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)
	v • d • e

1~0 EN4;4 -~ ~

(8/97)

NUCI.KARENGINEERING DEPARTMENT Calculation Cover Sheet Cook Nuclear Plant SafetyRelatedMechanicalSystems Sheet 1 of II~

CALCULATIONNO.

ENSM720719FK SAFETYRELATED YES g NO Q SYSTEM TITLE 9CP/RFC/MM/PM/PR/CR/TM/NO.

$3/;4 FILE LOCATION j / '~iv/ i~r I I I/E.~

INDIANAMICHIGANPOWER COMPANY UNITNO.

1 CALCULATEDBY:

F. Kuo VERIFIED BY:

APPROVED BY:

7/19/72 DATE DATE CALCULATIONDESCRIPTION:

This calculation determines the NPSH to unit 1 cast centrifugal charging pump (CCP) from thc volume control tank (VCT)

METHOD OF VERIFICATION:

y 5gmr~ gv'E~

I ALTERNATECALCULATION~ REVIEW REVISION cason for Change 1

Correct NPSH calc using absolute terms instead of a candu ate format Calculated B'J.'ak Date 7/1/98 Vcrificd Bv Date Approved B

Date PL78<

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Table ofContents Title Discussion and Purpose Design Inputs and Data Sources References

~Pa e

Method Acceptance Criteria Assumptions Calculation ary ofResults and Conclusion Original Calculation (2 pages)

Original Computer Output (1 page) and Input Data (4 pages)

AuxBldg Drwgs 5441 2 5443, VCT and Pipe Details Pacific Pump Foundation Plan FC-45605 Pacific Pump Test Curve 34617 - I Attachment 1

Discussion and Pu ose I 4 T

lculation is being revised to correct the error ofusing gauge instead ofabsolute 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 ofVCT outlet pipe flange

= 611'-0-1/40 = 611.02', per Drawing 1-5441-12, B/8 2, Elevation ofpump centerline

= 590'-9"

= 590.75', per Drawing 1-5443-23, C/5.

3. Elevation ofPump suction nozzle is 20" above the centerline, per Pacific Pump Drawing PC-45605 tI II 1 I II It

590'-9" + 20" = 592'-50

592.42'.D Ig II

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

3I Note; Max normal operating flow is letdown flowof 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 of204 ~ m.

5. Temperature Normal suction temperature = 115', per UFSAR table 9.2-3 VCT hi temp alarm QTI-451 set at 134 '

with+/- 3 deg uncertainty, per ECP 1-CG-16B Operating procedure limitof 185', per 01 OHP 4021.003.001, Rev 19 Use 190 '

as boundin

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 ofFluids, 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 ofliquid absolute, determined at the suction nozzle and referred to datum, less the absolute vapor pressure ofthe liquid in feet ofliquid 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 ofliquid in 6 absolute Hs

= total suction head in ft (2) Hs =Z+P/y-Hf Where Z

= elevation ofliquid in tank above pump suction nozzle in ft P/y = tank pressure in psig converted to ft ofhead by the density factor.

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

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

The friction value for flows other than the 98 gpm used in the original willbe calculated based on the square relationship offlowto 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 ~

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

A~i

1. Based on review ofthe 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 ofthe 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 ofthe 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 ofthe margin of 12 ft.

5. The extremely conservative assumption that the seal leakoff on all 4 RCPs is at the maximum 6 gpm instead ofthe nominal 3 gpm. Procedure Ol-OHP 4022.002.001, Rev 8, C. S. 1, steps 3 &, 15 trips the pump and the unit ifthe 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 flowof204 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 frictionofthe 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> = frictionofthe 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 ofwater@190'

