title ~Pa e Discussion and Purpose Design Inputs and Data Sources References Method Acceptance Criteria Assumptions Calculation ary of Results and Conclusion Original Calculation (2 pages) Attachment 1 Original Computer Output (1 page) and Input Data (4 pages) Attachment 2 Aux Bldg Drwgs 5441 2 5443, VCT and Pipe Details Attachment 3 Pacific Pump Foundation Plan FC-45605 Attachment 4 Pacific Pump Test Curve 34617 - I Attachment 5

Discussion and Pu ose I 4 T lculation is being revised to correct the error of using gauge instead of absolute terms when calculating for the centrifugal charging pump taking suction from the volume control tank (VCT) during normal operation. The format is also updated to current convention and for clarity. Although the original calculation was in error, the error was in the conservative direction wherein the calculated NPSH available (NPSHa) was one atmosphere or 34 ft below the actual value. Therefore the actual margin is 34 ft higher than calculated.

Desi n In uts and Data Sources

1. Elevation of VCT outlet pipe flange = 611'-0-1/40 = 611.02', per Drawing 1-5441-12, B/8 2, Elevation of pump centerline = 590'-9" = 590.75', per Drawing 1-5443-23, C/5.

tI Ig II II 1 I

=Ip II It gp,p Dgglllpll 3.-3,4 *~.

3. Elevation of Pump suction nozzle is 20" above the centerline, per Pacific Pump Drawing PC-45605

= 590'-9" + 20" = 592'-50 = 592.42'.D 3I Note; Max normal operating flow is letdown flow of 120 gpm (max) plus 60 gpm miniflow, all per UFSAR table 9.2-2, plus 24 gpm seal return flow, per assumption 5 below, for a total fiow of 204 ~ m.

5. Temperature Normal suction temperature = 115 ', ' per UFSAR table 9.2-3 VCT hi temp alarm QTI-451 set at 134 Operating procedure limit of 185 Use 190 ' as boundin

', with+/- 3 deg uncertainty, per ECP 1-CG-16B per 01 OHP 4021.003.001, Rev 19

6. VCT Pressure = 0 to 60 psig, per UPSAR Table 9.2-3; cise 0 si<<as a conservatism.

7. NPSH required (NPSHr) at 204 gpm = 12 ft, per representative NPSH curve on Pacific test curve 34617 I.

nces

l. Updated Final Safety Analysis (UFSAR)

2. Hydraulic Institute Standards, 12 Edition, 1969

3. Flow of Fluids, Tech Paper No. 410, 14 printing 1974, Crane Co.

4. Procedures 01-OHP 4021.003.001, Rev 19 and 01-OHP 4022.002.001, Rev 8, C. S. 1

5. AEP Drawings 1-5441-12 and 1-5443-23, (Attachment 3, Sheets 1 8c 2)

6. Pacific Pump Co Drawing FC-45605 and Test Curve 34617-I, (Attachments 4 2 5)

Method The NPSHa is defined as the total suction head in feet of liquid absolute, determined at the suction nozzle and referred to datum, less the absolute vapor pressure of the liquid in feet of liquid pumped.

Therefore; (1) NPSHa = Ha - Hvpa+ Hs, per Hydraulic Institute Standards page 41 Where Ha = atmospheric pressure in ft absolute (14.7 psi or 34 ft)

Hvpa = vapor pressure of liquid in 6 absolute Hs = total suction head in ft (2) Hs =Z+P/y-Hf Where Z = elevation of liquid in tank above pump suction nozzle in ft P/y = tank pressure in psig converted to ft of head by the density factor.

Hf = pipe &iction in ft between the tank and the pump suction nozzle.

Note; the pipe friction computed for the original calculation will be used for this revision.

The friction value for flows other than the 98 gpm used in the original will be calculated based on the square relationship of flow to friction as shown in the Darcy-Weisbach equation lHf = f(L/D)(V/2g), eq 2-8, pg 2-8 Crane, that is; (3) Hfz =Hfi(Q2/Ql) . ENS/141 Let07/s1 r I W

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Acce tance Criteria able operating conditions exist when the NPSHa exceeds the NPSHr.

