ML20116F448
| ML20116F448 | |
| Person / Time | |
|---|---|
| Site: | 05200003 |
| Issue date: | 07/29/1996 |
| From: | Cooper M, Piplica E WESTINGHOUSE ELECTRIC COMPANY, DIV OF CBS CORP. |
| To: | |
| Shared Package | |
| ML19311C165 | List: |
| References | |
| WCAP-14706, WCAP-14706-R, WCAP-14706-R00, NUDOCS 9608070020 | |
| Download: ML20116F448 (62) | |
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Westinghouse Non-Proprietary Class 3
+ + + + + + + +
AP600 Automatic Depressurization System Stage 1,2, and 3 Cold Flow Test Westinghouse Energy Systems yge: , ,;. ; .
n ,y
AP600 DOCUMENT COVER SHEET TDC: IDS: I S Form 58202G(5/94) AP600 CENTRAL FILE USE ONLY:
0058.FRM RFS#: RFS ITEM #:
AP600 DOCUMENT NO. REVISION NO. ASSIGNED TO RCS-T2R-020 (non-prop) O Page 1 of W-PIPLICA g ALTERNATE DOCUMENT NUMBER: WCAP.14706 WORK BREAKDOWN #:
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ATTACHMENTS: N/A DCP #/REV. INCORPORATED IN THIS DOCUMENT REVISION: N/A e
CALCULATION / ANALYSIS
REFERENCE:
N/A ELECTRONIC FILENAME ELECTRONIC FILE FORMAT ELECTRONIC FILE DESCRIPTION m:\2962w.wpf Wordperfect 5.2 for Windows (C) WESTINGHOUSE ELECTRIC CORPORATION 1996 O WESTINGHOUSE PROPRIETARY CLASS 2 TNs document contains informat6on proprietary to Westinghouse Electric Corporation: it is submitted in con 6dence and is to be used solely for the purpose for wNch It is turrushed and retumed upon request. TNs document and such information is not to be reproduced, transmitted, disclosed or used otherwise in whole or in part without prior written authortzation of Westinghouse Electric Corporation, Energy Systems Business Unit, subject to the legends contained hereof.
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COMPLETE 1 IF WORK PERFORMED UNDER DESIGN CERTIFICATION -OR COMPLETE 2 IF WORK PERFORMED UNDER FOAKE.
1 @ DOE DESIGN CERTIFICATION PROGRAM - GOVERNMENT LIMITED RIGHTS STATEMENT [See page 2)
O Copyright statement A license is reserved to the U.S. Govemment under contract DE-AC03-90SF18495.
O DOE g toCONTRACT DELIVERABLES exg, disclosure of gELIVERED data is restricted DAT] september 30,1995 or Design Certi$ cation under DOE EPRI CONFIDENTIAL: NOTICE: 1 0 2 3 4 5 CATEGORY: A 0 B C D E F 2 O ARC FOAKE PROGRAM - ARC LIMITED RIGHTS STATEMENT [See page 2)
Copyright statement A license is reserved to the U.S. Govertrnent under contract DE-FCO2-NE34267 and subcontract ARC-93-3-SC-001.
O ARC CONTRACT DELIVERABLES (CONTRACT DATA)
Subject to specited excephons, 'disclosure of tNs data is restricted under ARC Subcontract ARC-93-3-SC-001.
ORIGINATOR Sfl M. H. Cooper M.TURE/DATE,L M (T)d gQ ')/2Qfq6 AP600 RESPONSIBLE MANAGER ISpiATURE' APPRO AL D TE Qp , \
E. J. PipliCa 5%) , /f 7 2 f Q, Approv.g,iney._
, manag.r s.gnie.s ih.py,, .i , eau,r.d rev,ews are compus, ei.ciron,c tie is siisoned and documenos cs s.
l AP600 DOCUMENT COVER SHEET P ge 2 Form 58202G(5/94) LIMITED RIGHTS STATEMENTS DOE GOVERNMENT LIMITED RIGHTS STATEMENT (A) These data are submitted with limited rights under govemment contract No. DE-ACO3-90SF18495. These data may be reproduced and ,
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cose newem
WESTNGHOUSE NO+ PROPRIETARY CLASS 3 AP600 Automatic Depressurization System Stage 1,2, and 3 Cold Flow Test May 1996 Authors: L.Conway M. Cooper WESTINGHOUSE ELECTRIC CORPORATION Energy Systems Business Unit Nuclear Technology Division P.O. Box 355 Pittsburgh, Pennsylvania 15230-0355 C1996 Westinghouse Electric Corporation All Rights Reserved mA2962w.non:1b-072296
l TABLE OF CONTENTS Section Title Page i I
ABSTRACT
1.0 INTRODUCTION
1-1 2.0 FACILITY DESCRIPTION 2-1
. 2.1 Major Components 2-1 2.2 Instrumentation 2-7 )
3.0 TEST DESCRIPTION 3-1 3.1 Test Matrix 3-1 l 3.2 Test Procedures 3-1 4.0 DATA ANALYSIS 4-1 4.1 Single Stage Tests 4-1 4.2 Multiple Stage Tests 4-3 l 5.0 RESULTS 5-1 5.1 Single Stage Tests 5-1 5.2 Multiple Stage Tests 5-1 5.3 Flow Distribution 5-2
6.0 CONCLUSION
S AND RECOMMENDATIONS 6-1 REFERENCES 6-2 APPENDICES A. Instrument List A-1
. B. Data Plots B-1 C. Calculations C-1 D. Data Files D-1 E. Data Validation E-1 F. Error Analysis F-1 m:\2962w.non:1b-072296 iii
LIST OF TABLES Table No. Title Page 2.1 -1 ADS Package Piping Specifications 2-4 2.2-1 List of Instruments Relevant to Cold Flow Tests 2-9 2.2-2 Differential Pressure Transmitter Installation 2-10 3-1 Summary of ADS Cold Flow Tests 3-4 5-1 Summary of Valve Loss Coefficients 5-3 5-2 Comparison of Total Flows in Multistage Tests Calculated from Valve Loss Coefficients 5-4 5-3 Adjusted Gate Valve Loss Coefficients to Normalize Flow to Same Flow as Calculated form Globe Valve 5-4 5-4 Overall Loss Coefficients 5-5 5-5 Flow Distributions in Run KV6 5-5
. i
>=
l m:\2962w.non:1H72296 iv
(
LIST OF FIGURES Figure No. Title Page 2.1-1 VAPORE Facility Configuration for ADS Cold Flow Tests 2-3 2.2-1 AP Cells Added for ADS Loop Cold Flow Tests 2-8 l
l 1
e l
l m.m.non:1b-072296 y
ABSTRACT Hydraulic characteristics of the AP600 Automatic Depressurization System (ADS) Stages 1,2, )
and 3 valve and piping package utilized in the ADS Phase B2 testing were measured with cold water at the VAPORE test facility in Casaccia, Italy. Hydraulic loss coefficients for the stage 1,2 and 3 flow paths, referenced to the 14-inch Sch.160 inlet line, were, respectively:
- [ ]*** (dimensionless). The calculated flow distribution using these loss coefficients for the three stages were, respectively
- [ ,
]*** The overall stage loss coefficients are provided for use in computer !
