ML20237D285
| ML20237D285 | |
| Person / Time | |
|---|---|
| Site: | 05200003 |
| Issue date: | 08/31/1998 |
| From: | WESTINGHOUSE ELECTRIC COMPANY, DIV OF CBS CORP. |
| To: | |
| Shared Package | |
| ML20237D283 | List: |
| References | |
| WCAP-14138, WCAP-14138-R02, WCAP-14138-R2, NUDOCS 9808250295 | |
| Download: ML20237D285 (350) | |
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WESTINGHOUSE NON-PROPRIETARY CLASS 3 FLNAL WCAP-14138 Rev.2 , FINAL DATA REPORT - . FOR l PCS LARGE-SCALE TESTS, PHASE 2 AND PHASE 3 1 l August 1998 m:\3578w.non:lb-082098 Rev.2
FINAL . 1
;i l
l 1 TABLE OF CONTENTS Section Title Ea.ge., S UMMARY . . . . . . . . . . . . . . . . . . . . . . . . . . . ......... .................... I
1.0 INTRODUCTION
. . . . . . . . ........................................... 1-1 1.1 Test Objectives ............... ....... ....................... 1-5 j 1.2 Facility Scaling ....................... .... ................... 1-6 3 1.2.1 Test Vessel . . . . . . . . . . . . . . . . . . . . . . .... ...... ....... 1-6 i 1.2.2 Heat Sinks . . . . . . . . . . . . . . . . . ..... .......... ... ...... 1-7 1.2.2.1 Short Term Heat Sinks .. ........................ 1-7 1.2.2.2 Long Term Heat Sinks .. ... ................ ...... 1-8 1.3 Test Matrix . . . . . . . . . . ... ................. .. ...... ...... 1-9 1.3.1 Phase 2 Test Matrix . . . . . . . . . . . . . . . . . . . . . . . . . ............ 1-9 1.3.2 Phase 3 Test Matrix .......................... .... ..... 1-11 1.3.2.1 Test Series 222 . . . . . . . . . . . ............. .... . . . 1-11 1.3.2.2 Test 223.1 . ..... ......... .............. .... . 1-12 1.3.2.3 Test Series 224 . . ............................. . . 1-12 i 1,
2.0 TEST FACILITY DESCRIPTION . ..... ....................... ...... 2-1 2.1 Facility Component Description . . . . . . . . . . .......................... 2-6 2.1.1 Foundation and Tower . . . . . . . ..................... ..... 26 2.1.2 Pressure Vessel . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . ........ 2-6 2.1.3 Steam Supply. . . . . . . . . . . . . . . . . . ......................... 2-7 2.1.3.1 Facility Steam Supply . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 27 2.1.3.2 High Capacity Boiler . . . . . . . . . . . . . . . . . . ............. 2-7 2.1.3.3 Steam Injection . . . . . . . . . ...... .......... ........ 2-8 2.1.4 Vessel Internals . ......................... ............. 2-8 2.1.4.1 Baseline Test Series .................. ..... ..... . 2-8 2.1.4.2 Phase 2 and Phase 3 Test Series . .................... . 2-9
' 2.1.5 ' Condensate Handling . . . . . . . . . . . . . . . . ...... ....... ...... 2-10 2.1.6 External Cooling Annulus and Air Ducting . . . ................. 2-10 2.1.7 Axial Fan . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2- 1 1 2.1.8 Helium Addition . . . . . ....... .. ........ .. ... ...... 2-11 l
2.2 Instrumentation and Measurements . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .... 2-20 i .2.2.1 Condensate Flow . . . ......... ..... ............ ... . . 2-20 2.2.2 Pre ssu re . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . ...... 2-20 2.2.2.1 Vessel Pressure . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2-20 2.2.2.2- Steam Inlet Pressure . . . . . . . . . . .. ................. 2-21 2.2.3 Wind Speed and Direction . . . . . . . . . . . . . . . . . . ... ...... . . . 2-21 2.2.4 Vessel Water Cooling Flow . . . . . . . . . . . ........... . . . . . . . 2-22 m:\3578w.non:lb-081898 iii L_ _- . _ _ _ _ - _ _ _. _ _
FINAL TABLE OF CONTENTS (Cont.) S*CtiOD M E8Et 1 2.2.5 Steam Flow . . . . . . . . . . . . . . . . . . . ............ .......... 2-23 2.2.5.1 3 In. Vortex Meter . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2-23
' 2.2.5.2 Gilflo Variable Orifice Flow Meter . . . . . . . . . . . . . . . . . . .. 2-24 2.2.5.3 6 In. Vortex Meter (Phase 3 Tests) . . . . . . . . . . . . . . . . . . . . . 2-25 2.2.6 Annulus Differential Pressure . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2-25 2.2.7 Containment Annulus Air Flow and Temperature . . . . . . . . . . . . . . . . 2-26 2.2.8 Internal Velocity . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2-27 2.2.8.1 Pacer . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2-27 2.2.8.2 H5ntzsch .......... ...........................2-28 2.2.9 Containment Vessel Wall Temperatures ........... . . . . . . . . . . . 2 28 2.2.10 Annulus Wall Temperatures . . . . . . . . . . . . . . . . .............. 2-29 2.2.11 Vessel Fluid Temperatures . . . ............. . . . . . . . . . . . . . . 2-29 2.2.12 Gas Sampling . . . . . . . . . . . . . ...........................229 2.3 Data Acquisition .............................................. 2-38 2.4 Facility Operation . . . . . . . , . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2-53 3.0 D ATA REDUCTION . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3- 1 3.1 Data Acqui red . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3-1
