ML20199L841

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Rev 4 to M-51-62, NPSH Analysis Residual Heat Removal Sys
ML20199L841
Person / Time
Site: Limerick  Constellation icon.png
Issue date: 01/15/1998
From:
PECO ENERGY CO., (FORMERLY PHILADELPHIA ELECTRIC
To:
Shared Package
ML20199L838 List:
References
M-51-62, M-51-62-R04, M-51-62-R4, NUDOCS 9802100043
Download: ML20199L841 (40)
v • d • e


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L ATTACHMENT 1 l l

Limerick Generating Station Unit i NPSH Analysis Residual Heat Removal System 9902100043 990202 PDR ADOCK 05000352

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.Effcctivo Dato: 0; M- % Exhibit nE-C-42o-o, nov. 2 PORO HO 00NTFl0LLED COPY "*'* ISNad n

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I CALCULATION REVILIION SHEET

)( INTERIH REVISION MARGIN REVISION Ti!IS CALCULATION HAS DEEN IMPACTED PER THIS REVISION SHEET AS FOLLOWS Tms (2evostM Is kertoesete To UN*r I onc1. rms C+t c o wna is gevosco ro p crt,m ou r- nte LJour C<sc (LHA Sus m blPSH A Ano To CAu.o esrc NPsn A M us,a As A trsvur Of ntc In smu.wca on NetJ L.Nm--

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EffCetivo Datot b* N'9 b Exhibit NE-C-420~3, Rev. 2

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CALCULATION REVIEW CITECKLT8T i l

MANUAL COMPU1!R '

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X Calculation is the appropelate beats for the activity Calculation assmptions, conalderatione, and wthodology conform to b j

'ka applicable design requirements '

X X tources of data and forculas were reviewed and verifled to be correct armi complete Yo l X X input data is 9errect and used properly b X

The analytical method used in the calculation has been considered and is 42 proper for the intended use Y X

Hathematical accuracy has been checked ard is correct (Irdleste method used)

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a) Complete check of each calculation b b) spot check of selected calculations N9/

c) Ferformance of alternate or approximation calculation (attached) i X k N#

Calculation results kers checked against applicable design critarla ard /to were found to be in comtlance X X taisting calculations requiring revision as a result of this calculation NM2 have been identIfled and doemented i X

The analytical methods described in the coguter calculation swmary are -. N/A proper for the intended use X X All system and topic nmbers associated with the calculation are ilsted Ydo X

Computational accuracy has been checked and is correct (Irdicate method Md8 used) a) Check sample calculation using data other than that used in the sample N/A i

b) Performance of alternate or approximation calculation (attached) NIP c) Describe other method used: N44 1

X Program used is appropriate, input is valid, ard output is reasonable - N/A considering the input i X X Base calculation has been reviewed against current drawing revisions and Yeo'y '

} posted DCDs to identify significant differences '

The criteria 1 Lated above are the minimum criteria to be considered and are not x intended to limit the initiative of the reviewer to considor other criteria.

> Attributen applicabic to manual and computer calculations are noted by an *X" cppropriate column. in the List the documents used to support this review.[N'M9o MCemt+t8

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,mcmR CALCULATION C.OVER SHEET _

2 GROUP UNIT (5) N O PDAPS DOCTYPE 061 E Responsiole Brancfr 7. S Sahwy Related 4'MODINCRIECH No.: NW & hst Py No. 20 0 No"Safett Rela'ed Othec PGP r#644457 .

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,/j qi.gcJe LII d/ 4M8 CALCUL Afl0N SCpttNING F00 THE AS. BUILT DESIGN I (> The purpose of this calculation revision il to document that the calculation res..tl mand conclusions are still applicable to the al. built design of the plant including difications.

j Q Reviewer has determined the calculation results and conclusions are applicable to the al. built design of the plant becaule 0

O the original design margin was large and subsequent modifications have had little or no impact on the design margin, ere have been no modifications to the lyttem which affect this calculation, the pre.op where telt results appropriate) are (al adjusted to agree with calculation allumptioni, conlittent with the calculation and lublequent modl have not significantly affected the calculation resultl. ,

Others l

C Reviewer has determined the calculation results and Corclusions are no longer applicable to the al built design of the plant because the calculation design margin has already been exceeded.