- l. analyses of flow distributions in the AP600 ADS 1-3. These loss coefficients must be modified ,
if different valves are used in the AP600.
i m.h.non:1b-072296 Vi
,i
i i
1.0 INTRODUCTION
i l The AP600 is a Westinghouse advanced pressurized v ater reactor (PWR) designed with plant j safety features that rely on natural driving forces, such as gravity, convection, and natural
! circulation. This plant includes an automatic depressurization system (ADS) to depressurize 4
the reactor coolant system (RCS) and initiate and maintain long-term gravity injection for core
! cooling in the event of a loss-of-coolant accident (LOCA). The ADS design consists of four flow paths, two of which are connected to the top of the pressurizer and a flow path from each
! of the two RCS hot legs. During a LOCA, the two flow paths from the pressurizer discharge
- l. steam and/or water from the RCS into the in-containment refueling water storage tank-i (IRWST) through spargers located underwater. The discharged steam is normally condensed with no increase in containment pressure or temperature. Each of the two pressurizer piping l' flow paths consists of a 14-in. pipe, which connects to three parallel paths / stages (one is 4 in.
! and two are 8 in.), forming the ADS valve / piping package. Each of these three parallel paths j have two normally closed valves in series. The three parallel paths connect to a single 16-in.
discharge line, which discharges through a sparger submerged in the IRWST. When the ADS is operated, the closed valves are sequentially opened to provide a staged, controlled depressurization of the RCS from operating conditions at 2250 psia /650 F to saturated conditions at approximately 25 psia. This staged valve opening limits the maximum mass flow rate through the sparger and the loads imposed on the IRWST, which is maintained at containment pressure. The AP600 ADS operation for each stage consists of first opening the upstream (isolation) valve, followed by opening the downstream (flow control) valve.
A full scale test of the ADS was performed at the ENEA VAPORE test facility in Casaccia, Italy. The B2 phase of this ADS test included one full scale ADS Stage 1,2, and 3 valve and piping package. The AP600 ADS test program was performed as part of a joint technical agreement among Westinghouse, ENEA, ENEL, and SOPREN/ANSALDO. A series of cold ;
water flow tests of the AP600 ADS 1-3 are documented and analyzed in this report. These l tests were performed on May 18-19,1995. Tests of the ADS at AP600 operating conditions have been reported elsewhere (References 3,4).
- The objective of these tests was to measure the hydraulic characteristics of the ADS 1-3.
Specifically, the loss coefficients for the valves and fittings in each of the three flow lines and ,
I the flow distributions when pairs of the lines and all three lines were opened were to be determined.
l l
l maassaw.non:tb-o722es 1-1 l
2.0 TEST FACILITY DESCRIPTION The ADS cold flow tests were performed at the VAPORE facility as utilized in the ADS Phase B tests with some minor modifications. The facility consisted of a steam / water supply tank, associated valves and piping, the ADS valve / piping package, a full-scale sparger, a large quench tank, facility instrumentation, data acquisition system (DAS), and facility controls. ,
Each test run was performed by filling the steam / water supply tank with cold water and l pressurizing it with compressed air. The specified ADS valves were opened, thus allowing the supply tank to blowdown through the ADS package to the sparger. A detailed description of .
, the facility and its various components is documented in Reference 2. A summary of the key portions of the facility used for the cold flow tests are described in the following sections. l
~
2.1 Major Components
- Figure 2.1-1 is a simplified flow diagram of the VAPORE facility, as modified for the ADS Cold Flow Test. The major components of the facility, which include the steam / water supply tank l (pressurizer), water supply piping from the supply tank to the ADS package, ADS va!ve/ piping i package, quench tank, sparger, and piping and valves, are described in the following paragraphs.
2.1.1 Steam / Water Supply Tank The 1412-ft.'(40-m )8 steam / water supply tank was the source of water for the ADS Cold Flow Test. The supply tank was a vertically oriented cylinder with hemispherical ends, made from low alloy steel with stainless steel cladding on all internal surfaces in contact with water or steam. The tank was equipped with electrical heaters to heat the water in the tank to the specified initial test temperatures and pressures. These heaters were not used for the Cold Flow Test.
2.1.2 Piping and Valves
- For the Cold Flow Test, the facility was configured so that water was discharged from the bottom of the supply tank. This configuration is similar to the saturated water blowdowns for the ADS Phase B1 Test. '
i Water Supply Line ;
1 A 12-in. insulated water supply line ran from the bottom of the supply tank through two gate valves (VLI-1 and VLI-2) to a 12-in. flanged connection. This 12-inch supply line was connected to the 14-inch ADS package inlet piping as shown in Figure 2.1-1. The steam !
supply line from the top of the supply tank was not utilized and was isolated with a blind flange for the Cold Flow Test.
1 mA2ssaw.non:1b-o7229s 2-1
i l
Water Supply isolation Valves VLl-1 was an Edwards 12-in. gate valve that isolated the supply tank. VLl 2 was an Atwood and Morrill 12-in. gate valve. The valves were fitted with fast-operating motor actuators that required approximately 30 seconds to stroke from the full closed to full open position or vice versa. Both valves were set to full open positions prior to the start of each test.
2.1.3 Automatic Depressurization System Package l l
. The ADS consisted of 14-inch inlet and 16-inch discharge lines, and the ADS piping / valve package (Figure 2.1-1). The piping specifications are shown in Table 2.1-1.
~
Automatic Depressurization System Valve Package inlet " piping The ADS valve inlet piping ran from the 12-in, flanged connections for the interchangeable spool piece into a 14-in. diameter line before entering into the ADS valve package. The inlet piping incorporated a prototypic loop seal to keep the ADS package upstream of the ADS valves full of water and to cool the ADS package. The inlet piping was insulated up to the top of the loop seal.
Automatic Depressurization System Valve Package The layout of the VAPORE ADS valve package simulates the AP600 ADS package and includes: a 4-in. flow path containing one 4-in. globe valve (VAD-1) and a 4-in. gate valve (VAD-4) simulating first-stage; and two 8-in. diameter flow paths, each containing one 8-in.
gate valve (VAD-2 and VAD-3, respectively) and one 8-in. globe valve (VAD-5 and VAD-6, respectively) simulating second-stage and third-stage ADS. The ADS stages were connected to the inlet and discharge piping with reducers and tees. The valve package was uninsulated.
The individual valves are described in the following paragraphs. Valves VAD-4, VAD-5, and VAD-6 were installed after completion of the ADS Phase B1 Test (References 3,4). Spool pieces, with ori,fices, were used to represent these three valves in the ADS package during the Phase B1 test.
General Requirements for Valves ADS valves were required to meet the following requirements:
. All valve motor operators were to be set to their maximum torque switch setting, or to the maximum allowable for the valve, if this value was limiting.
. The motor operator torque switch was by-passed until the valve reached 50 percent of opening travel.
m:\2962w.non:1b-072296 2-2
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- Figure 2.1-1 VAPORE Facility Configuration for ADS Cold Flow Tests m
- \2962w.non:1b-072296 2-3
3 TABLE 2.1-1 ADS PACKAGE PIPING SPECIFICATIONS Valve inlet Piping Valve Outlet Piping p Valve Package Discharge inlet Piping Stage 1 Stage 2 Stage 3 Stage 1 Stage 2 Stage 3 Piping Pipe Size (in.) 14 4 8 8 4 8 8' 16 . Pipe Schedule 160 160 160 160 80 80 80 80 , Design Temp. (*F) 680 680 680 680 600 600 600 485") 0 Design Pressure (psig) 2485 2485 2485 2485 1500 1500 1500 580) Notes:
") Discharge piping pressure and temperature rating is based on expansion bellows rated for 580 psig (40 bar).
to S
i
- No sharp edges on the seats, discs, and guides.