- 3.2 Data Hand li n g . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3-1 3.3 Test Evaluation . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . ............ 3-4 3.3.1 Test Acceptance . . . . . . . . . . . . . . 4 ......................... 3-4
- 3.3.2 Test Analysis . . . . . . . . . . . . . . . . . . . . . . . . . . . ............... 3-4 3.3.2.1 Heat Balance . . . . . . . .. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 35 3.3.2.2 Pressure Check . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3-7 3.3.2.3 Steam Flow Measurement ............................ 3-7 3.3.2.4 Internal Velocity . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3-8 3.3.3 Test S u mmary . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3-9 4.0 . TEST RESULTS . . . . . . . . . . . . . . . ................................4-1
' 4.1 Test Results 202.3 . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . ........... 4-1 4.2 Test Results 2 03.3 . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4- 1 1 4.3 ~ Test 212.1 . . . . . . . . . . . . . . . ................................. 4-20 4.4 Test Results 2 1 3.1 . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-3 7 4.5 Test 214.1 . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-5 5 4.6 Te st 215.1 . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4-68 4.7 ' Test 216.1. . . . . . ............ ................. ... ....... 4-81 4.8 Test 217.1 . . . . . . . . . . . . . . . .. . . . . . . . . . . . . . . . ........... . . . . 4-95 4.9 Test 218.1 . . . . . . . . . . . . . . . . . . . . . . . . . . . .................... 4-110 4.10 Test 219.1 . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4- 125 4.11 Test 220.1 . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4- 142 m:\3578w.non:1b-081898 iv
r-y t FINA1. 4 l l J TABLE OF CONTENTS (Cont.) l i Section Thig P.gge f 4.12 Test 221.1 . . . . . . . . . . . . . . . . . . . . . . . ....................... 4-157 i 1 L 4.13 Te st 2 2 2.1 . . . . . . . . . . . . . . . . . . . . . . . . . . .. . . . . . . . . . . . . . . . . . . . . 4-175 )
- 4.14 - Test 222.2 . . . . . . . . . . . . . . . . . . . ......................... .. 4-189 )
( 4.15 Test 222. 3 . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .............. 4-206 i 4.16 Test 222.4 . . . . . . . . . . . . . ................... . . .......... 4-223 4.17 Test 223.1 . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. . . . . . . . . . . . . . . . . 4-240 4.18 Test Results 224.1 . . . . . . . . . . . . ................... ......... 4-249 l
-4.19 Test Results 224.2 . . . . . . . . ............. ................... 4-257
5.0 CONCLUSION
S . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . ................... 51 l t
6.0 REFERENCES
. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 6-1 l
l APPENDIX A - Facility Drawings . . . . . . . . . . . . . . . . . . . . . . . . . ..................A-1 l- ' APPENDIX B - Sampling Apparatus .... .... ................................ B-1 j i APPENDIX C - Data Handling . . . . . . . . . ...................................C-1 l
.i I APPENDIX D Official Test Data Files . . . . . . . . ....................... ........ D-1 )
3 f APPENDIX E - Baseline Test Data . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . E-1 i L 1 I i i l 1 :1 L i I 1 r t
- m:\3578w.non:Ib-081898 y Rev.I
1 I FINAL,
SUMMARY