= 9.340 psia per Crane, Pg A-6 weight density ofwater @ 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 ofNPSHa over NPSHr = 25 - 12 = 13 ft Summa ofResults 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 REV.
1 PAGE 13 OF 13 EM",o)5) i:iiih)
DONALD C.
COOK NUCLEAR PLANT Fur}ct'i':oni.fSAi:ez
~v~wkrv;use>>si>>>>>>:i>>~>>e VERIFICATION CHECKLIST - CALCULATIONS Cal cul at i on Number r-I'~~'ev.
Signature of Verifier 7
Date 1.0 Mere the inputs/'data~souCces correctly selected, incorporated and documented into the calculation2 Yes,~
N/A Basi s:
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Are assumptions necessary to perform the calculation adequately described and reasonable2 Yes ~
N/A Q).)p'r) )7i Ori'~
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3.0 Are the applicable
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N/A Basis:
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~~6.0 Basis~~
Are the results numerically correct2 0! ))-P>dry=
Cr!/-.I. ~/)-;~~
Yes ~
N/A pE'ph)
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4 lXISA F Attachment 5
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8-c~
KNSM 720719FK Rev.l Alternate Calculation Verification XNPUTS 1.
Proto-Flo Version 3.04 Model for CVCS Normal charging floivpath developed for approved Calculation ¹ 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 flowat 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 ofthe 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 ofthe inputs listed.
The revised Proto-flo model was run 7/6/98 on a Dell computer model =:.'XMT5133, AEP specific PC ¹ 6738. Results ofthis 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 ofthe 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 l8 M - C:FPROTOFLOiCVCS1.PDB-Cook Plant - ECCS/CCP System Pump Status Report Page 1
Pump Name Pump Name Manufacturer Model:
PP50W Drawings:
Pump Status:
OFF Speed (RPM):
Hydraulic Horsepower:
Pump Impeller Datum (ft)
Pump Suction Temperature ('F 190.00 NPSH Curve:
PP50 NPSH NPSH Available:
Flow (gpm)
Head (ft):
Inlet Node Elevation (ft): 597.00 NPSH Required:
Manufacturer Model:
Head (ft):
5.494.61 Inlet Node Elevation (ft): 596.33 PP50E Drawings:
Pump Status:
PP50 Speed (RPM):
Flow (gpm):
201.25 Hydraulic Horsepower:
270.37 Pump Impeller Datum (ft)
Pump Suction Temperature ('F 190.00 NPSH Curve: NPSH NPSH Available'4.21
~
NPSH Required:
11.02 Zg ~y
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gt=i" I
I I 07-06-1998 14:17 Page 1
PROTO-FLO 3.04 by Proto-Power Corporation - Serial 4000 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-3
- Balancing Parameters Used Pipe:
1.00 N1: CS1 N2: CS2 Pipe:
2.00 N1: CS2 N2: CS3 ID =
4.260 Flow =
144.01 Vel= 3.242 Turbulent f = 0.0177 Reynold's Number = 3.2017E+05
'* Press=
14.70 Elev= 611.02 Flow= 0.00 Press=
14.71 Elev=
610.42 Flow= 0.00 ID =
4.260 Flow =
201.25 Vel= 4.530 Turbulent f = 0.0173 Reynold's Number = 4.4742E+05 Press=
14.71 Elev= 610.42 Flow= 0.00 Press=
19.39 Elev=
597.00 Flow= 0.00 Temp=