- The contact a,*eas on seat rings, discs, and guides were maximized to minimize the loading per unit of contact surface area.
- The bonnet cavity of each gate valve was vented to the valve body upstream of the valve seat.
- Critical compon6ats were dimensionally inspected.
After assembly, all valves were leak and cycle tested in accordance with ANSI B16.34. I i- Anchor Darling 4-in. Globe Valve (VAD-1) l The Anchor Darling globe va!'/e is a "T-type" globe valve with a full body guided plug. The valve body is designed to allow smooth tran..itionc that minimize cavitation. The trim package is a skirted swivel plug, which has full body guides and is designed to provide !!near flow . characteristics. The plug, skirt, and seat are hardfaced with stellite #6. The motor operator is a Limitorque model number SMB-1-25. 2 Anchor Darling 8-in. Gate Valve (VAD-2) i The Anchor Darling gate valve is a double disc gate valve design. The double disc 09 sign 4 utilizes wedges between the discs which strike a closing stop and force the disc against the l valve seats. The motor operator is a Limitorque model number SB-2-80. Westinghouse 8-in. Gate Valve (VAD-3) i The Westinghouse gate valve incorporates a flexible one piece wedge gate with an articulating stem to disc connection. The pWes are made of 17-4PH material and the seat and disc contacting surfaces are
- hard.aceJ with stellite 68. The motor operator is a Limitorque SB-3-100.
1 Edward Valves 4-in. Gate Valve (VALM) The Edward Valves gate valve (model number B12011) has a flexible wedge (equiwedge) design. The motor operator is a commercial quality Limitorque motor operator model number L120-20-10, which is equivalent to a nuclear quality SB-1. m:\2962w.non:1b-072296 2-5
Edward Valves 8-in. Globe Valve (VAD-5) The Edward Valves globe valve (Model B2016) is a "T-type" globe valve with a full body guided plug-piston. The valve body is designed to allow smooth flow area transitions that minimize fluid cavitation. The plug-piston and seat are hardfaced with stellite. The motor operator is a commercial quality Limitorque motor operator model number L120-800-150, , which is equivalent to a nuclear quality SB-4150. Crane 8-in. Globe Valve (VAD-6) The Crane 8-in. Flomatics AU Series (Model No. AU577) control valve is equipped with dual seats and a balanced cage guided trim package that has linear flow characteristics. The balanced trim balances the pressure above the disc with the upstream pressure, which enables the use of a smaller motor operator. The motor operator is a commercial quality Limitorque motor operator model number L120-420, which is equivalent to the nuclear quality SMB-3 model. Automatic Depressurization System Valve Package Discharge Piping The ADS valve package discharge line is a 16-in. line and contains two 10-in, line connections, each with a bellows section followed by a 90-degree elbow that connect to the I existing facility 16-in. piping to the quench tank. This 16-inch line to the quench tank runs approximately 100 ft. (30.5-m), sloping downwards to the sparger inlet in the quench tank. Two vacuum breaker valves are provided in the 16-in. line to the quench tank to prevent quench tank water from being drawn up when the flow stopped. A 16" butterfly valve is I installed in this line prior to the cold flow tests to ensure that the pipe remained full of water when discharging water. The discharge piping is uninsulated. 2.1.4 Sparger and Quench Tank The sparger consists of a vertical 24-in. stainless steel pipe with four 8-in. radial arms, each perforated with [ )" diameter holes on the upper quarters. The arms are connected to the sparger body at a ( ]" from the horizontal. The design is prototypic of the AP600 plant sparger and is mounted on a pedestal in the center of the quench tank so that the sparger arm connections are [ ]" below the normal ~ quench tank water level. The 25.1 ft. (7.6-m) diameter cylindrical quench tank is filled to a nominal depth of about 24 ft. (7.3 m), containing approximately 11,900 ft.' (337 m ) of water. The quench tank is constructed of concrete with a porous surface. mA2962w.non:1b-072296 2-6
2.2 Instrumentation The Cold Flow Test utilized the VAPORE instrumentation available for the ADS Phase B1 test ; with the addition of lower range pressure differential transducers. Differential pressure j transducers supplied by SIET, who also calibrated and installed these devices, were added to measure the pressure differentials in the ADS package for the analyses presented in this report. A listing of the relevant instrumentation, model numbers, and accuracy of equipment used during the cold flow test is provided in Table 2.2-1. Besides the differential pressure transducers, the relevant instrumentation is limited to the supply tank pressure, supply tank level, and ADS loop discharge collector pressure. Figure 2.2-1 illustrates the locations of the sensors. Table 2.2-2 summarizes the location of each differential pressure transducer and the components comprising the flow path being measured. l l 1 l I mM962w.non:1b-072296 27
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=te
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TABLE 2.21 LIST OF INSTRUMENTS RELEVANT TO COLD FLOW TESTS Manufacturer's Location Type of Specified Transducer I.D. Transducer Make/Model Range Accuracy Water Supply Tank PT-04 Pressure Rosernount 0 - 2900 psig 1 05% of full (Piezoresistive) 1144-G6000-A22 (0 - 200 bar(g)) scale LT-1 B Mass Delta P Rosernount 0 - 79380 lb 2 035 % Bellows Type 1511NPE22B1 (0 - 36000 kg)
. ADS Package Discharge Pipe PE-16W Pressure (0 - 2.5 bar(g))
ADS Loop and Components DP-67 Differential Minn-Honeywell 160 kPa 0.2% of Pressure ST 3000 calibrated span DP-78 Differential Minn-Honeywell O to 700 kPa 0.2% of Pressure ST 3000 calibrated span DP-89 Differential Minn-Honeywell -50 to 200 kPa 0.2% of Pressure ST 3000 calibrated span DP-610 Differential Minn-Honeywell -25 to 105 kPa 0.2% of Pressure ST 3000 calibrated span DP-613 Differential Minn-Honeywell -100 to 400 kPa 0.2% of Pressure ST 3000 calibrated span DP-616 Differential Minn-Honeywell O to 700 kPa 0.2% of Pressure ST 3000 calibrated span DP-916 Differential Minn-Honeywell -25 to 105 kPa 0.2% of Pressure ST 3000 calibrated span DP-1011 Differential Minn-Honeywell O to 700 kPa 0.2% of Pressure ST 3000 calibrated span