This document presents the test data for the last two phases of large-scale passive containment cooling tests defined as confirmatory and follow-on tests, respectively. The tests were all performed at the j Westinghouse large-scale test facility at the Westinghouse Science and Technology Center in Churchill, PA. This test report, preceded by a series of " Quick Look" repons (References 6.1 through 6.12), reissues the data in engineering units with post-test calibration considerations included. Additionally, the first phase of tests, " baseline tests," was reponed in Reference 6.13. The data from these baseline tests are included in this document as Appendix D for purposes of document completeness. The passive containment cooling system (PCS) tests were designed to characterize the heat removal capabilities of the AP600 containment design. Throughout the testing process, emphasis was placed on the importance of verifying the test behavior versus the new innovative passive safety system design. The test data was and will be compared to calculational results obtained using the same analytical tools used in the analysis of the design, in this case, the Westinghouse-Gothic code (WGOTHIC). All testing has shown that the PCS will perform its intended function reliably and efficiently. Heat transfer data and pressure drops have been measured and compared very favorably with respect to l predictions. The ability of the PCS to distribute water over the containment has been proven, and the i environmental effects of wind and cold on the performance of the system have been shown to be minimal. Due to the extensive testing to date, as well as analytical results, a high degree of confidence in the performance of the PCS has been established. I m:\3578w non.1b-o81898 1 Rev.I
FINAI, l \ I
1.0 INTRODUCTION
l The advanced light water reactor (ALWR) AP600 passive containment cooling system (PCS) design, shown in Figure 1.0-1,is significantly different from past and current nuclear plant designs. This containment design concept represents one of the significant advances in the progress of the nuclear l plant design industry toward simple, passively safe plant designs. I In the AP600 design, the function of the PCS is to provide a safety-grade means for transferring heat from the containment to the environment following postulated events that results in containment heatup and pressurization. The AP600 utilizes passive cooling of the free-standing steel containment vessel. Heat is transferred to the inside surface of the steel containment vessel by convection and condensation of steam and through the steel wall by conduction. Heat is then transferred from the outside containment surface by free convection to the air that enters an annular space around the steel containment shell. Cooling of the containment is enhanced by the addition of water distributed over the containment surface, which is heated and is evaporated into the air stream. The heated air and water vapor rises as a result of the natural draft developed and exits the shield building through an outlet (chimney) located above the containment shell. The performance of the AP600 PCS depends predominantly upon the cooling air buoyant driving force, the air flow path pressure losses, the effective containment shell heat transfer coefficient, and the wetted PCS heat transfer area. Other factors that can influence PCS performance include wind conditions, nearby buildings and topography, inside containment circulation pattems, water distribution patterns, and the effects of noncondensible gases inside the containment. As is the case of all new designs, key concepts and principles are researched, which then evolve into a definition of the overall matrix of testing necessary to obtain the data in support of the design. j Initially, where data is lacking, small basic research tests are conducted to demonstrate fundamental j principles and feasibility of concepts. Based on these tests, larger and more sophisticated tests are l designed to further evaluate the engineering and safety concepts of the design. The AP600 PCS large-scale test facility (Section 2.0), described in this document, is one example of this approach. In order to accurately assess the impact of these parameters on the AP600 PCS. heat removal capability, a total testing program (Table 1.0-1) was prepared that includes the following series of tests:
- AP600 heated plate test (Reference 6.14)
AP600 PCS water distribution test (Reference 6.15) l AP600 small-scale containment cooling test (Reference 6.16) AP600 large-scale passive containment cooling system test (Reference 6.l'i) { AP600 PCS wind tunnel test (Reference 6.18) AP600 PCS air flow path pressnre drop test (Reference 6.19) This report presents the test data from the phase 2 and phase 3 heat transfer tests of the AP600 ! large-scale containment cooling test (LST). I
- ast .:ib-081898 1-1 Rev.1 L_----_------------------------- .- -. -