Other:

C #eviewer cannot determine that the calculation results and conclusions are applicable to the 45 built design of the plant in the time available. Further technical evaluation il recomended.

ef er to Sheet for 'a list of @ cpl. DCPl design document $ and pre.op telt results hat were reviewed during the calculation Screening review.

L'tt11tation of this calculation by petoone, without access to the pertinent f actore and without proper relate tot its purpose, coul4 need to ottoneous concluetoes.

Should it become necessary to use any of thle' calculation la your work to the future, it is sultested that sta calculation be reviewed with authertsed F ehtel paroonnel, to eneute

t horoughly unde rs t ood.that the purpotet, assumptions. judlaente end-Itattations are Sechtel cannot assume toeponstbtitty for the use of tal-

[culatione not under out direct control.

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SA.k9.A SAErL X- X CALCVLATION 13 THE APPRQPR! ATE BA31$ FOR THE ACTIVITY X X CALCULATION A3SUMPTIONJ, CCN33 DERAT 30N2, AND METHDDOLCCY CONFORM TC I i APPLICABLE Dt33cN REQUIREMENT 3 $

X X Y COURCE3 0F DATA AND FORMULAS WERE REY!tWED MD VERIFIED To ht CORRECT AND COMPLETE L X X INPUT DATE 33 CORRECT AND UstD PROPtRLY X THE ANALYT3 cat HETHOD U3tD $N THE CALCULATION HA3 httN CON 210tRED f '

AND 13 PROPER FOR THE 2NTENDED U38 i X '

MATHEMATICAL ACCURACY MA3 attn CHECKt0 AND 18 CORRtCT (INDICATE O HETHOD U3LD)

A) COMPLETE CHECK OF EACH COMPUTATION ,,,, Y B) SPOT CHtCK OF SELECTED COMPUTATIONS Md C) PERFORMANCE OF ALTERNAtt OR APPROX 3MATICN CALCULATION A8 d (ATTECHED)

X X CALCJLATICel RESW i WERE CHICKED ACAlNST APPL 3CARLE DES 3CN CRITERIA AND WERE FOUND TO Rt $N COMPL!ANCE X X EXIST!NO CALCULATIONS REQUIRINC REVISION AS A RESULT OF THIS _

CALCVLATION HAVE BttN 3 DENT!F!t0 & DOCUNtNTfD X THE ANALYTICAL M'THODS CtsCR3 BED IN THE COMPUTER CALCULATION A/A SUHWY !$ PRO', '0R THE INTENDED USE X X ALL SYSTEM AND TCPIC NUN &tR3 A330CIATED WITH THE CALCULATION ARE Y LISTED X COMPUTATIONAL ACCURACY HA3 8ttN CHtCKED AND 3$ CORRICT (InJ3CATE AM HETHOD USED)

A) CHECK SAMPLt CALCULATICN U23NC CATA CTHER THAN THAT V3t0 IN M4 THE SAMPLE

8) PERFORMANCE CF ALTERNATE OR APPROX 3 MAT 3CN CALCULATION M ,,,,, *

(ATTACHED)

C) DESCRIBE OTHER METHOD USED: .. Alb .

X PRocRAM U$rD 15 APPROPRIATE, INPVT 33 VALID, AND CUTPUT 3 5 Mb REASONABLE CON 3IDERING THE INPUT X X- Bast CALCULAT30N HAS BFEN PrV3tWED ACAINST CURRENT DRAWING M

' REVIS10NS AND POSTED DCDS TO 1DENTITY $1CN!FICANT D3FFERENCES The criteria listed above are the minimum criteria to be considered and are not

-intended to limit the initiative of the reviewer to consider other criteria.

Attributes applicable to manual and computer calculations are noted by an 'X' in the appropriate column, List the documents used to support this review. I'"* I$ Alh1 #*H" 410

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8N . $HF2TNO.M YC ,f. 2Y fd The Following WDCPs, DCPs Design Documents, and Pre-Op Test Results Were Reviewed, f.0 Circled items relate specifically to this calculation.