. DP-1112 Differential Minn-Honeywell -50 to 200 kPa 0.2% of Pressure ST 3000 calibrated span DP 1216 Differential Minn-Honeywell 0 to 60 kPa 0.2% of . Pressure ST 3000 calibrated span DP-1314 Differential Minn-Honeywell -60 to 100 kPa 0.2% of Pressure ST 3000 calibrated span DP-1415 Differential Minn-Honeywell O to 700 kPa 0.2% of Pressure ST 3000 calibrated span DP-1516 Differential Minn-Honeywell -60 to 120 kPa 0.2% of Pressure ST 3000 calibrated span m.\2962w.non:1b-072296 29 l
. - . - . = . .. _ - - . . - _ _ - - - .. _
- TABLE 2.2-2 i DIFFERENTIAL PRESSURE TRANSMITTER INSTALLATION Transmitter identification Location Components Between Pressure Taps DP-610 Inlet line to inlet of VAD-2 14" pipe (13.1 ft),14" elbows (2),14" tees '
(2),14" x 8" reducer (1), 8" pipe (1.0 ft) DP-67 Inlet line to inlet of VAD-4 14" pipe (19.6 ft),14' elbows (2),14" tee
- (2),14" x 8' x 4" reducer (1)
DP-613 inlet line to inlet of VAD-3 14" pipe (18.3 ft),14" elbows (2),14' x 8' ! x 4' reducing tee (1),14" tee (1), 8" pipe j (2.4 ft) DP-616 Inlet line to outlet line Depends on valve arrangement DP-1011 VAD 2 VAD-2,8' pipe (0.6 ft) DP 1112 VAD-5 VAD-5,8" pipe (4.7 ft),8" elbow (1) DP-1216 VAD-5 outlet to outlet line 8' pipe (3.8 ft),4" x 8" x 16' tee (1), 16" pipe (1.2 ft) DP-78 VAD-4 VAD-4,4" pipe (2.1 ft),4' elbow (1) DP-89 VAD-1 VAD-1,4' pipe (6.0 ft),4" elbow (1) DP-916 Outlet of VAD-1 to outlet pipe 4' pipe (0.9 ft),16" x 8' x 4" reducing tee (1),8" pipe (3.0 ft),16" pipe (1.2 ft) DP 1314 VAD-3 8" pipe (1.8 ft), 8" elbow (1), VAD-3 DP 1415 VAD-6 8" pipe (7.6 ft), VAD-6 DP-1516 Outlet of VAD-6 to outlet line 8" pipe (1.4 ft),16' x 8' x 8' tee (1),16' pipe (1.2 ft) Notes: (1) Transmitters are identified by upstream and downstream pressure tap numbers, respectively. (2) Pipe lengths were determined from the following ANSALDO drawings: (a) VAP0001DMLX2250001, Sheet 1, V.A.P.O.R.E. Plant Phase B, Isometric Main Lines, Loop ADS (b) VAP0001DMBX2260001, Sheet 1, V.A.P.O.R.E. Plant Phase B, Composite Piping, Loop ADS-Plan and Section A-A mA2962w.non:1b-072296 2-10
3.0 TEST DESCRIPTION The test matrix for the cold flow tests and the test procedures are provided in this section. 3.1 Test Matrix 4 Six tests were performed; in the first three tests, Group 1, AP measurements were made with flow through one ADS stage at a time. In the second three tests, Group 2, AP measurements j were made with flow through Stages 1 and 2, Stages 1 and 3, and Stages 1,2, and 3. The test matrix is summarized in Table 3-1. ' l 3.2 Test Procedure The general test approach for the cold flow tests was similar for both Groups of tests. For all of the tests, the pressurizer was partially filled with water at ambient temperature,15 to 20 C. The gas space in the supply tank was pressurized with compressed air to about 6.0 bar from the facility shop air system. l The 12" isolation valves, VLI-1 and VLl-2, were opened prior to the initiation of the test. Then the appropriate gate valve for the stage (s) being tested was opened. Opening of the globe valve (s) in the stage (s) being tested initiated the tests. Blowdown was terminated for all the tests by closing VLI-1. Data acquisition was started 5 seconds before the opening of VLI-1 for all the tests. The test procedure is slightly different for each of the two groups of cold flow tests. These j test procedures are summarized below: Group 1 Test Procedure
- 1. The pressurizer is filled with demineralized cold water. The water inventory will be at
. least 15 metric tons of water.
- 2. Open VLI-2.
- 3. Check all other ADS valves are closed.
- 4. Open vent valves VSR-1 and BKV-344 to allow venting of 12" water feed line and ADS Loop.
- 5. Open gate valve of the involved stage.
m:\2962w.non:1b 072296 3-1
- 6. Open the VWM valve and keep filling up the ADS Loop with cold water. When water keeps exiting through VLM-X, then close VLM-X.
- 7. Fill the 12" line and the loop. When water exits through BKV-344, then close BKV-344.
- 8. Fill up the 12" line and ADS Loop. When water exits from VSR-1 line, then close VSR-1.
- 9. Increase the pressure of the air bubble in the pressurizer by introduction of
. compressed air, until the maximum compressed air pressure is reached (typically ranging around 6 - 7 bar g). ~
- 10. Check and record the VR 1.2 position (butterfly valve on the discharge line).
- 11. Open VLI-1.
- 12. Open the GLOBE valve of the involved ADS stage to initiate the flow.
- 13. Wait until at least the " TEST TIME" of Table 31 has elapsed. For the Group 1 Test runs, the Test Time starts when the GLOBE VALVE reaches the full open position.
When Test Time has elapsed, then activate the command "close" to the Globe Valve of the involved stage.
- 14. Close VLl-1.
Group 2 Test Procedure
- 1. The pressurizer is filled with domineralized cold water. The water inventory will be at least 15 metric tons of water. The VLI-1 and VBR-1 valves must be closed.
I
- 2. Open VLl-2.
- 3. Check all ADS valves are closed.
- 4. Open vent valves VSR-1 and BKV-344 to allow venting of the 12" water supply line j and the ADS Loop.
- 5. Open the VWM valve and keep filling up the ADS Loop with cold water.
- 6. Fill the 12" line and the ADS loop. When water exits through BKV-344, then close BKV-344.
l m:\2962w.non:1tF072296 3-2
- 7. Continue filling the 12" line and ADS Loop. When water keeps exiting from VSR-1 line, then close VSR 1.
- 8. Increase the air bubble pressure in the pressurizer by introduction of compressed air, until the maximum compressed air pressure is reached (typically ranging around 6 - 7 bar g).
- 9. Check and record the VR 1.2 position (butterfly valve on the discharge lins).
. 10. Open ALL ADS VALVES OF THE STAGES BEING TESTED.
- 11. Check other ADS valves are closed (if applicable).
- 12. Open VLI-1 and initiate the flow.
- 13. Walt until at least the " TEST TIME" of Table 3-1 has elapsed. For the runs of Group 2, the Test Time starts when the command "open" is launched to VLl-1.