FINAL TABLE 1.0-1 AP600 PASSIVE CONTAINMENT COOLING SYSTE51 TESTS Passive Completion Containment Cooling System Tests Test Objective / Conclusion Date Air Flowpath Pressure Drop Test 14easured air annulus loss coefficients are Completed. (Westinghouse STC) predictable; form losses minimized January 1988 Water Film Formation Test Phte wetting characteristics with and without Completed, (Westinghouse STC) coating are excellent February 1988 Heated Plate Test (Westinghouse STC) Water film behavior is stable under all Completed, conditions; heat transfer rates are predictable May 1988 Bench Wind Tunnel Experiment Wind from any direction always enhances air Completed. (Westinghouse STC) flow with high air inlet August 1988 Condensation Tests (University of Wisconsin)
. Surface Tests Heat transfer coefficients measured for Completed, various surfaces and orientations November 1990
. Non-condensible Tests Assessed effect of helium on heat transfer Con pleted, coefficient Julv 1993
. Two-dimensional Test Models Obtain data on heat and mass transfer September 1994 phenomena using a small 2-D test model of the AP600 large-scale test Integral PCS Test (Westinghouse STC)
Phase 1 Established the capability of the PCS to Completed, provide adequate heat removal using an October 1989 integrated test facility Phase 2 Obtained data during PCS operation over the Completed, full range of design basis operating conditions July 1992 Large-Scale PCS (Westinghouse STC) Obtain data during PCS operation on a scaled Completed, structure that accurately models both the Phase I containment dome and sidewall heat transfer May 1992 areas, and inside containment structures Completed, Phase 2 September 1993 m11578w.nonib 081898 12 Rev.I
FINAt. l TABLE 1.01 (cont.) AP600 PASSIVE CONTAINMENT COOLING SYSTEM TESTS Passive Completion l Containment Cooling System Tests Test Objective / Conclusion Date PCS Water Distribution (Westinghouse AESD) l Phase ! - Center of Dome,20 ft. Demonstrated the effectiveness of water Completed, Diameter distribution on the center of the containment June 1991 [- dome Phase 2 - Full Scale 1/8 Section Demonstrated the effectiveness of water Completed, distribution on the containment dome and January 1992 l upper sidewall l' Verify design of water distribution system Completed, l Phase 3 - Full Scale 1/8 Section September 1993 PCS Wind Tunnel (University of Western Ontario)
- Phase 1 - Overall building Measured the wind induced pressure on the Completed, effects (1/100th scale) containment shield building due to air July 1991 inlet / outlet configurations and site structures
- Phase 2 - Detailed Model, Final Verification Measured baffle loading and the effect af Completed, j (1/100th scale) wind on containment annulus air flow February 1992
- Phase 4A/4B - 1/30th scale &
1/800th scale . To perform tests at higher Reynold's numbers Completed, j and to determine effects on site geography. November 1993 I L m:\3578w.non:1b-08I898 ].3 Rev.I
FINAL PCS Water - t i Storage Tank f' %M i t t
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t FINAL, l l 1.1 Test Objectives l The purpose of the passive containment cooling system (PCS) heat transfer test is to examine the anticipated thermal-hydraulic phenomena on a large scale: the interior natural convection and steam condensation, the exterior water film evaporation, air cooling heat removal, and water film behavior. This experiment is de-igned to induce similar containment dome heat transfer processes and circulation / stratification patterns inside containment as in the AP600; however, it is not meant to simulate specific AP600 accident scenarios. The large scale test data is used to validate the EGOTHIC computer code, which will be used to analyze the AP600 containment. The se 2 tests provide data to validate the EGOTHIC containment heat and mass transfer correlations over a range of prototypic internal conditions, including the effects of external parameters. The tests provide data on the transient heat transfer and the distribution of noncondensables. The effects of noncondensables on the containment heat transfer are observed. The follow-on tests (phase 3) examine special effects, such as the location of the steam discharge and effects of the concentrations of noncondensables, and are not strictly necessary for code validation, but aid in the overall understanding of the containment cooling phenomena. I
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t i i I m:uS78w.non ib-081898 1-5 Rev.1 ,