A~i

1. Based on review of the values, the friction value used in the original calc is assumed to be correct.

2. The level in the VCT is conservatively assumed to be below the low level alarm and actually out of the tank.

3. The liquid temperature is conservatively assumed to be 190 ', 5 ' above the highest procedural limit.

4. It is assumed that the values calculated based on the piping configuration of the unit 1 East pump are applicable to all 4 pump installations. This assumption is made since the slight differences in the unit 1 West and both unit 2 pumps are considered insignificant relative to magnitude of the margin of 12 ft.

5. The extremely conservative assumption that the seal leakoff on all 4 RCPs is at the maximum 6 gpm instead of the nominal 3 gpm. Procedure Ol-OHP 4022.002.001, Rev 8, C. S. 1, steps 3 &, 15 trips the pump and the if unit the flow on any one RCP rapidly increases to 6 gpm (the max reading on the flow instrument). We are assuming the unprecedented condition where the flow on all 4 RCPs reach 6 gpm simultaneously..

Calculation late the NPSHa at a flow of 204 gpm, at 190 deg F

1. Establish the friction (Hf) at 204 gpm based on the original HFLC2 computer calc at 98 gpm.

Hfi = total friction of the four series segments 1 through 4 from the VCT to the pump at 98 gpm

= 1.12+ 0.04 + 0.01 + 0.05 = 1.22 ft

=

Hf> friction of the segments at 204 gpm

= Hfi(Q2/Ql) [eq 3] = 1.22ft x.(204/98) = 5.29 ft

2. Calculate total suction head Hs = Z + P/y - Hf [eq 2] = (611.02' 592.42') + 0 - 5.29' 13.31 ft

3. Calculate NPSHa NPSHa = Ha - Hvpa+ Hs [eql]

vapor pressure of water@190' = 9.340 psia per Crane, Pg A-6 weight density of water @ 190 ' = 60.343 8/ft per Cran'e, Pg A-6 therefore Hvpa = P/y = 9.340 psia/(60.343 0/ft /144in2/ft ) = 22.29 ft NPSHa = 34- 22.29+ 13.31. = 25.02 ft, use 25 ft

4. Margin of NPSHa over NPSHr = 25 - 12 = 13 ft Summa of Results and onclusions Adequate NPSH exists at the extreme worst case bounding conditions reviewed in this revision since the NPSHa well exceeds the NPSHr with a margin of 13 ft.