M NDCP DCP PCR/PCN

, g UNIT 1 UNIT 2 'JNIT 1 UNIT 2 UNIT 1 UNIT 2 0024-1 0815-1 5579-2 68 2006 5 1115 6878 03 0035-1 0431-1 6006-2 76 2014 80 5006 6995 0047 1 5010-1 78 2015 84 5012 8203 0133-1 5042-1 81 2021 86 5013 8455 gf, 0171-1 5054 1 109 2044 116 5022 8466 0176-1 5178-1 115 2083 121 5042 8468 0 0193-1 5228-1 117 2088 248 5510 8477

_ 0302-1 5261-1 139 2092 620 5562 8595 0303-1 5579-1 156 2095 6005 20173

  • 0363-1 5650-1 239 2103 6080 20176 0397-1 5658-1 289 6084 20179 0494-1 5663-1 367 6116 20181 0522-1 5716-1 493 6121 20216 0680-1 5770-1 558 6171 20319 0696-1 5709-1 559 6208 20321 0793-1 5791*1 563 6240 20329 0801-1 5906-1 2014 6241 20383 2015 6306 20405 2021 6331 20423 2083 6354 20477 2088 6373 20562 2092 6494 20580 2095 6569 20739 2103 6620 20886 Other'Desitn.Documentab 4

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CALCULATION M-51-62, PAGE 3A 3

REFERENCES (CONTINUED) 11.- Specification No. NE-265, Revision 1, Specification for ECCS Suction Strainers.

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12. Bechtel Drawing 8031-M 277, Revis3.on 66.

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13. SDOC NE-265-00037, Revisionji: ABB Calculation 599-PENG-CALC-060, Revision 0, Limerick ECCS Strainer Sizing for Debris Loading and Pressure Drops, 4
14. SDOC NE-265-18, Revision 0: ABB Calculation MISC-PENG-CALC-062, Revision 0, Evaluation of Predictions and Data for Prototype Strainer.

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IT 0~2 MI- DATE- M hN CHECKED M ^ byJADATE IO/L"/ N PROJECT $~ $?#I E S l C h' $Y I'T" $ $ JOB NO. _- $DSl SUBJECT- N dNEM N b $HEET NO- 1, . O' '

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CALCULATION SHEEi g M lt 1/j'a q's p Os cAtc.No. M-R- 6 2 nEv.uo, pf 1 oaiciNATon M M Y#T4d64L oATE / O//4 /8B _cHEcKEO 'I A/L*1h/tG ATE [pl C-/Of-eno;EcT l- / MEW / CM- (JA/ #7- / I f.- Jo8 No. [

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E D 6915/761 l

I3d0 CALCULATION SHEEi S- CALC. NO. M **  !'~ b QEV.NO. O

- OniclN ATOR N' M V'IMd CO/- DATE/O!M'!Ob CHECKEOh Alamla40 ATE 10 / r*/M PROJECT [ / M N # C !d MA / T' /2 JOB NO. 08!

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CAI.CULATION SHEEi gget k ICMV /!/30/98 0 cAtc.no. M*'TI-d b nEv.no. . b L oniclN ATOR - N / TANS 7 M DATE /O! OO CHECKEO'f ^/d*'dyAS ATE /n i f / M rnosEcT l-l ME~R / r K Ur.) / 7 / 8 2. soa no. 802/ ,

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  • DATE /0 !80 CHeCKEb'I ^ $ ; g DATE ! D/ I/ N rRoster t !ME~RidL Uniir / A 2. ,oe no. 803/ ,

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EO 69 (6/761 l

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PROJECT NIO /C O^l/T / E JOB NO. O [ a A HR. S ys7&M N'P,5//

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E D-69 (5/76) 8o

'. 196 214s3 IS4

PECO ENERGY CALC NO.: M s162 NuCt. EAR GnouP CALCULATION SHEET eAGe: 1s Revision 4 REVISION 4 To re- aluate the net positive suction head available (NPSHA) for the residual heat te val (RHR) system ' h suction aligned from the suppression pool (SP) under the worst expected nditions and with an inc ase in the maximum allowable differential pressure across the suction rainer of 5.0 psid (the original ign was 2.0 psid).