FLNAL 1.2 Facility Scaling 1.2.1 Test Vessel ne AP600 containment vessel is cylindrical with 2:1 elliptical heads at the top and bottom of the cylindrical section (Reference 6.17). The overall height of AP600 is from elevation [
-]" with an inside diameter of 130 ft. On this basis, a 1/8th linear scale model vessel should be 23.729 ft. high. The operating deck is at elevation [
]" below the top of the containment or [ ]" below the top of the model. The containment area above the operating deck is cooled on the outside and is considered the active heat transfer area.
Below the operating deck in the AP600 containment building, there are free volumes where equipment is installed. These volumes are normally in communication with the volume above the operating deck, so any steam released in an accident can either enter or discharge into them. If a volume has more than one path, circulation will exist between this volume and the containment atmosphere above the operating deck, and is referred to as an open volume. A volume in which the containment fluid does not readily circulate with the containment atmosphere above the operating deck is called a dead-ended compartment. The open volumes and dead-ended volumes are approximated by the following AP600 compartments: Open Volumes
- Refueling cavity
. Steam generator loop compartment (without break)
- Dead-Ended Volumes
*- 107 ft. elevation of containment
- In-containment refueling water storage tank
= Reactor cavity
- Accumulator areas
- Chemical and volume control system module ne total free volume below the operating deck and the free volume occupied by each sub-compartment were calculated. When the large scale test was b. c. signed, the AP600 plant design showed that the open volumes occupied [ ]" of the tou /olume below the operating deck.
The dead-ended volumes occupied [ ]", and the steam generator compartment (with break) occupied 9 percent of the total free volume below the operating deck, here are two steam generator compartments in the AP600. For LST test purposes, one is considered as part of the open volume. The other is considered the steam generator volume because steam release is simulated in it. i mus78w.non:ib.os209s 16 Rev.2
FINAL. The phase 2 and phase 3 tests have representations of the open, dead-ended, and steam generator volumes. The open volume provides venical communication with the vessel volume above the operating deck. The dead-ended volume has one entrance (from the open compartment) and no exits. It does not communicate with the containment atmosphere above the operating deck. The percentages 1 given above were used to determine the volume of the open, dead-ended, and steam generator i companments below the operating deck in the LST. As built, the LST open volume occupies [ ]" of the total volume below the operating deck. The dead-ended volume occupies [ ]", and the steam generator compantnent occupies [ ]" of the total volume below the operating deck. In the SSAR AP600 plant design, the open volumes occupy ( ]", the dead-ended volumes occupy [ ]", and the steam generator compartment occupies [ ]" of the total free - volume below the operating deck. The volume percent occupied by each compartment in the LST is very close to the volume percent occupied by each compartment in the AP600 and is sufficient to validate the capability of WGOTHIC to represent each type of volume in the AP600. 1.2.2 Heat Sinks l Heat sinks are available in the AP600 as equipment in containment and the containment structural materials. These constituents are divided into two groups: shon and long term heat sinks. The short term heat sinks are the materials that absorb heat quickly, whereas the long term heat sinks continuously remove heat over the long term, such as heat transfer through the concrete to the surrounding soil around the bottom of the containment vessel. 