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227200-STG-5400-02
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REV. 1 PAGE 13 OF 13 EM",o)5) DONALD C. COOK NUCLEAR PLANT i:iiih)
Fur}ct'i':oni.fSAi:ez
~v~wkrv; use>>si>>>>>>:i>>~>>e VERIFICATION CHECKLIST - CALCULATIONS Cal cul at i on Number r- I'~~
7 Signature of Verifier Date 1.0 Mere the inputs/'data~souCces correctly selected, incorporated and documented into the calculation2 Yes ,~ ' N/A
..f.':u<< --/-'-"~V='I.'>> //-'~;)).,~".)) -.i:)= 0 p~">i>i ~i~
Basi s:
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2.0 Are assumptions necessary to perform the calculation Basis:
adequately described and reasonable2 Q).)p'r) )7i Ori'~ 4+;! r; /~i-. f lj)~<<() I+~s . 'i ~
Yes g e.,51/
N/A
~). 7;)ll) ))
k 'S8 '"' ~rs ~
i-Js~ )>> ~v/-')Iv vc')
3.0 Are the applicable codes, standards and regulatory requirements identified and requirements for design met2 Yes ~ N/A Basis: .51() /ki 1 Fc LI ~ lb /~)~5h u~/~&8'~)' )-Qk s~,
~ l l4 (.))J 0J)/pSW (.'.p - /s, . 0Z W . =II>~'.~ .'aCC) C~~))s
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(,.I4 /fP/<. ~ ~ '4 ).w (.) ).
~
rJI u'=ii~~ Ci '><<'~c AD'e/ rid' r S)V '-r>
$ ,0 Basis:
Mas an appropriate design method used2 C ~L .<st sq Yes
~ C
+s=ss 'I
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G'1 Is-'5 s.'z) >Oh iQ - /aiE zw>g r =:I h>>))i/rg1g 2- + f
~ 5/"I/cr% r i);Yi/.r~,
~A J)f /J" W 'l))~p r i)
-cubi)c 7 Bl/ ) Se <<~ivW
~~~~5.0 Bas1s~~~~
Is the output reasonable compared to input2 86 tM<) ~AT ~85 8P) 9s >(.') ('rf Yes
~J
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M/A P~AL" *LA'7rw~ w'/ls .)I )~Qy7) f C~v uV .
- RZecr.
~~~~6.0 Basis~~~~
Are the results numerically correct2 0! ))-P>dry= Cr!/- .I. ~/)-;~~ pE'ph)
Yes
'"L
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Attachment 5
KNSM 720719FK Rev.l Alternate Calculation Verification XNPUTS
~~~~1. Proto-Flo Version 3.04 Model for CVCS Normal charging floiv path developed~~~~
~~~~¹ for approved Calculation ENSM961213AF Rev. 1, Approval Date 5/28/97.~~~~
~~~~2. Model inputs Specific to Charging Pump NPSH Calculation ¹ ASM 720719FK Rev. 1 under worst case normal operating conditions.~~~~
~ Suction Temperature 190 '
~ VCT Pressure 14.7 psia
~ 'eal water injection flow 44 gpm Charging header flow 100 gpm
~ CCP mini-flow in service (model calculated flow at 57.24 gpm vs the 60 gpm assumed by calculation initiator)
Discussion Charging Pump NPSH calculation was verified using a previously approved Proto-flo model of the CVCS system under calculation ENSM 961213AF Rev. 1. Model inputs were revised slightly to reflect inputs used by calculation ENSM 720719FK Rev. 1.
The revised inputs are stated under item ¹2 of the inputs listed.