When Test Time has elapsed, then activate the command "close" to the VLI-1. l A m:\2962w.non:1b-072296 3-3 i
l TABLE 3-1
SUMMARY
OF ADS COLD FLOW TESTS Involved Test Run No. Stage (s) Time (s) Operative Sequence (Main Lines) Group 1 KV 1 1 120* Pre-open VLl-2 and VAD-4; Open VLI 1 + VAD-1; Terminate: Close VAD-1 + VLl 1
. KV 2 2 30* Pre-open VLl 2 and VAD-2; Open VLI-1 + VAD-5; Terminate: Close VAD-5 + VLl-1 KV-3 3 30* Pre-open VLI-2 and VAD-3; Open VLI-1 + VAD-6; Terminate: Close VAD-6 + VLI-1 Group 2 KV-4 1+2 15" Pre-Open VLI-2 + VAD-1 + VAD-4 + VAD-2 + VAD-5; Open VLl-1; Terminate Close VLI-1 KV-5 1+3 15" Pre-Open VLl-2 + VAD-1 + VAD-4 + VAD-3 + VAD-6; Open VLI-1; Terminate: Close VLI-1 KV-6 1+2+3 15" Pre-Open VLI-2 and all ADS valves; l
Open VLI-1; Terminate: Close VLi-1 Time starts when ADS globe valve reaches 100 percent stroke. Time starts when VLl-1 reaches 100 percent stroke. l l i I m:\2962w.non:1b-072296 3-4
l 4.0 DATA ANALYSIS The methodology used to analyze the cold flow test data is described in this section. l 4.1 Single Stage Tests The loss coefficients for the segment of the ADS between each set of the 13 differential , pressure transmitters installed in the test facility were calculated based on the Darcy equation l' for fluid friction loss-i l 2 AH = Kv {4,1) 2g where: K = loss coefficient (dimensionless) AH = pressure loss, ft. of fluid V = velocity, ft/sec. I g = acceleration of gravity = 32.2 ft. sec.8 Substituting English engineering units in equation (1) results in equation (2) for the pressure drop: AP = K(F)2 (4-2) 2 x 144 x g x p x A8 4 Or rearranging to solve for K and substituting the values for g (32.2 ft/sec. ) and p (62.5 lb/ft. for water at 20 C), Equation (4 2) becomes: K = 579,600 A8 AP (4-3) F2 where: A = area of pipe, ft.8 AP = pressure drop, psi F = flow rate, Ib/sec. mes2w.non:1b-0722se 4-1
1 l i Since the experimentally measured loss coefficients, K7, includes a valve and piping, or in some cases, a valve, piping, and fitting (such as 90 elbow, reducer, or tee), the loss coefficient for each valve was calculated by subtracting the loss coefficients for the piping and the pipe elbows included in the differential pressure measurement. This relationship is stated by the following equation: K, = K1 - K, - K g @-9 0 where: K, = loss coefficient for valve Kr = loss coefficient for total segment measured K, = loss coefficient for the piping Ke = loss coefficient for elbows The loss coefficients are expressed in numbers of velocity heads and are therefore dimensionless. l The loss coefficients for the straight runs of piping were calculated using the Moody charts published in Reference 1. The fluid Reynolds number was determined from the flow and pipe dimensions as follows: Dup Re (4-5) p where: Re = Reynolds number, dimensionless D = pipe diameter, ft.
~
u = fluid velocity, ft/sec. p = fluid density, Ib/ft.8
= fluid viscosity, Ibm /ft.-sec.
The friction factor, f, was obtained from the graphical correlation of f with Reynolds number on page A-24 of Reference 1. m:\2962w.non:1b-072296 4-2 1
The loss coefficient for the pipe was then calculated from equation (4-6): K' - f _l_ (4-6) D , where: K, = loss coefficient for pipe (dimensionless) f = friction factor (dimensionless) . L = length of pipe, ft. g D = pipe diameter, ft. The loss coefficients for the 90 degree elbows were calculated using the equivalent lengths of
<v r 8 l 7
the elbows - , correlated as a function of relative bend ratio on page A-27 of l S> S> Reference 1. This relationship is given by equation: , l e v K,-f _L (4-7) S> where: f = friction factor at flow conditions in pipe (dimensionless)
<g v equivalent length of elbow, number of pipe diameter Si Kg = loss coefficient for elbows (dimensionless)
I - relative radius, radius of bend / pipe diameter
- . D 4.2 Multiple Stage Tests When two or more stages of the ADS were open, the pressure drop across the open valves in each stage and their previously measured loss coefficients were used to calculate the flow I rate through each stage. The flow rate through the nth stage is calculated from i equation (4-8):
l muss 2w.non:1b-072296 4-3 i
579,000 A2 3 p, (4-8) F" = Kyn) ( , The percentage of the total flow through each stage is then computed from equation (4-0): F
%F= n ," x 100 g)
{f n=1 n j s Flow rates through each stage are calculated individually from the loss coefficients for each of the two valves in each stage during the blowdown transient to obtain a comparison between the flows predicted from globe valve versus gate valve loss coefficients. The total flows - predicated using the valve loss coefficients are compared with the measured flow rates. The results of these analyses are summarized in Table 5.1-1. Details of the analyses are provided in the spreadsheet, Table C-3 provided in Appendix C. An attemative analysis is based on the calculation of the overall loss coefficient for the multistage tests. The experimental value for the overall loss coefficient is then compared with the overall loss coefficient calculated from the individual stage loss coefficients measured in the first group of experiments. The overall loss coefficient for two parallel flow streams is calculated from the individually ; measured loss coefficients by the following equation: l 1 K= 1 1 1 (4-10)
-+2 +-
K, ) Ki K, K2 e , where: i K,, = overall loss coefficient (dimensionless) K, = loss coefficient for stage 1 (dimensionless) K2= loss coefficient for stage 2 (dimensionless) i l m:\2962w.non:1b-072296 4-4
1 l For three stages, the equation defining the overall loss coefficient becomes: 1 4 1 1 1 1 1 1 (4-11)
-+2 +2 +2 +-+- 1 KK ) KK KK '
K, T i 2 i 3 $ 2 3 K3 K3 l Derivations for equations (5-10) and (5-11) are presented in Appendix, C1. where: l Ko = overall loss coefficient (dimensionless) K, = loss coefficient, stage (1) (dimensionlese) K, = loss coefficient, stage (2) (dimensionless) K3= loss coefficient, stage (3) (dimensionless) I Equations (4-10) and (4-11) are valid only when the diameter of the pipe upon which the loss ; coefficients are the same. If different diameter pipes are used for each loss coefficient, the j equations would become very complicated with terms representing the ratios of the individual diameters. For this reason, the loss coefficients for the three ADS stages in this analysis were referenced to the 14-inch ADS valve / piping package inlet line. l l l l O i mM962w.non:1b-072296 4-5
l l l 5.0 RESULTS The results of the data analyses described in Section 4.0 are presented in this section. 5.1 Single Stage Tests Loss coefficients were calculated for the six ADS valves from the data obtained in the single stage flow test, KV1 through KV3, using equations _ (4-3) through (4-7). For each valve, the loss coefficients were calculated at three times during the test period. The data was averaged over a 1.5 second interval (data was obtained at a frequency of 1000 times per second and reduced to 0.25 second intervals by the data reduction program). The calculated loss coefficients, their standard deviations, and 95 percent confidence limits are summarized in o Table 5-1. Details of the calculation are contained in the Appendix, Table C-1. The loss coefficients for the Anchor Darling and Edwards globe valves are in the range expected for globe valves. The loss coefficient for the Crane globe valve is about three times higher than the other two globe valves because of its double-seat configuration, which causes a higher pressure drop. Loss coefficients for the Edwards and Westinghouse gate valves were [ ]'** while that of the Anchor Darling gate valve was [ ]'"# which is the expected range for these lower resistance valves. 5.2 Multiple Stage Tests Flow rates through each stage were calculated for each of the test runs, KV4 through KV6, where flow through multiple ADS stages occur. The loss coefficients determined from the single stage tests described in Section 5.1 were used for these calculations. The total loss coefficient measured across the valve, piping, and fitting between pressure taps was used for this analysis to eliminate uncertainties introduced by the use of published data for fitting and piping resistances. The individual flows through each stage were calculated using the loss coefficients for both the globe valves and gate valves. The calculated flows using the globe valve loss coefficients and the gate valve loss coefficients were individually summed and compared with the measured total flow in Table 5-2. Details of this analysis are provided in 2 the Appendix, Table C-2. Total flows calculated from the individual globe valve loss coefficients agree closely with the measured flow rate. The total flows calculated from the gate valve loss coefficients in two out of the three runs were less accurate. In addition, the deviation for the flows based on the gate valves are much larger than average deviation for the glove valve. The globe valve loss coefficients result in more accurate flow estimates because their magnitudes are five to ten times greater than the gate valve loss coefficients and therefore are less sensitive to small errors in pressure drop measurements. The flows calculated from the gate valve loss coefficients are very sensitive to small changes in these coefficients, as shown in Table 6-3. In this table, the gate valve loss coefficients necessary to yield the same flow as the globe valves are compared with the measured gate valve loss coefficients. These changes are I mA2962w.non:1b-072296 5-1
1 l l small in absolute magnitude and can occur from some consistent systematic difference, such i as incomplete bleeding of the sensing line to the differential pressure transmitters. Because the mass flow is calculated based on the change in measured level in the water supply tank, a small change in measured level results in a large change in the flow rate. Apparent flow oscillations occurred in Run KV1 and KVS, which may have been caused by an indicated level change resulting from a wave with a 10 to 12 second frequency in the water supply tank. The amplitude of tnis wave is much gieater in KV5 than in KV1 (pages B-47 and B-8, Appendix B). The effect on the analysis of Run KV1 is negligible because the amplitude
, was small. However, the anomalous results for the total flow in Run KV5 probably were caused by this indicated flow instability. The loss coefficients for this test were calculated based on pressure drops at 60 seconds, which was near the peak of the indicated flow oscillation. The flow rate probably did not really vary, since the difference in liquid head was only a few inches of water.