1.2.2.1 Short Term Heat Sinks The initid steam release into the containment raises containment pressure. Intemal masses absorb he.it, condense steam, and reduce the transient pressure. To address the effect of thermal storage on initial pressurization and evaluate noncondensible gas distributions, surface area and mass are added inside the large scale containment model. As steam enters the containment from the steam generator compartment, steam and air are forced into the open and dead-ended compartments below the operating deck. Relatively large areas and masses condense the steam, and the remaining air is thermodynamically stable and is expected to remain within the compartments below the operating deck. The panial density of steam above the operating deck increases together with the rate of diffusion for condensing steam on the vessel walls. The steel in the companment walls, deck supports, operating deck cover, and operating deck grating provide some heat storage. Based on the surface area available for heat transfer in the AP600, additional heat transfer area was needed in the large scale test. Aluminum plates were added to supply [ additional heat removal from the con *.ainment atmosphere. The aluminum plates were designed to I m:uS7sw.non:ib-os2098 1-7 Rev.2
FINAt. provide a relatively short heat transfer time constant. He time constant for effective heat removal from the steam and air containment atmosphere is approximately 100 seconds. The required surface area was provided by [ ]" aluminum plates, each [
)", mounted in banks inside the large scale test. The plates are positioned in these groupings: [ ]" plates in the dead-ended compartment, [ ]" plates in the open compartment, and
[ ]" plates just above the operating deck. Each plate has [ )" of ama. The three groups are representative of the additional surface area available in the AP600 in these '%e general locations. 1.2.2.2 Long Term Heat Sinks The purpose of representing long term heat sinks in the large scale test is to model long term heat removal and any effect it may have on noncondensible gas distribution, he effect of the long term heat sinks is mor 'ed in the LST by removing the bottom insulation surrounding the open and dead-ended compartme...s. Information from AP600 analyses concerning long term heat sinks, such as heat sink surface area, heat removal rate late in the transient, and the percent of heat removed by the long term heat sinks, were considered when evaluating long term heat sink representation in the LST. Test numbers 218.1,219.1,220.1, and 221.1 in the phase 2 test matrix include the effects of long term heat sinks. m:\3578w.non:lb.082098 }.8 Rev.2
FINrt. 1.3 Test Matrix The tests were conducted in three phases:
- Baseline tests
* ' Phase 2 tests Phase 3 or follow-on tests The baseline tests consisted of sixteen steady-state tests that were performed at three constant pressure j conditions while investigating the effects of different water coverage levels, various external air flow '
rates, and the presence of internal structures. The baseline tests were reported in Reference 6.13, and the test matrix is provided in Table 1.3-1 for reference.
]
'Ihe test matrices for the phase 2 and phase 3 of the large scale PCS test series are shown in J
Tables 1.3-2 and 1.3-3, respectively. The fo!!owing paragraphs contain a discussion and purpose of each of the phase 2 and phase 3 tests. 1.3.1 ~ Phase 2 Test Matrix The large-scale phase 2 test matrix consisted of the twelve tests specified in Table 1.3-2 for the AP600. The tests in the phase 2 matrix covered a range of pressures and operating conditions that are sufficient to validate the code's ability to predict pressure and temperature responses to accident scenarios. All the tests were performed with water from the PCS at a temperature of 50 to 80*F. The l extemal water flow rates were chosen to simulate the amount of coverage expected on the AP600 plant. The annulus air flow was maintained at an external air velocity of 12 ft/see by adjusting the fan speed for all of the tests performed during phase 2. It was not deemed necessary to vary the air velocity in this set of tests since the focus is on intemal distributions and heat transfer. Tests 202.3 and 203.3 were provided as repeats of the constant pressure tests performed during the baseline test series (202.1,202.2,203.1 and 203.2). They were included to evaluate the effect of the addition of the steam generator model and the bottom insulation and to obtain additional test data with the increased level of instrumentation. Tests 212.1 through 221.1 were steam-flow rate specified transient tests. The effects of the various parameters were investigated by changing one parameter while all others were held constant. Tests 202.3 through 217.1 addressed the effects of the short term heat sinks installed in the test facility. Long term heat sinks were modeled in tests 218.1,219.1,220.1, and 221.1 by partial removal of the insulation on the bottom of the test vessel (see Section 1.2.2.2). For tests 212.1 and 213.1, three steam flow rates were tested as the system approached a steady-state condition after each flow adjustment. The three nominal flow rates selected were [