The revised Proto-flo model was run 7/6/98 on a Dell computer model =:.'XMT5133,
¹ AEP specific PC 6738. Results of this alternate calculation along with a CVCS System Nodal Model Drawing have been attached with the Verification Check List. The Proto-flo model automatically calculates NPSHa and compares the value against the NPSHr curve which was input as part of the model design. The verification calculation confirtns within one ft the results obtained under ENSM 720719FK Rev. 1
07-06-1998 14:17 PROTO-FLO 3.04 by Proto-Power Corporation - Serial 4000 Page 1 l8 M - C:FPROTOFLOiCVCS1.PDB-Cook Plant - ECCS/CCP System Pump Status Report Pump Name PP50W Manufacturer Model:
Drawings:
Pump Status: OFF Speed (RPM): Flow (gpm) Head (ft):
Hydraulic Horsepower:
Pump Impeller Datum (ft) Inlet Node Elevation (ft): 597.00 Pump Suction Temperature ('F 190.00 NPSH Curve: PP50 NPSH NPSH Available: NPSH Required:
Pump Name PP50E Manufacturer Model:
Drawings:
Pump Status: PP50 Speed (RPM): Flow (gpm): 201.25 Head (ft): 5.494.61 Hydraulic Horsepower: 270.37 Pump Impeller Datum (ft) Inlet Node Elevation (ft): 596.33 Pump Suction Temperature ('F 190.00 NPSH Curve: NPSH NPSH Available'4.21 ~ NPSH Required: 11.02 Zg ~y ~p ]~irvai~
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I I 07-06-1998 14:17 PROTO-FLO 3.04 by Proto-Power Corporation - Serial 4000 Page 1 I8 M - C:iPROTOFLOiCVCS1.POB-Cook Plant - ECCS/CCP System Combined Output Report Convergence: Pressure-"1.02-5 Sum 0=1.0E-2 Friction=1.0H FCV-"1.0E-4 PCV=1.0E-3 Temperature=5.0E Balancing Parameters Used Pipe: 1.00 ID = 4.260 Flow = 144.01 Vel= 3.242 Turbulent f = 0.0177 Reynold's Number = 3.2017E+05 N1: CS1 '* Press= 14.70 Elev= 611.02 Flow= 0.00 Temp= 190.00 N2: CS2 Press= 14.71 Elev= 610.42 Flow= 0.00 Temp= 190.00 Pipe: 2.00 ID = 4.260 Flow = 201.25 Vel= 4.530 100.00% Vel Turbulent f = 0.0173 Reynold's Number = 4.4742E+05 N1: CS2 Press= 14.71 Elev= 610.42 Flow= 0.00 Temp= 190.00 N2: CS3 Press= 19.39 Elev= 597.00 Flow= 0.00 Temp= 190.00 Pipe: 4.00 ID = 6.357 Flow = 201.25 Vel = 2.034 Turbulent f = 0.0169 Reynold's Number = 2.9983E+05 N1: CS3 Press= 19.39 Elev= 597.00 Flow= 0.00 Temp= 190.00 N2: CS5 Press= 19.61 Elev= 596.33 Flow= 0.00 Temp= 190.00 Pipe: 500 ID = 8.329 Flow = 201.25 Vel = 1.185 Turbulent f = 0.0169 Reynold's Number = 2.2884E+05 N1'S5 Press= 19.61 Elev= 596.33 Flow= 0.00 Temp= 190.00 N2: CS6 Press= 19.60 Elev= 596.33 Flow= 0.00 Temp= 190.00 Pipe: 6.00 ID = 6.357 Flow = 201.25 NPSHA =24.21 NPSHR = 11.02 N1: CS6 Press= 19.60 Elev= 596.33 Flow= 0.00 Temp= 190.00 N2: CS7 Press= 2,324.70 Elev= 590.75 Flow= 0.00 Temp= 190.00 Pipe: 8.00 ID = 3.626 Flow = 201.25 Vel = 6.253 Turbulent f = 0.0176 Reynold's Number = 5.2565E+05 N1: CS7 Press= 2,324.70 Elev= 590.75 Flow= 0.00 Temp= 190.00 N2: CS9 Press= 2,323.84 Elev= 592.00 Flow= 0.00 Temp= 190.00 Pipe: 10.00 ID = 1.689 Flow = 57.24 Vel = 8.197 100.00% Vel Turbulent f = 0.0208 Reynold's Number = 3.2095E+05 N1: CS9 Press= 2,323.84 Elev= 592.00 Flow=. 