During the regular ump valve and flow tests, measurements will be taken of e pressure at the pump suction (PP 51102A and PP 51202A D) with suction aligned to the SP d with no flow (static) and with design rated (10,0 gpm) flow (dynamic). The purpose of these m asurements is to show loop capability for LGS Techn al Specification requirements. An addalonal urpose of this calculation is to establish the maximum val for the difference between these two asured pressures beyond which the loop may not satisfy its s ety function, i

Results With suction aligned from the SP, un r worst expected conditions (212*F and 1 atm), with a pump flow l

rate of 11,000 gpm, a SP level of 199' %", and a m ' um allowable differential pressure across the

, suction strainer of 5.0 psid, the calculate et positi uction head available is i

NP 7.97 feet The margin to the net positive sucaon head re ulr by the pump is, argin = 2. feet With a system test (SP to SP) flow rat of 10,000 gpm, the aximum allowed change in suction pressure measured at PP 51 1(2)02 D) is 6.3 psid.

P ,,,, P% > 6.3 psid Max. Allowed These results are applicable t both LGS Unit 1 and Unit 2, inputs T = 212 'F P = 45 psia (only us to determ p and )

P = 59.81992 lbm/ cutt 4 = 0.28222 cp P . 1 atm

  • = 1 atm O - 11,000 gpm -

d = 23.25 Inches L,(24") = 474.5 feet Ly(30") = 151.5 feet b = 199.95833 feet

$m = 174.87500 feet NPSHR = 6.0 feet @ 11,000 gpm

. _ . - . . . =___ .-- -_--~-.-. .. . . - - . - . - . ~ . -

196 21403 tr4

  • cal.C NO.t M 51-62

- PECO ENERGY nuo m acnou, CALCULATION SHEET exaE: 1e Revision 4 Calebations rins Gt A.

NET PO TIVE SUCTION HEAD AVAILABLE Flow losses et including stralner; f rom page 3 2 of References 5 & 6, Re = 50.65929 OP pd

= 5,08 E+06 To account for 40 year life, assu e a roughness factor of .00085 feet (equivalent to cast iron)

From page A 24 of References 5 &

4 f = 0.0163-~ $ .

From page 3 2 Equation 3 b of Reference &6 1

/ p 02

. A P, = 2.1 037 33E-4 ,

23.25 "

y = 474.5 + 151.5 s 9.25 3

= 522.57 feet AP, - 2.161037233E-4 (0.0163351)(59.81992)(52 57)(11000)2 (23.25)5 i

= 1.965 psid

196 214531C4

. . PECO ENERGY cal.C NO.: M 5162

'~

NUCLEAR GROUP CALCULATlON SHEET exce: 17 Revision 4 WS Calet'tations (Cont'd) Ft A Calcu ting the NPSHA, with P. - P,,

NPSHA = 1 (P. - P y- AP -f AP,uno,) + Z -Z, p

= 199.95833 - 174.875 - l 59 81992 (1.965 + 5.0)

= 8.17 feet @ p = 5 .1992 lbm/cuft

= 8.317 x 9.81 92 62,4

= 7.97 et @ p 62.4 lbm/ cult Thus, NP HA = 7,97 et PSHR = 6.00 feet @ 11,000 gpm. Ref 10)

Margin - 2.00 feet

. 11t6 214s31C4

. . PECO ENERGY CALC NO.: M 51-62 uucu>a anou,, CALCULATION SHEET eAos: 18 Revision 4 Chulations (Cont'd)

MAXIN M VALUE The press e loss due to flow calculated above considered the longest suction line f m the SP and assumed a r ughness factor of 0.00085 to account for a 40 year life. The equival t length calculated is therefore co servative for the calculation of NPSHA, but should not be used i evaluate a maximun value for a mea red diiterence in suction pressure between static and dyna conditions because it would attribute o measured flow dP to the line itself and less to the stral r. Thus a conservativel/

LOW value of equi lent length should be used for this part of the calculat n.

It is conservative to as ume the hotest SP temperature expected durl the test, that of the maximun' SP temperature allowab by Technical Specification during normal p nt operation,95'F.