190.00 Temp=
190.00 100.00% Vel Temp=
190.00 Temp=
190.00 Pipe:
4.00 N1: CS3 N2: CS5 Pipe: 500 N1'S5 N2: CS6 ID =
6.357 Flow =
201.25 Vel =
2.034 Turbulent f = 0.0169 Reynold's Number = 2.9983E+05 Press=
19.39 Elev=
597.00 Flow= 0.00 Press=
19.61 Elev=
596.33 Flow= 0.00 ID =
8.329 Flow =
201.25 Vel =
1.185 Turbulent f = 0.0169 Reynold's Number = 2.2884E+05 Press=
19.61 Elev=
596.33 Flow= 0.00 Press=
19.60 Elev=
596.33 Flow= 0.00 Temp=
190.00 Temp=
190.00 Temp=
190.00 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 N1: CS7 N2: CS9 Pipe:
10.00 N1: CS9 N2: CS10 Pipe:
11.00 N1: CS10 N2'S11 Pipe:
12.00 N1: CS11 N2: CS12 ID =
3.626 Flow =
201.25 Vel = 6.253 Turbulent f = 0.0176 Reynold's Number = 5.2565E+05 Press=
2,324.70 Elev=
590.75 Flow= 0.00 Press=
2,323.84 Elev=
592.00 Flow= 0.00 ID =
1.689 Flow =
57.24 Vel =
8.197 Turbulent f = 0.0208 Reynold's Number = 3.2095E+05 Press=
2,323.84 Elev=
592.00 Flow=. 0.00 Press=
24.26 Elev=
592.00 Flow= 0.00 ID =
2.067 Flow =
57.24 Vel= 5.473 Turbulent f = 0.0202 Reynold's Number = 2.6226E+05 Press=
24.26 Elev=
592.00 Flow= 0.00 Press=
17.21 Elev= 605.58 Flow= 0.00 ID =
4.260 Flow =
57.24 Vel =
1.288 Turbulent f = 0.0194 Reynold's Number = 1.2725E+05 Press=
17.21 Elev= 605.58 Flow= 0.00 Press=
16.89 Elev= 606.33 Flow= 0.00 Temp=
190.00 Temp=
190.00 100.00% Vel Temp=
190.00 Temp=
190.00 Temp=
190.00 Temp=
190.00 Temp=
190.00 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
l.a L ~
eu
~
~,i Page 2 07-06-1998 14:17 PROTO-FLO 3.04 by Proto-Power Corporation - Serial ¹000 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 N1'S12 N2: CS2 Pipe:
17.00 N1: CS9 N2: CS16 Pipe:
18.00 N1: CS16 N2: CS15 ID =
4.260 Flow =
57.24 Vel =
1.288 Turbulent f = 0.0194 Reynold's Number = 1.2725E+05 Press=
16.89 Elev=
606.33 Flow= 0.00 Press=
14.71 Elev= 610.42 Flow= 0.00 ID =
3.626 Flow =
144.01 Vel =
4.475 Turbulent f = 0.0179 Reynoid's Number = 3.7615E+05 Press=
2,323.84 Elev=
592.00 Flow= 0.00 Press=
2,324.86 Elev=
588.50 Flow= 0.00 ID =
3.626 Flow =
144.01 Vel = 4.475 Turbulent f = 0.0179 Reynold's Number = 3.7615E+05 Press=
2,324.86 Elev=
588.50 Flow= 0.00 Press=
2,321.33 Elev=
596.17 Flow= 0.00 Temp=
190.00 Temp=
190.00 100.00% Vel Temp=
190.00 Temp=
190.00 Temp=
190.00 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 N2: CS17 Press=
2,283.15 Elev=
594.58 Flow= 0.00 Temp=
190,00 Temp=
190.00 Pipe:
20.00 N1: CS17 N2: CS18 Pipe:
21.00 N1: CS18 N2: CS19 ID =
2.626 Flow =
144.01 Vel= 8.531 Turbulent f = 0.0187 Reynold's Number = 5.1939E+05 Press=
2,283.15 Elev=
594.58 Flow= 0.00 Press=
2,279.61 Elev=
596.08 Flow= 0.00 ID =
2.626 Flow =
100.01 Vel= 5.925 Turbulent f = 0.0190 Reynold's Number = 3.6069E+05 Press=
2,279.61 Elev=
596.08 Flow= 0.00 Press=
2,282.08 Elev=
588.50 Flow= 0.00 Temp=
190,00 Temp=
190.00 Temp=
190.00 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 N2: CS19A Press=
2,281.67 Elev=
588.50 Flow= 0.00 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 N2: CS19B Press=
2,161.75 Elev=
594.50 Flow= 0.00 Pipe:
24.00 ID =