0.00 Temp= 190.00 N2: CS10 Press= 24.26 Elev= 592.00 Flow= 0.00 Temp= 190.00 Pipe: 11.00 ID = 2.067 Flow = 57.24 Vel= 5.473 Turbulent f = 0.0202 Reynold's Number = 2.6226E+05 N1: CS10 Press= 24.26 Elev= 592.00 Flow= 0.00 Temp= 190.00 N2'S11 Press= 17.21 Elev= 605.58 Flow= 0.00 Temp= 190.00 Pipe: 12.00 ID = 4.260 Flow = 57.24 Vel = 1.288 Turbulent f = 0.0194 Reynold's Number = 1.2725E+05 N1: CS11 Press= 17.21 Elev= 605.58 Flow= 0.00 Temp= 190.00 N2: CS12 Press= 16.89 Elev= 606.33 Flow= 0.00 Temp= 190.00
!! Reverse Flow Thru Check Valve
++ Section Was Balanced Fixed Pressure
%% Pressure Below Vapor Pressure rV Temperature Outside Fluid Property Range W NPSHA less than NPSHR M Flow Past End of Pump Curve
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~ ~,i 07-06-1998 14:17 PROTO-FLO 3.04 by Proto-Power Corporation - Serial ¹000 Page 2 1&M - C:iPROTOFLOiCVCS1.PDB-Cook Plant - ECCS/CCP System Combined Output Report Convergence: Pressure=1.0E-5 Sum Q=1.0E-2 Friction=1.0E-6 FCV=1.0'CV=1.0E-3 Temperature=5.0E Balancing Parameters Used Pipe: 13.00 ID = 4.260 Flow = 57.24 Vel = 1.288 Turbulent f = 0.0194 Reynold's Number = 1.2725E+05 N1'S12 Press= 16.89 Elev= 606.33 Flow= 0.00 Temp= 190.00 N2: CS2 Press= 14.71 Elev= 610.42 Flow= 0.00 Temp= 190.00 Pipe: 17.00 ID = 3.626 Flow = 144.01 Vel = 4.475 100.00% Vel Turbulent f = 0.0179 Reynoid's Number = 3.7615E+05 N1: CS9 Press= 2,323.84 Elev= 592.00 Flow= 0.00 Temp= 190.00 N2: CS16 Press= 2,324.86 Elev= 588.50 Flow= 0.00 Temp= 190.00 Pipe: 18.00 ID = 3.626 Flow = 144.01 Vel = 4.475 Turbulent f = 0.0179 Reynold's Number = 3.7615E+05 N1: CS16 Press= 2,324.86 Elev= 588.50 Flow= 0.00 Temp= 190.00 N2: CS15 Press= 2,321.33 Elev= 596.17 Flow= 0.00 Temp= 190.00 Pipe: 19.00 ID = 2.626 Flow = 144.01 Vel = 8.531 Turbulent f = 0.0187 Reynold's Number = 5.1939E+05 N1: CS15 Press= 2,321.33 Elev= 596.17 Flow= 0.00 Temp= 190,00 N2: CS17 Press= 2,283.15 Elev= 594.58 Flow= 0.00 Temp= 190.00 Pipe: 20.00 ID = 2.626 Flow = 144.01 Vel= 8.531 Turbulent f = 0.0187 =
Reynold's Number 5.1939E+05 N1: CS17 Press= 2,283.15 Elev= 594.58 Flow= 0.00 Temp= 190,00 N2: CS18 Press= 2,279.61 Elev= 596.08 Flow= 0.00 Temp= 190.00 Pipe: 21.00 ID = 2.626 Flow = 100.01 Vel= 5.925 Turbulent f = 0.0190 Reynold's Number = 3.6069E+05 N1: CS18 Press= 2,279.61 Elev= 596.08 Flow= 0.00 Temp= 190.00 N2: CS19 Press= 2,282.08 Elev= 588.50 Flow= 0.00 Temp= 190.00 Pipe: 22.00 ID = 2.626 Flow = 100.01 Vel = 5.925 