T = 95

  • P = 45 sia P = 62.06687 lbm/cdt M 0.71955 cp O - 10.000 gpm Calculating the Reynold's Number for ese input p meters yields,

. Re .65929 OP d

= 1.88 +06 and using clean pipe with a r ghness factor of 0.00MS, get a friction factor of, f = 0.01' 4405 Re-evaluating the a to I equivalent line length using shorter line ngths of, lp,24") = 450 feet g30") " 100 feet -

23.2ps L q = 450 + 100 x

( 29.25 j

= 481.73 feet e

. sos.2i453 ted PECO ENERGY cal.C NO.: M 5162 WCWR GRN CALCULATION SHEET e^os: 19 Revision ,,, 4 _ _ _

talculations (Cont'd) '

Ev ating the line losses (not including the suction strainer), b Pf = 2.161037233E-4 (0.0124405)(62.06687)(481.73)(1 - )8 (23.25)s

= 1. 83 psid The difference betwe3n the p ssure at the pump suction (PP) at s tic conditions and at dynamic conditions can be expre *ed a A =P, -Pen, ,

A + Py + A P, w, where, P,.. = pre ute att pump suction with no flow P ,,,,,,, = pr ssure at the ump suction with flow APf

  • ressure loss du o flow (not including the suction strainer)

AP, = pressure loss due t velocity (i.e, the velocity head in psid)

A P,,,,,,, = maximum allowable p ssure drop across the strainer (5.0 psid)

The pressure loss due to velocit is evaluated, using the 30" sucti pipe (since the pressure tap is in the 30" portion of the suction li e) as, APy = 1.80086E-5 P

= 1.80086E-5 (62.06687) (10W (29.25)4

= 0.1527 psid N

PEC EN CAL.C NO.: M 5162 Y

CALCULA. TION SHEET e^oe 20 nevision __ 4 calculations (Cont'd)

W f Thus the difference between the measured suction pressure at static copdtlons and at dynam e

', conditions becornes, '

AP = APf + APy+ AP, 3 ,

= * .18 + 0.15 5,00

= 6.3 p Max. Allowed l

-,%9

CALCULATION M 51-62, PAGB 21

1. - CALCULATE NPSHA IOR MODE " A-1" (REF.1)

Ooemting Condill0D1 Flow = 10,150 gpm Temperature = 170'F I

Specific Weight @ 170'F = 60.79 lb/ft' (Ref 7)

Minimum Suppression Pool W.L. Depth = 18.04 ft (Ref 2)

Minimum Suppression Pool W.L. Elevation = 199' l1%" (Ref 2)

Pressure @ Suppn:ssion Pool = 14.7 psia (Ref 1)

Vapor Pressure @ 170*F = 5.99 psia (Ref 7)

Pump Suction Elevation = 174.875 ft (Ref 3)

NPSHA = h, - hy , + h, - hr.

where, .

h, = absolute pressure (in feet of liquid) on the surface of liquid supply level 9

hy, = head (in feet) corresponding to the vapor pn:ssure of the liquid being pumped h., = static head (in feet) of liquid above centenine of impeller eye hr. = suction line friction losses (in feet)

Calculate Suction Line Losses (AP)

AP = 0.000216 (Ref 5) d,

.where, AP = friction losses, psi Q = flow, gpm L = length of pipe, ft d = internal diameter of pipe, inches p = weight density of fluid, Ib/ft' f = friction factor

, CALCULATION M-51-62, PAGE 22 Reynolds Number of Flow in Pine Re = 50.6 O# (Ref 5) dp where, p = absolute (dynamic) viscosity in centipoise = 0.4 @ 170* F (Ref 5) 6P Eb 24" Line Rc = = 335x10' (23.25)(0.4) c/D (Relative Pipe Roughness)

Use Cast Iron Pipe to account for Pipe Aging 24" DIA, Cast Iron Pipe = 0.0004 (Ref 5) f = 0.016 (Ref 5)

AP3 . = 0.000216(0.016W,(60.79)(10150)'

(23.25)'

= 1.51 psi 6P Eb 30" Line Re = = 2.66x10' (29.25)(0.4) c/D (Relative Pipe Roughness)

. Use Cast Iron Pipe to account for Pipe Aging 30" DIA, Cast Iron Pipe-= 0.00034 (Ref 5) f = 0,015 (Ref 5)

AP, = 0.000216 (0.015)(152)(60.79)(10150)2 (29.25)'

= 0.144 psi j

, CALCULATION M-51-62, PAGB 23

AP of Suction Strainer -

Diny AP @ 11,000 gpm @ 180'F = 7.11 ft (Ref 13) . 'i For Modc A-1 the strainer AP @ 10,150 gpm @ 170'F is needed.

The 10' F difference in temperature between Mode A-1 conditions and Reference 13 is '

addressed in the note.on page 24.