This level oscillation may have been caused by a reflected pressure wave that occurred when the ADS piping was initially filled or when flow was initiated. The main 12-inch valve was opened to fill the loop while the globe valve of the loop being tested was closed. The test procedure also required introducing compressed shop air at six to seven bar into the pressurizer. Either of these actions could initiate the wave in the pressurizer resulting in the apparent mass flow oscillation. Overall loss coefficients for each stage and for the multiple stages were calculated from the measured flow and the total pressure drop (DP616). The flows and pressure drops were averaged over the same 1.5 second interval used in the previous analyses. Table 5-4 , summarizes the measured overall loss coefficients for the individual and multiple stages and j the calculated overall loss coefficients using the individual stage loss coefficients and j equations (4-10) and (4-11), Section 4. Details of this analysis are shown in the Appendix, l I Table C-3. The overall multistage loss coefficients determined from the experimental data agree closely with these calculated from the single stage loss coefficients, with the exception I of Run KV5. i 5.3 Flow Distribution l The flow distribution among the three stages in Run KV6 was calculated by two methods:
. Loss coefficients for each globe valve and its measured pressure drop were used to calculate the flow in each stage.
- The measured overall loss coefficient for each stage was used to calculate the flow distribution directly.
The results of these analyses which agree within 14 percent, are compared in Table 6-5. Details of the analysis are provided in the Appendix, Section C-4. m:\2962w.non:1b-072296 52
t _ n - i e - i c f f e o _ C 5 9 - - S . T _ . S _ E 7 4 2 1 2 9 T 1 0 0 0 0 1 E a 0 0 0 0 0 0 G 1 1 1 i i 1 A _ T S - E L _ G _ N I S S _ T ~ _ N 1E I 5C I EF , LF K BE AO TC - _ _ S S O _ L _ E _ V L A V _ F O _ Y _ e R p g g A y in in e s M T l r l r u M ) a a o ) ) U '4 D (
)D
'8 r
)h 8g
) s
'4 d
'8 s (d r
'8
( S r eo b h ( o eh (in et s ( r e a e a bn ee - bw w anc o _ - lo cn t t ae t ad id loar _ GA GA GW GE GE Gc i . e 1 2- 3- 4- 5- 4 _ l v D D D D D D a A A A A A A V V V V V V V n Blyi{UE u6
.l ! ll lll (Illl. l l ll!::I
l l TABLE 5-2 COMPARISON OF TOTAL FLOWS IN MULTISTAGE TESTS CALCULATED FROM VALVE LOSS COEFFICIENTS Measured Calc. Flow, Calc. Flow, Flow, Globe Valve Gate Valve, Run Ib/sec lb/sec % Diff.* lb/sec % Diff.* KV4
- ~
-0.6
*** 25.6 KV5 -12.7 2.6 1
KV6 + 8.1 92.2 ' Calc. Flow - Meas. Flow'
*% Diff. = x 100 l Meas. Flow ,
TABLE 5-3 ADJUSTED GATE VALVE LOSS COEFFICIENTS NORMALIZED TO SAME FLOW AS CALCULATED FROM GLOBE VALVE Run Single-Stage Tests Normalized KT KI KV4 Stage 1
- ~
Stage 2 KV5 Stage 1 Stage 2 KV6 Stage 1 Stage 2 Stage 3 _ _ _ _ m:\2962w.non:1b-072296 5-4
TABLE 5-4 OVERALL LOSS COEFFICIENT (Referenced to 14-inch Main inlet Line) K. K, (Calculated from Single-Run (Exp. Data) Stage Loss Coefficients) - KV1 -- KV2 -- KV3 - KV4 *** KV5 KV6 _ _ I l TABLE 5-5 FLOW DISTRIBUTIONS IN RUN KV6 i
% Flow i
Calculated from Overall Stage Calculated from Globe Valve Loss Coefficients Loss Coefficients % Diff. Stage 1
*** 14.0 Stage 2 2.9 Stage 3 _ _ _ _
0.6 m:\2962w.non:1b-072296 5-5 l l
l
6.0 CONCLUSION
S AND RECOMMENDATIONS The flow distribution through the three stages of ADS 1-3 calculated using the overall loss coefficients for these stages measured with single phase, room temperature water are: Loss Coefficient Flow % (Dimensionless) Stage 1: *** ***
- Stage 2:
Stage 3: _ _ _ _ Calculation of the flow distribution from the overall stage loss coefficients is recommended in preference to using valve loss coefficients. Gate valve loss coefficients are inherently very low, leading to large flow variations from small measured pressure differences. Globe valve loss coefficients are larger and result in more accurate flow predictions. However, the overall stage loss coefficients result in the most accurate analyses of the system flow distributions, since the effects of piping, bends, and fittings are included in these coefficients. The overall loss coefficients and flow distributions can be modified if other model valves are ! used in later designs of the ADS. In this case, published data can be used for the replacement valve while the measured loss coefficients can be used for the unchanged j I stages, if the replacement valve is the same as one tested, then the measured loss coefficient reported herein should be used. ! There appears to be a systematic error in the measurement of the pressure drop across the 9 ate valves in the single flow path tests of stages 2 and 3, which leads to small overprediction i of the flow through these stages in the multiple stage tests. Insufficient data are available to determine the source of this error. The water supply tank level should be monitored in any future tests of this nature to be sure that the water level is stable after the loop is filled and the compressed air has been introduced. This precaution may eliminate the level oscillations that were recorded as mass i , flow oscillations in Run KV1 and KV5. l l m:\2962w.non:1b-072296 61
REFERENCES
- 1. " Flow of Fluids Through Valves, Fittings, and Pipe," Engineering Division, Crane Co.,
Chicago, Technical Paper No. 410, thirteenth printing,1973.
- 2. WCAP 14303, " Facility Description Report, AP600 Automatic Depressurization System, i
Phase B1 Tests," V.V. Miselis, A.J. Brockie, J.S. Nitkiewicz, March 1995.