Turbulent f = 0.0190 Reynold's Number = 3.6069E+05 N1: CS19 Press= 2,282.08 Elev= 588.50 Flow= 0.00 Temp= 190.00 N2: CS19A Press= 2,281.67 Elev= 588.50 Flow= 0.00 Temp= 190.00 Pipe: 23.00 ID = 2.626 Flow = 100.01 ++ Vel = 5.925 Turbulent f = 0.0190 Reynold's Number = 3.6069E+05 N1: CS19A Press= 2,281.67 Elev= 588.50 Flow= 0.00 Temp= 190.00 N2: CS19B Press= 2,161.75 Elev= 594.50 Flow= 0.00 Temp= 190.00 Pipe: 24.00 ID = 2.626 Flow = .100.01 Vel = 5.925 100.00% Vel Turbulent f = 0.0190 Reynold's Number = 3.6069E+05 N1: CS19B Press= 2,161.75 Elev= 594.50 Flow= 0.00 Temp= 190.00 N2: CS19C Press= 2,087.86 Elev= 613.75 Flow= 0.00 Temp= 190.00
.! Reverse Fiow Thru Check Valve
++ Section Was Balanced Fixed Pressure
%% Pressure Below Vapor Pressure
?? Temperature Outside Fluid Property Range
¹¹ NPSHA less than NPSHR
&& Flow Past End of Pump Curve
t~ 0 (g,(p 07-06-1998 14:17 PROTO-FLO 3.04 by Proto-Power Corporation - Serial 4000 Page 3 IBM -I C:iPROTOFLOiCVCS1.PDB-I
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~ ~
Cook Plant - ECCS/CCP System
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Combined Output Report
>>~
Convergence'Pressure=1.0E-5 I Sum Q=1.0E-2
~
~
~
I Friction=1,0E-6
~
I I ~
FCV"-1.0E4 PCV=1.0E-3
~ ~ Temperature=S.OE Balancing Parameters Used Pipe: 25,00 ID = 2.626 Flow = 54.02 Vel = 3.200 100.00% Ve I Turbulent f = 0.0198 Reynold's Number = 1.9484E+05 N1: CS19C Press= 2,087.86 Elev= 613.75 Flow= 0.00 Temp= 190.00 N2: CS20 ** Press= 2,085.00 Elev= 615.75 Flow= 0.00 Temp= 190.00 Pipe: 26.00 ID = 2.626 Flow = 45.99 Vel = 2.724 100.00% Vel Turbulent f = 0.0200 Reynold's Number = 1.6585E+05 N1: CS19C Press= 2,087.86 Elev= 613.75 Flow= 0.00 Temp= 190.00 N2: CS21 ** Press= 2,085.00 Elev= 615.75 Flow= 0.00 Temp= 190.00 Pipe: 35.00 ID = 2.626 Flow = 44.00 Vel= 2.607 Turbulent f = 0.0201 Reynold's Number = 1.5870E+05 N1'S18 Press= 2,27961 Elev= 596.08 Flow= 0.00 Temp= 190.00 N2: CS30 Press= 2,277.04 Elev= 601.81 Flow= 0.00 Temp= 190.00 Pipe: 36.00 ID = 2.626 Flow = 44.00 Vel = 2.607 Turbulent f = 0.0201 Reynold's Number = 1.5870E+05 N1: CS30 Press= 2,277.04 Elev= 601.81 Flow= 0.00
~ Temp= 190.00 N2: CS31 Press= 2.280.91 Elev= 591.75 Flow= 0.00 Temp= 190.00 Pipe: 37.00 ID = 2.626 Flow = 44.00 Vel = 2.607 Turbulent f = 0.0201 Reynold's Number = 1.5870E+05 N1: CS31 Press= 2,280.91 Elev= 591.75 Flow= 0.00 Temp= 190.00 N2: CS32 Press= 2,280.86 Elev= 591.75 Flow= 0.00 Temp= 190.00 Pipe: 38.00 ID = 1.689 Flow = 44.00 Vel = 6.301 Turbulent f = 0.0211 Reynold's Number = 2.4674E+05 N1: CS32 Press= 2,280.86 Elev= 591.75 Flow= 0.00 Temp= 190.00 N2: CS33 Press= 2,279.64 Elev= 587.84 Flow= 0.00 Temp= 190.00 Pipe: 43.00 ID = 2.626 Flow = 44.00 Vei= 2.607 Turbulent f = 0.0201 Reynold's