The diny strainer AP given in Reference 13 consists of nonnal system losses and bed losses (the layer of debris consisting of fiber and corrosion products). - When adjusting the AP for various flow rates the system losses are proponional to the square of the flow rates , while the bed losses have a linear relationship to the flow rates (Reference 14).

From Reference 13 the actual system losses are 2.85 ft and the bed losses are 4.26 ft @

l1,000 gpm @ 180'F.

Therefore, the diny AP @ 10,150 gpm @ 180* F is:

(2.85 fif(11,000s .+ (4.26 ftp0,W .

= 636 ft H O 2

'\l1,000s

> Total Suction Line Friction Losses hr, = AP24. + AP 3o. + APSTRAINER hr, = (1.51 + 0.144)(144/60.79) + 6.36 = 10.28 ft H2O Static Head h,, =. Min W.L. @ Suppression Pool - Elevation @ Center Line of Pump Suction Nozzle

- h,o= 199.96 ft - 174.875 ft = 25.085 ft

, CALCULATION M-51-62, PAGE 24 MODE A-1 NPSHA NPSHA = h, - hy. + h,, - hr, NPSHA = (14.7 - 5.99)(144/60.79) + 25.085 - 10.28 = 35.44 ft H 2O RHR Pump NPSHR @ 10,150 gpm = 5 ft H2 O (Ref 10)

NPSHA > NPSHR NOTE - the dirty strainer AP used is for 180

  • F. Based on Reference 14 the strainer AP will be slightly greater at 170
  • F (from 180
  • F to 100
  • F the strainer AP only increases by approximately 2 ft). Since the NPSHA @ 180
  • F is greater than the NPSHR by approximately 30 ft the slight increase in strainer AP from 180* F to 170
  • F will not result in the NPSRA being less than the NPSHR for Mode A-1.

i t

i

, CALCUIATION M-51-62, PAGE 25

2. CALCULATE NPSHA FOR MODE " A-2" (REF. D -

Opcrating Conditions Flow = 11,000 gpm Temperature = 180'F1 Specific Weight @ 180* F = 60.57 lb/ft' (Ref 7)

Specific _ Weight @ 212'F = 59.81 lb/ft(Ref 7)

Minimum Suppression Pool W.L. Depth =-18.04 ft (Ref 2)

Minimum Suppression Pool W.L. Elevation = 199'-11%" (Ref 2)

Pressure @ Suppression Pool = 14.7 psia (Ref 1)

Vapor Pressure @ 180'F = 7.511 psia (Ref 7)

Pump Suction Elevation = 174.875 ft (Ref 3)

NOTE: Equations for NPSHA, AP, and Reynolds Number are defm' ed in the section of this -

- calculation evaluating Mode A-1 (see page 21 and page 22).

AP O 24" Line

= absolute (dynamic) viscosity in centipoise = 0.35 @ 180'F (Ref 5)

Re = (5 .6XM,000X6037) = 4.14x10' (23.25X035) c/D (Relative Pipe Roughness)

Use Cast Iron Pipe to account for pipe aging.

24" DIA, Cast Iron Pipe = 0,0004 (Ref 5) f.= 0.016 (Ref 5)

AP3 . = 0.000216(0.016X474.5)(60.57XI1000)2 -

(23.25)'

= 1.77 psi-

' AP a 30" Line

,9x10 5 Re

(29.25X035) c/D (Relative Pipe Roughness)

Use Cast Iron Pipe to account for pipe aging.

30" DIA, Commercial Steel Pipe = 0.00034 (Ref 5) f = 0.015 (Ref 5)

. CALCULATION M-5162, PAGB 26 All, = 0,000216 (0.0@2)(60W000f (29.25)'

= 0.169 psi AE of Suction Strainer 4

Actual Diny AP @ 11,000 gpm @ 180'F = 7,11 ft H2 O (Ref 13)

Maximum Allowable Diny AP @ l1,000 gpm @ 212'F = 12 ft H 2O (Ref 11 and Ref 13)