2.626 Flow =
.100.01 Vel =
5.925 Turbulent f= 0.0190 Reynold's Number = 3.6069E+05 N1: CS19B Press=
2,161.75 Elev= 594.50 Flow= 0.00 N2: CS19C Press=
2,087.86 Elev= 613.75 Flow= 0.00 Temp=
190.00 Temp=
190.00 Temp=
190.00 Temp=
190.00 100.00% Vel Temp=
190.00 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 Page 3 PROTO-FLO 3.04 by Proto-Power Corporation - Serial 4000 IBM - C:iPROTOFLOiCVCS1.PDB-I
>>~
~
I
~
~
~I
~
~
~
I
~
I
~
~
~
~
I Cook Plant - ECCS/CCP System Combined Output Report Convergence'Pressure=1.0E-5 Sum Q=1.0E-2 Friction=1,0E-6 FCV"-1.0E4 PCV=1.0E-3 Temperature=S.OE-3
- Balancing Parameters Used Pipe:
25,00 ID =
2.626 Flow =
54.02 Vel =
3.200 Turbulent f = 0.0198 Reynold's Number = 1.9484E+05 N1: CS19C Press=
2,087.86 Elev= 613.75 Flow= 0.00 N2: CS20
~~Press=~~
2,085.00 Elev= 615.75 Flow= 0.00 Pipe:
26.00 ID =
2.626 Flow =
45.99 Vel =
2.724 Turbulent f = 0.0200 Reynold's Number = 1.6585E+05 N1: CS19C Press=
2,087.86 Elev= 613.75 Flow=
0.00 N2: CS21
~~Press=~~
2,085.00 Elev= 615.75 Flow=
0.00 100.00% Ve I Temp=
190.00 Temp=
190.00 100.00% Vel Temp=
190.00 Temp=
190.00 Pipe:
35.00 ID =
2.626 Turbulent f =
N1'S18 N2: CS30 Flow =
44.00 Vel= 2.607 0.0201 Reynold's Number = 1.5870E+05 Press=
2,27961 Elev= 596.08 Flow= 0.00 Press=
2,277.04 Elev=
601.81 Flow=
0.00 Temp=
190.00 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 N2: CS31 Press=
2.280.91 Elev= 591.75 Flow=
0.00 Temp=
190.00 Temp=
190.00 Pipe:
37.00 N1: CS31 N2: CS32 ID =
2.626 Flow =
44.00 Vel =
2.607 Turbulent f = 0.0201 Reynold's Number = 1.5870E+05 Press=
2,280.91 Elev= 591.75 Flow= 0.00 Press=
2,280.86 Elev=
591.75 Flow= 0.00 Temp=
190.00 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 N2: CS33 Press=
2,279.64 Elev= 587.84 Flow= 0.00 Temp=
190.00 Temp=
190.00 Pipe:
43.00 N1: CS33 N2: CS37 Pipe:
44.00 N1: CS37 N2: CS38 Pipe:
45.00 N1: CS38 N2: CS39 ID =
2.626 Flow =
44.00 Vei= 2.607 Turbulent f= 0.0201 Reynold's Number = 1.5870E+05 Press=
2,279.64 Elev= 587.84 Flow= 0.00 Press=
2,279.55 Elev=
587.84 Flow= 0.00 ID =
2.626 Flow =
44.00 Vel = 2.607 Turbulent f= 0.0201 Reynold's Number = 1.5870E+05 Press=
2,279.55 Elev=
587.84 Flow= 0.00 Press=
2,279.49 Elev=
587.84 Flow= 0.00 ID =
2.626 Flow =
44.00 Vel =
2.607 Turbulent f = 0.0201 Reynold's Number = 1.5870E+05 Press=
2,279.49 Elev=
587.84 Flow= 0.00 Press=
2,276.66 Elev= 594.00 Flow=
0.00, Temp=
190.00 Temp=
190.00 Temp=
190.00 Temp=
190.00 Temp=
190.00 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
A, ~
Page 4 07-06-1998 14:17 PROTO-FLO 3.04 by Proto-Power Corporation - Serial ¹000 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-3
- Baiancina Parameters Used Pipe:
46.00 ID =
1.689 Flow =
11.00
++
Vel =
1.575 Turbulent f = 0.0236 Reynold's Number = 6.1685E+04 N1: CS39 Press=
2,276.66 Elev= 594.00 Flow= 0.00 N2: CS40 Press=
2,085.38 Elev= 616.50 Flow= 0.00 Pipe:
47.00 ID =
1.689 Flow =
11.00 Vel =
1.575 Turbulent f = 0.0236 Reynold's Number = 6.1685E+04 N1: CS40 Press=
2,085.38 Elev= 616.50 Flow= 0.00 N2: CS41 Press=