- 3. WCAP-14324, " Final Data Report for ADS Phase B1 Tests," April 1995.
i s
- 4. WCAP-14305, "AP600 Test Program, ADS Phase B1 Test Analysis Report," H. C. Yeh, et al., June 1995.
i 4 -1 J 4 1 ) i l # 1 1 4 1 1 m:\2962w.non:1b-072296 6-2
I
'l l
l l I b APPENDlX A INSTRUMENT LIST l l i 1 1 P-l l l l mMb.non:1b-072396 A-1
- .. __._m _ _ _ . _ _ _ _ _ _ _
3-TABLE A-1 INSTRUARENT UST cr 2 Ch. l.D. Description Full Scale Signal Reference EWV Pref RAsin Excitation Offset g No. out Trened. Gain (EU) 1 26 DP6-7 DP between PT6W & PE7W 0-3 bd 1-5V Obd=1V 0.7501 1 1 WA -0.7505 27 DP7-8 DP between PE7W & PE8W 0-3 bd 1-SV Obd=1V 0.7497 1 1 N/A -0.7500 28 DP8-9 DP between PE8W & PE9W 0-7 bd 1-5V Obd=1V 1.7495 1 1 N/A -1.7426 29 DP9-16 DP between PT9W & PT16W -1.345.7 bd 1-5V Obd=1V 1.7503 1 1 N/A -3.0492 30 DP6 DP between PT6W & PT10W 0-2 bd 1-5V Obd=1V 0.4999 1 1 N/A -0.5001 39 DP10-11 DP between PT10W & PE11W 0-k bd 1-SV Obd=1V 0.5000 1 1 N/A -0.5005 40 DP11-12 DP between PE11W & PE12W 0-7 bd 1-5V Obd=1V 1.7516 1 1 N/A -1.7654 41 DP12-16 DP between PE12W & PE16W -1.345.5 bd 1-5V Obd=1V 1.7012 1 1 N/A -3.0041 42 DP6-16 DP between PT6W & PE13W 0-7 bd 1-SV Obd=1V 1.7505 1 1 N/A -1.7527 43 DP6-13 DP between PT6W & PE13W 0-2 bd 1-5V Obd=1V 0.5001 1 1 N/A -0.4994 44 DP13-14 DP between PE13W & PE14W 0-2 bd 1-SV Obd=1V 0.5002 1 1 N/A -0.5004 45 DP14-15 DP between PE14W & PE15W 0-7 bd 1-SV Obd=1V 1.7506 1 1 N/A -1.7485 46 DP15-16 DP between PE15W & PE16W -1.345.7 bd 1-5V Obd=1V 1.7498 1 1 N/A 4.0484 77 LT1B Kg. of Water in Pzr. 0-36000 3-1V Okg=3V -17606.66 N/A N/A N/A 52819.96 126 TE6W 14* Water Supply for ADS 0-400*C Non- Type 9 N/A 1 400 N/A 0 Piping linear _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ . _ _ _ _ _ _ _ . _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ ________________________ __ _. _ _ ___ _____j
" "- -=& *- 4m,+=e4 um . m -
a- + a mg,y _ ,g_ m I i i 1 I + l i e APPENDIX B DATA PLOTS l 1 i I o i I i 1 i l I m.W.non:1b-072396 B-1
- Data Charts for KV1 O
m.Rb.non:1b472396 B-2
1 i i I l
'1 l
i Data Charts for KV2 i O m.MJ.non;1b-072396 g.g
1 5 I 4 i ? '. 1 i i 1 . 4 ? I i t f 1 i 4 e, Data Charts for KV3 , t 1 i a 9 k 4 d 4 't, 4 s m sess o m 1 w 723es B-17
l I i r i i k i 1 i l l Data Charts for KV4 l l 1 1 l l 9 mM962a_b1.non:1b-072396 B.24
1 i i I I i Data Charts for KV5 i i j O I i m.W1.non:1H72396 B-36
Data Charts for KV6 O m.6:1b 072306 B-48 l l l .
w _ A._ & m' h4am.444,4..a-,.- a.s.a 4-.. 4.4m a. aAa t Jm..a.4 .,em.Ga4 A .uu 5m _.aA . -.aa a_m A r . @. .A.._ 4.-..J,s.- 4 __.,_._s gaaa a i a l l 1 i I APPENDIX C CALCULATIONS l 9 l 1 i i
)
NM.f.non:1b-072396 C-1
C-1 Derivation of Parallel Path Flow Equations
- 1. For two parallel paths:
The total flow is: Fr - F, + F, (C-1) Since the two lines are in parallel, the pressure drop across each line is equal to the overall pressure drop: AP7 = AP,- AP, (C-2) The flow in each line and the total flow is related to the pressure drop and loss coefficients as defined below: AP (C-3) F" = 3 K, ll. For three parallel paths: The total flow is: Fr = F, + F, + F, (C-7) m.M_f.non:1tF072396 C.2
I Similarly to the derivation for two parallel paths, the expression for flow can be substituted into the definition of the overall loss coefficient: AP , AP (C-8) 4 - (APF): (p,. p,. p,): 7 p,2 + 2F F, + 2F,F, + 2Fa F, + Fa' + F'3 3 Substituting the expression for F and cancelling the AP term as before, we obtain: 1 4 1 (C-9) 1
+2 1
+2 1
+2 1
+ +- 1 K, 3 K,K, 3 K,Ka 3 K,K3 K, K3 masac_f.non:1b-0723es C-3
l l e , s ~ ie _ Vm Kd s s le Em Kd s s le Pm Kd s e i e Tm Kd t ef e r q Ae 3-1 e S f s D ie A m F d O S T
. . s 7
T oe N% W e ?. O Rd L F D cc L E oes O G le/ C A Vf t F T O S S E t I S L gf, Y G nn L N I ii t iq t A S FE N A
- et 2- ip f, C PI n E
L B t A f, T em pa ii Pd . . c we o/ s l FI h P . e t t l ee Dp ~ _ e 0 5 0 0 5 0 iemc 0 1 2 1 5 1 0 1 2 1 5 1 0 5 0 7 0 5 0 6 0 7 5 5 5 6 5 7 5 5 5 6 5 7 Ts o 1 2 4 5 N 8 9 1 1 1 1
. 7- 8- 0 1 3 4 t 1 1 1 1 s P P P P P P I
n D D D D D D o N 1 2 3 n V V V u K K K 5 4 6 R 8 8 8 ag[=:hghwE A (
l l l1ll
~
f f i D c e
/s he l t
, a FG c
e
/ se . l hb o 3- ,l 1 FG S
- D **
A F O f f S t e i D T Ta S KG % E T W E O G S L F A e W T b O e D S o t L E Tl L F a O L KG G C P L F I A T T O L
,t O
S U aF T f f i I S M e . r q D Y AS % L l A i N s p A
- P e e b
3- l t ea l o C DG G E L i B s p A P beo T s . l e el - e _ DG M . e 4 5 6 g n V V V t a u K K K S 1 2 1 3 1 2 3 R e mc ie 0 5 0 5 0 C 0 6 0 5 0 5 0 5 Ts o N 4 V 5 6 n V V u K K K 7 8 9 - R 8 8 8 - 3 C g o4 1
E O 11 li 2 l # 8 II l e s e . i 11 9 8 8 s 5 m
!! I
5 l l1 l a 3 l
- ll I 9 s s s s s I
.g I = = s e = s E E E E E E i
5 - ~ e , , . b k h ! h b mA2962c f.non:1b-072396 ' C.6
C-5 Calculation of Flow Distributions A. From Flows Calculated for Globe Valve Loss Coefficients F
% Flow = ," x 100
' [ F, Stage 1 [ ] ** c Stage 2 [ ] ** c Stage 3 [ ] ** c B. From Flows Calculated for Single Stage Overall Loss Coefficients a
% Flow - 3 E F, ni Stage 1 [ ] **e Stage 2 [ ) **x mA29s2c_f.non:tb-omse C-7
Stage 3 [ ] *** C.' From Overall Loss Coefficients F, = $=@ 1K, s K. 3 3 Fr -E @ 1k n+1 %
%F = .F" x 100 F..