Convened to 180'F = (12)(59.81/60.57) = 11.85 ft H2 O

! Igjal Suction Line Friction losses hr, = AP24. + AP 3o. + APSTRANER Br. sed on Actual Strainer Diny AP:

he, = (1.77 + 0.169)(144/60.57) + 7.11 = 11.72 ft H 2O Based on Maximum Allowable Strainer Diny AP:

hr, = (1.77 + 0.169)(144/60.57) + 11.85 = 16.46 ft H 2O Static Head h,, = Min W.L, @ Suppression Pool- Elevation @ Center Line of Pump Suction Nozzle h,, = 199.96 ft - 174.875 ft = 25.085 ft MODE A-2 NPSHA NPSHA = h, - hy, + h,, - hr, NPSHA Based on Actual Strainer Dirty AP=

(14.7 - 7.511)(144/60.57) + 25.085 - 11,72 = 30.46 ft H 2O NPSHA Based on Maximum Allowable Strainer Strainer Diny AP=

(14.7 - 7.511)(144/60.57) + 25.085 - 16.46 = 25.72 ft H 2O RHR Pump NPSHR @ l1,000 gpm = 6 ft H 2O (Ref 10)

NPSHA > NPSHR

, CALCULA*I1ON M-51-62, PAGE 27 y*

3. CALCE4TE NTSHA FOR MODE "B" (REF.1)

)

Operatine Conditions Flow = 10,000 gpm Temperature = 212

  • F Specific Weight @ 212 *F = 59.81 lb/ft' (Ref 7)

Minimum Suppression Pool W.L. Depth = 18.04 ft (Ref 2)

Minimum Suppn:ssion Pool _W.L. Elevation = 199'-11%" (Ref 2)

Pressure @ Suppression Pool = 14.7 psia (Ref 1)

Vapor Pressure @ 212'F = 14,696 psia (Ref 7)

Pump Suction Elevation = 174.875 ft (Ref 3)

NOTE: Equations for NPSHA, AP, and Reynolds Number are defined in the section of this calculation evaluating Mode A-1 (see page 21 and page 22).

AP Eb 24" Une l

= absolute (dynamic) viscosity in centipoise = 0.29 @ 212

  • F (Ref 5)

Re = (50.6)(10,00n)(59.81) = 4.49x10' (23.25)(0.29) c/D (Relative Pipe Roughness)

Use Cast Iron Pipe to account for pipe aging.

24" DIA, Cast Iron Pipe = 0.0004 (Ref 5) f = 0.016 (Ref 5)

AP3. = 0.000216 0.0MW)(R8 @,00#

(23.25)'

= 1,44 psi AP 1b 30" Line Re = ( '

= 3.57x10' (29.25)(0.29) c/D (Relative Pipe Roughness)

Use Cast Iron Pipe to account for pipe aging.

30" DIA, Commercial Steel Pipe = 0.00034 (Ref 5) f = 0.015 (Ref 5)

,-_ - CALCULA110N M-51-62, PAGE 28

a AP, = 0.000216 (0.0@228W0,00@

(29.25)'

= 0.138 psi AP of Suction Strainer Maximum Allowable Dirty AP @ 212.5

  • F_ @ l1,000 gpm = 12 ft H O 2 (Ref 11 and Ref 13) _

For Mode B the strainer pressure drop @ 212'F @ 10,000 gpm is needed.

The AP associated with the strainer consists of normal system losses and bed losses (the layer-

- of debris consisting of fiber and corrosion products). _When adjusting the AP for various flow rates the system losses r.re proportional to the square of the flow rates while the bed losses have a linear relationship to the flow rates (Ref 14).

From Reference 13 the actual system losses are 2,85 ft @ 213

  • F @ 11,000 gpm. Therefore it is assumed the maximum specified dirty AP of 12 ft from Reference 11 allows for 9.15 ft for l._ bed losses. >

1 Therefore the Maximum Dirty AP @ 212

  • F @ 10,000 gpm is:

f10*000 f10,000'

- (2.85 ft)(l1,000s+ (9.15 ft)(l1,000s= 10.67 ft H O 2 NOTE: The strainer AP obtained from Reference 11 is based on 212.5

  • F and 11,000 gpm.

The actual system losses obtained from Reference 13 is based on 213

  • F and 11,000'gpm. The Mode B operating temperature is 212
  • F (Reference 1). The difference in temperature is considered negligible based on the insignificant change in water properties between 212
  • F, 1212.5 'F, and 213
  • F which would have no impact on NPSHA.