2,085.30 Elev= 616.50 Flow= 0.00 100.00% Vel Temp=
190.00 Temp=
190.00 100 00% Vel Temp=
190.00 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 N2: CS42
~~Press=~~
2,085.00 Elev= 616.94 Flow=
0.00 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 N2: CS43 Press=
2,276.32 Elev=
594.75 Flow= 0.00 Temp=
190.00 Temp=
190.00 Temp=
190.00 Temp=
190.00 Pipe:
50.00 1: CS43 N2: CS44 ID =
1.689 Flow =
11.00
++
Vel=
1.575 Turbulent f = 0.0236 Reynold's Number = 6.1685E+04 Press=
2,276.32 Elev=
594.75 Flow=
0.00 Press=
2,085.13 Elev= 616.94 Flow=
0.00 100.00% Vel Temp=
190.00 Temp=
190.00 Pipe:
51.00 ID =
1.689 Flow =
11.00 Vel =
1.575 Turbulent f = 0.0236 Reynold's Number = 6.1685E+04 N1: CS44 Press=
2,085.13 Elev= 616.94 Flow= 0.00 N2! CS45 Press=
2,085.09 Elev= 616.94 Flow=
0.00 100.00% Vel Temp=
190.00 Temp=
190.00 Pipe:
52.00 N1: CS45 N2: CS46 ID =
1.338 Flow=
11.00 Vel =
2.510 Turbulent f= 0.0238 Reynold's Number = 7.7867E+04 Press=
2,085.09 Elev= 616.94 Flow=
0.00
~~'ress=~~
2,085.00 Elev=
616.94 Flow= 0.00 Temp=
190.00 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 N2: CS47 Press=
2,276.00 'lev= 595.50 Flow= 0.00 Temp=
190.00 Temp=
190.00 Pipe:
54.00 N1: CS47 N2: CS48 ID =
2.626 Flow =
11.00
++
Vel= 0.652 Turbulent f= 0.0240 Reynold's Number = 3.9675E+04 Press=
2,276.00 Elev=
595.50 Flow= 0.00 Press=
2,084.23 Elev= 619.00 Flow= 0.00 100.00% Vel Temp=
190.00 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 Page 5 PROTO-FLO 3.04 by Proto-Power Corporation - Serial 0000 I8 M - C:iPROTOFLOiCVCS1.PDB-t~~
~
~
I
~~
~
~
~
I
~
~
I
~
~
~
~
~
~
I Cook Plant - ECCS/CCP System Combined Output Report Convergence: Pressure=1,0E-5 Sum Q=1.0E-2 Friction=1,0E-6 FCV=1.0E-4 PCV=1.0E-3 Temperature=5.0E Balancing Parameters Used Pipe:
55.00 ID =
2.626 Flow =
11.00 Vel =
0.652 Turbulent f = 0.0240 Reynold's Number = 3.9675E+04 N1: CS48 Press=
2,084.23 Elev=
619.00 Flow= 0.00 N2: CS49 Press=
2,085.63 Elev=
615.58 Flow= 0.00 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 N2: CS50
"'ress=
2.085.00 Elev=
616.94 Flow= 0.00 100.00% Vel Temp=
190.00 Temp=
190.00 Temp=
190.00 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 N2'S51 Press=
2,275.68 Elev=
596.25 Flow= 0.00 Temp=
190.00 Temp=
190.00 Pipe:
58.00 N1: CS51 N2; CS52 ID =
2.626 Flow =
11.00
++
Vel= 0.652 Turbulent f = 0.0240 Reynold's Number = 3.9675E+04 Press=
2,275.68 Elev=
596.25 Flow=
0.00 Press=
2.085.33 Elev= 616.50 Flow=
0.00 100.00% Vel Temp=
190.00 Temp=
190.00 Pipe:
59.00 N1: CS52 N2: CS53 ID =
2.626 Flow =
11.00 Vel =
0.652 Turbulent f = 0.0240 Reynold's Number = 3.9675E+04 Press=
2,085.33 Elev= 616.50 Flow=
0.00 Press=
2,085.30 Elev= 616.50 Flow= 0.00 100.00% Vel Temp=
190.00 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 N2: CS54 "Press=
2.085.00 Elev= 616.94 Flow= 0.00 Temp=
190.00 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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ML17335A155

Text

590'-9" + 20" = 592'-50

2.0 Basis

6.0 Basis

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