r g 1 1
= x 100 = x 100 3 3 M[ 1K, [ 1K, n-i 3 .., 3 K, = [ f** K=[ 2 f*# K=[
3 f** Stage 1 m 2ssac_f.non:1w723es C-8
Sb,C Stage 2
**e Stage 3 Note: Methods shown in B and C are the same since the AP in B cancels, resulting in same mathematical form as C.
mA2962c_f.non:1b-072306 C-9
APPENDIX D DATA FILES mA2962c_f.non:1b-072396 D-1
The data are stored in tl;e following AP600 files: a prsgkv1.txt 1798 tape blocks a prsgkv2.txt 842 tape blocks a prsgkv3.txt 924 tape blocks a prsgkv4.txt 925 tape blocks a prsgkv5.txt 926 tape blocks a prsgkv6.txt 926 tape blocks mN2962c_f.non:1b-072396 D-2
- - - . - ~ ~ . . - . - . . _ , _ . _ , , _ . - , , _ _ _ , . _ , _ , _ _ _
i i l 1 l APPENDIX E I DATA ANALYSIS TECHNIQUES AND EVALUATION
\ . i l
I m.M_f.non:15072396 E-1
This appendix describes the data reduction and analyses performed (in Pittsburgh) on the data recorded during the Phase B1 testing. The Prosig data were recorded at a high sampling rate. In order to reduce the volume of data, a process was developed to decimate these data files. E.1 Data Reduction Techniques After the data was recorded on the data acquisition systems, the data files were copied onto a CD disk for permanent storage. The Prosig data files were also in binary format and the
. Prosig analysis software was used to analysis this data. Time-history traces were generated
. for all the data.
E.1.2 Prosig Data The Prosig analysis software was used to analysis and generate time history plots of the raw data recorded at 1000 sps (samples per sec). In addition, power spectral density (PSD) plots were generated for the quench tank pressure data (PE09-PE20). Prior to plotting the time-history data, the Prosig software was used to shift the time axis of each transient.' Time-zero in the raw data files corresponded to the start of data collection not the start of transient or valve actuation. One of the Prosig data channels recorded the trigger signal to start the valve actuation. This channel was analyzed to determine the exact time when the valve actuation started. This point in time was set to zero. Therefore, time-zero corresponded to the start of valve actuation. The 16 channels of thermocouple data (TE1W - TE16W) were low pass filtered at 40 Hz prior to plotting and data processing. The low pass digital filter was based on a recursive second order Butterworth filter model with a 48dB/ octave cut-off rate. Only channel 126 - TE6W was plotted and used for the cold flow tests. After plotting the time history traces at 1000 sps, the Prosig software was used to decimate the data and generate 136 ASCil files (one for each data channel) containing a single column
. . of numbers representing the channel amplitude in engineering units at 4 sps. This decimation was accomplished in the Prosig software by first integrating the time history trace, then decimating (i.e., save the first data point,250th data point,500th data point and son on) the integrated curve and differentiating this decimated integrated curve to obtain the original time history with an equivalent sampling rate of 4 sps. The area under the integrate curve remained constant by using this process to decimate the data. The results of this process were 136 ASCll files, which contained a time history at 4 sps. However, only 14 channels were generated (one temperature and 13 differential pressures for the cold flow tests).
One additional ASCll file was generated for the mass flow rate based on the data for LT-1B (mass in of the supply tank in kilograms). These data were processed using the Prosig
- analysis software to obtain the mass flow rate by differentiating the fluid mass in the supply m:\2962c f.non:1b-072396 E-2 I
tank. The raw 1000 sps data for LT-1B was also integrated and decimated similar to the process previously described. However, to obtain a smooth representation of the mass flow, the data were integrated, then decimated to an equivalent sampling rate of 0.5 sps. The next step in the process was to differentiate once to obtain the mass flow at 0.5 sps, then differentiate a second time to obtain the mass flow rate. The Prosig software was used to interpolate between successive data points to add data points (or effectively increase the sampling rate from 0.5 sps to 4 sps) using a spline function. In addition to the 136 ASCll files previously generated, one ASCll (referred to as channel 137 on the Prosig data) file was generated for this channel representing the mass flow rate. Electronic files of all the Prosig ASCll data at 4 sps were produced and archived. E.2 Data Evaluation A Day-of-Test report was issued which contained preliminary calculations of the valve loss coefficients. The loss coefficients were compared with published data as a preliminary evaluation of the validity of the test results. E.3 Pressure Drop Consistency Evaluation To test the validity of the pressure drop measurements, the sum of the individual pressure drops measured for each segment of each of the three stages in Run KV6 are compared with the measured overall pressure drop in Table E-1. The sums of the individual pressure drops compare within 2% for Stages 1 and 3, and differ by 6.8% for Stage 2. The reason for the discrepancy in Stage 2 may result from the location of some of the pressure taps adjacent to elbows or reducers which did not allow full pressure recovery prior to the measurement. mA2962c_f.non:1b-072396 E-3
l ll e c. b. c a n e r f e M f i D d i s p P A 4 I1 6 V
. K d i
N a p U R ,
- P A
S P O R D E d i R s p U S c P 1 S e A
- E s ER EP 0
5 L BD = A E e TR U i m i d a S T p A , E P M A F O N O d S i I R s p A , P P M A O C d i
. s p
P A M e g t a j 2 3 S Hl{, !{M$ mA 1l
h! APPENDIX F ERROR ANALYSIS e-t massac_f.rm1b-o72ae6 F-1
Loss Coefficient The equation for the loss coefficient can be written as: K =CAPF-2 (F1) If the partial derivative of this equation is taken relative to the error, E, the following equation is obtained for the maximum error in the loss coefficient: 2&F BK/8E = BAP BE dE Since the error resulting for the calibration of the pressure transmitter is 0.2% full scale, and most of the pressure differentials were at mid-scale: BAP/DE - 0.4% BF/DE = 0.35% (from WCAP-14324, " Final Data Report for ADS Phase B1 Tests," April 1995, Table E-2,
- p. E-18, Channel 77) '
Loss Coefficient Total Error = 0.4% + 2 x 0.35% , = 1.15% Flow Distribution
%F,= ,"
E F, 1 m wes2c_f.non:1b-o7230s F2
for n=3 f 3 B(%F) , BF, a BE DE BE n.i F", B(%F,) , 43F, dE BE since F, = C AP,'" K,'" BF, 1 BP 1 BK BE ~ Y BI YE DP/&E - 0.4% OK/dE = 1.15% BF, / BE = 1/2 x 0.4 + 1/2 x 1.15
= 0.2 + 0.6
-0.8%
a(%F,)
= 4 x 0.8 = 3.2%
BE mA2962c_f.non:1b-072396 F-3 an}}