Total Suction Line Friction Ensses h3= AP 24. + AP o.3 + APSTRAINER ha = (1.44 + 0.138)(144/59.81) + 10.67 ft = 14.47 ft H2 O

__- u

, CALCULA110N M 5163, PAGE 29 Statle Head h, = Min W.L. @ Suppression Pool Elevation @ Center Line of Pump Suction Nonle h, = 199.96 fl 174.875 ft = 25.085 ft MODE B...NPSHA NPSHA = h - h,,,, + h, - h,,

NPSHA = (14.7 - 14.7)(144/59.81) + 25.085 - 14.47 = 10.62 ft H 2O l

RHR Pump NPSHR @ 10,000 gpm = 5 fl H2O (Ref 10)

NPSHA > NPSHR The GB RHR Process Diagram (R:ference 1) requires the NPSHA at the pump suction nonle to be 210.3 ft plus the difference in elevation between a reference location and the centerline of the pump suction nonle. Reference I defines the reference location as 2 ft above the pump mounting flange. From Reference 12, the RHR pump mounting flange is at Elevation 177 ft.

Therefore, based on the requirements of Reference 1, the NPSHA must be 214.43 ft (177 + '

2 174.875 + 10.3). From above, the RHR pipluy, arrangement only provides 10.62 ft.

Although the NPSRA does not mM th:. generic design requirements specified in Rcference 1, NP5HA is considered acceptable based on the actual as built pump vendor requirements in accordance with Reference 10.

f

  • . i l, CALCULATION hi 5162, PAGB 30

.i

4. NPSIIA Marnin For Mode B Based On Actual Dirty Strainer AP i

The RHR System operating in hiode B is the limiting accident mode for NPSH, therefore the ,.

l NPSHA margin based on the Actual dirty strainer AP will be based on hiode B conditions.

RHR hiode B NPSHA = 10.62 ft H O 2 @ 10,000 gpm @ 212'F (page 29 of this calculation) 4 The above NPSHA is based on the maximum allowable AP for the new large capacity passive strainers. The purpose of this calculation is to determine the NPSH margin based on the actual dirty strainer AP. Therefore, the atx)ve NPSHA will be adjusted to obtain the NPSHA based on the actual dirty strainer AP:

NPSilAwtw = NPSHA%,3 + Maximum Allowable Dirty Strainer AP Actual Dirty Strainer AP hiaximum Allowable Dirty Strainer AP @ 10,000 gpm @ 212

  • F = 10.67 ft H 2O (Page 28)

The Actual Dirty Strainer AP is obtained from Table 1 of Reference 11:

Actual Dirty Strainer AP @ 11,000 gpm @ 213

  • P = Stralner System lesses + Strainerlied losses Actual Dirty Strainer AP @ l1,000 gpm @ 213
  • F = 2.85 ft + 3.75 ft = 6.60 ft H 2O NOTE: Thr; Actual Dirty Strainer AP obtained fmm Reference 13 is based on 213'F, however the actual hiode B temperature is 212'F. This 1 'F difference is considered to have an insignincant affect on the strainer AP based on the insignificant change in water pnresties from 212
  • F to 213'F.

Adjusting Actual Dirty Strainer AP adjusted to 10,000 gpm:

As previoulsy stated the actual dirty strainer AP consists of strainer system losses and strainer bed losses. From Reference 14 the system losses are proportional to the square of the flow rates while the bed losses have a linear relationship to the flow rates.

Therefore the Actual Dirty Strainer AP adjusted to 10,000 gpm:

, 00 ' '

(2.85 ft)(l1,000s + (3.75 ft)(l1,000s = 5.76 ft # 0 2 Therefore, NPSHA%.i oi,,y = 10.62 ft + 10.67 ft - 5.76 ft = 15.53 ft H 2O

a .

o

  • CALCULATION M 5162, PAGE 31 e.
k*

, Detennine NPSHA Margin:

a NPSHA Margin = NPSHA A oi, NPSHR

?

NPSHR = 5 ft H O 2 @ 10,000 gpm (Reference 10) i i ' n erefore, NPSHA Margin = 15.53 ft - 5 ft = 10.53 fl H 2O nerefore, there is suffielent margin between the RHR Pump NPSHA and the NPSHR when considering the actual dirty stminer AP of the new large capacity passive stminers.

a 1

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