Number = 1.5870E+05 N1: CS33 Press= 2,279.64 Elev= 587.84 Flow= 0.00 Temp= 190.00 N2: CS37 Press= 2,279.55 Elev= 587.84 Flow= 0.00 Temp= 190.00 Pipe: 44.00 ID = 2.626 Flow = 44.00 Vel = 2.607 Turbulent f = 0.0201 Reynold's Number = 1.5870E+05 N1: CS37 Press= 2,279.55 Elev= 587.84 Flow= 0.00 Temp= 190.00 N2: CS38 Press= 2,279.49 Elev= 587.84 Flow= 0.00 Temp= 190.00 Pipe: 45.00 ID = 2.626 Flow = 44.00 Vel = 2.607 Turbulent f = 0.0201 Reynold's Number = 1.5870E+05 N1: CS38 Press= 2,279.49 Elev= 587.84 Flow= 0.00 Temp= 190.00 N2: CS39 Press= 2,276.66 Elev= 594.00 Flow= 0.00, Temp= 190.00
.! Reverse Flow Thru Check Valve
++ Section Was Balanced Fixed Pressure
%% Pressure Below Vapor Pressure
'?7 Temperature Outside Fluid Property Range
,¹¹ NPSHA less than NPSHR
&& Flow Past End of Pump Curve
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07-06-1998 14:17 PROTO-FLO 3.04 by Proto-Power Corporation - Serial ¹000 Page 4 l8 M - C:>PROTOFLO'tCVCS1.PDB-Cook Plant - ECCS/CCP System Combined Output Report onvergence: Pressure=1.0E-5 Sum Q=1.0E-2 Friction=1.0E-6 FCV=1,0E-4 PCV=1.0E-3 Temperature=S.OE Baiancina Parameters Used Pipe: 46.00 ID = 1.689 Flow = 11.00 ++ Vel = 1.575 100.00% Vel Turbulent f = 0.0236 Reynold's Number = 6.1685E+04 N1: CS39 Press= 2,276.66 Elev= 594.00 Flow= 0.00 Temp= 190.00 N2: CS40 Press= 2,085.38 Elev= 616.50 Flow= 0.00 Temp= 190.00 Pipe: 47.00 ID = 1.689 Flow = 11.00 Vel = 1.575 100 00% Vel Turbulent f = 0.0236 Reynold's Number = 6.1685E+04 N1: CS40 Press= 2,085.38 Elev= 616.50 Flow= 0.00 Temp= 190.00 N2: CS41 Press= 2,085.30 Elev= 616.50 Flow= 0.00 Temp= 190.00 Pipe: 48.00 ID = 1.338 Flow = 11.00 Vel = 2.510 Turbulent f = 0.0238 Reynold's Number = 7.7867E+04 N1: CS41 Press= 2,085.30 Elev= 616.50 Flow= 0.00 Temp= 190.00 N2: CS42 ** Press= 2,085.00 Elev= 616.94 Flow= 0.00 Temp= 190.00 Pipe: 49.00 ID = 2.626 Flow = 33.00 Vel = 1.955 Turbulent f = 0.0207 Reynold's Number = 1.1902E+05 N1: CS39 Press= 2,276.66 Elev= 594.00 Flow= 0.00 Temp= 190.00 N2: CS43 Press= 2,276.32 Elev= 594.75 Flow= 0.00 Temp= 190.00 Pipe: 50.00 ID = 1.689 Flow = 11.00 ++ Vel= 1.575 100.00% Vel Turbulent f = 0.0236 Reynold's Number = 6.1685E+04 1: CS43 Press= 2,276.32 Elev= 594.75 Flow= 0.00 Temp= 190.00 N2: CS44 Press= 2,085.13 Elev= 616.94 Flow= 0.00 Temp= 190.00 Pipe: 51.00 ID = 1.689 Flow = 11.00 Vel = 1.575 100.00% Vel Turbulent f = 0.0236 Reynold's Number = 6.1685E+04 N1: CS44 Press= 2,085.13 Elev= 616.94 Flow= 0.00 Temp= 190.00 N2! CS45 Press= 2,085.09 Elev= 616.94 Flow= 0.00 Temp= 190.00 Pipe: 52.00 ID = 1.338 Flow= 11.00 Vel = 2.510 Turbulent f = 0.0238 Reynold's Number = 7.7867E+04 N1: CS45 Press= 2,085.09 Elev= 616.94 Flow= 0.00 Temp= 190.00 N2: CS46 *'ress= 2,085.00 Elev= 616.94 Flow= 0.00 Temp= 190.00 Pipe: 53.00 ID = 2.626 Flow = 22.00 Vel = 1.303 Turbulent f = 0.0217 Reynold's Number = 7.9350E+04 N1: CS43 Press= 2,276.32 Elev= 594.75 Flow= 0.00 Temp= 190.00 N2: CS47 Press= 2,276.00 'lev= 595.50 Flow= 0.00 Temp= 190.00 Pipe: 54.00 ID = 2.626 Flow = 11.00 ++ Vel= 0.652 100.00% Vel Turbulent f = 0.0240 Reynold's Number = 3.9675E+04 N1: CS47 Press= 2,276.00 Elev= 595.50 Flow= 0.00 Temp= 190.00 N2: CS48 Press= 2,084.23 Elev= 619.00 Flow= 0.00 Temp= 190.00 everse Flow Thru Check Valve
++ Section Was Balanced Fixed Pressure
%% Pressure Below Vapor Pressure
?? Temperature Outside Fluid Property Range W NPSHA less than NPSHR 8.8. Flow Past End of Pump Curve
((i i 07-06-1998 14:17 PROTO-FLO 3.04 by Proto-Power Corporation - Serial 0000 Page 5 I8 M I- C:iPROTOFLOiCVCS1.PDB-I
~ ~
Cook Plant - ECCS/CCP System
~~
~
~
Combined Output Report
~ ~ I ~ ~ Temperature=5.0E Balancing Parameters Used Convergence: t Pressure=1,0E-5I Sum Q=1.0E-2
~ ~
~
~ ~ Friction=1,0E-6 FCV=1.0E-4
~ PCV=1.0E-3
~
Pipe: 55.00 ID = 2.626 Flow = 11.00 Vel = 0.652 100.00% Vel Turbulent f = 0.0240 Reynold's Number = 3.9675E+04 N1: CS48 Press= 2,084.23 Elev= 619.00 Flow= 0.00 Temp= 190.00 N2: CS49 Press= 2,085.63 Elev= 615.58 Flow= 0.00 Temp= 190.00 Pipe: 56.00 ID = 1.338 Flow ='1.00 Vel = 2.510 Turbulent f = 0.0238 Reynold's Number = 7.7867E+04 N1: CS49 Press= 2,085.63 Elev= 615.58 Flow= 0.00 Temp= 190.00 N2: CS50 "'ress= 2.085.00 Elev= 616.94 Flow= 0.00 Temp= 190.00 Pipe: 57.00 ID = 2.626 Flow = 11.00 Vel= 0.652 Turbulent f = 0.0240 Reynold's Number = 3.9675E+04 N1: CS47 Press= 2,276.00 Elev= 595.50 Flow= 0.00 Temp= 190.00 N2'S51 Press= 2,275.68 Elev= 596.25 Flow= 0.00 Temp= 190.00 Pipe: 58.00 ID = 2.626 Flow = 11.00 ++ Vel= 0.652 100.00% Vel Turbulent f = 0.0240 Reynold's Number = 3.9675E+04 N1: CS51 Press= 2,275.68 Elev= 596.25 Flow= 0.00 Temp= 190.00 N2; CS52 Press= 2.085.33 Elev= 616.50 Flow= 0.00 Temp= 190.00 Pipe: 59.00 ID = 2.626 Flow = 11.00 Vel = 0.652 100.00% Vel Turbulent f = 0.0240 Reynold's Number = 3.9675E+04 N1: CS52 Press= 2,085.33 Elev= 616.50 Flow= 0.00 Temp= 190.00 N2: CS53 Press= 2,085.30 Elev= 616.50 Flow= 0.00 Temp= 190.00 Pipe: 60.00 ID = 1.338 Flow = 11.00 Vel = 2.510 Turbulent f = 0.0238 Reynold's Number = 7.7867E+04 N1: CS53 Press= 2,085.30 Elev= 616.50 Flow= 0.00 Temp= 190.00 N2: CS54 "Press= 2.085.00 Elev= 616.94 Flow= 0.00 Temp= 190.00
.. Reverse Flow Thru Check Valve
. + Section Was Balanced Fixed Pressure
%% Pressure Below Vapor Pressure 77 Temperature Outside Fluid Property Range W NPSHA less than NPSHR
&8 Flow Past End of Pump Curve
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5.0 Bas1s

6.0 Basis

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