. ]". These tests were used to validate WGOTHIC's ability to predict transient behavior,
- muS7swmon:ib.os2098 19 Rev.2
FmA1. while the effects of differences in PCS water coverages between tests 212.1 and 213.1 were demonstrated. Two tests (214.1 and 215.1) were performed where air flow was allowed to develop in natural convection (prior to initiation of the fan) to the [ ]" air annulus flow. The steam flow rate was held at approximately I lbm/see throughout the tests. After steady state conditions were reached, the fan was activated to exercise .WGOTHIC's ability to model the transition between free and forced convection. Test 215.1 required that a 180 degrees circumferential section be blocked off, such that the annulus air flow only enters around the remaining 180 degrees azimuthal section, to address the effect of partial blockage of th air inlet region. The 180 degrees azimuthal blockage was centered around the steaa generator. Test 216.1 was a transient between two steady-state conditions: 75 percent PCS coverage and 25 percent PCS coverage in quadrants. This test can be compared to tests 212.1 and 213.1 to evaluate the difference between PCS water coverage in stripes and in quadrants. Tests 217.1 through 221.1 addressed the effect of long term heat sinks, helium addition to simulate hydrogen from postulated severe accidents, and steam blowdowns. This definition is used to determine the helium concentration (helium, instead of hydrogen, is used for safety reasons) in the , large scale test. A hydrogen (helium) concentration of [ ]" is predicted when all the Zircaloy in the core is oxidized. The concentration of hydrogen in the plant should never reach [ ]" because ignitors are present in the plant to keep the concentration below [ ]". However, the tests were performed with [ ]" of helium to simulate the maximum possible hydrogen concentrations for tests 217.1,218.1,219.1 and 221.1. The purpose of test numbers 217.1 and 218.1 was to evaluate the effect of long term heat sinks on noncondensible distribution. Test number 218.1 was similar to test number 217.1, with the only difference being the inclusion of long term heat sinks. After the system has come to steady state with a steam flow rate of I lbm/sec, the helium is injected at a nominal flow rate of 0.0039 lbm/sec for 30 minutes, and the system is allowed.to achieve a second steady state. The purpose of test 219.1 was to evaluate how the noncondensables (specifically helium) distribute when the following scenario was followed: achieve steady state without external water flow, inject helium, come to steady state again, then start the PCS flow. This test provided data on the effects of rapid cooling of a dry containment on noncondensible distribution. Tests 220.1 and 221.1 addressed modeling heat transfer to heat sinks and the containment shell, as well as the effects on the flow field during the blowdown phase of a transient. Test 220.1 modeled a blowdown of a small steam line break. The blowdown was over within a minute and will be used to validate the WGOTHIC's ability to predict transient behavior. The blowdown rate for test 220.1 was based on a steam line break (SLB) at 102 percent power with a full m:us78w.non:lb-o82098 ] .10 Rev.2 _ _ - _ _ _ _ - _ - _ _ _ _ _ _ _ - _ - _ - _ _ _ _ _ _ _ _ _ _ -___-_-______--____-____-_____-_-__a
1 FINAL . double-ended rupture and main steam line valve failure. De test represents an AP600 limiting case l' with respect to containment pressure and temperature. The steam line break flow was scaled by 3 j volume (1/8 ) for the large scale test to produce the steam flow transient shown in Figure 1,3-1. The steam flow rate in the figure was a target test condition; a slightly lower peak flow rate does not affect the test purpose of validating WGOTHIC and was not meant to simulate the prototypical accident. l This test is used as the blind test for analysis validation, and as such, only the initial conditions arid !. forcing function data is contained in this report. l Test 221.1 modeled long term cooling during post-accident conditions. This was accomplished by starting the test with water flow on the outside, reaching a steady state after the initial steam blowdown (Figure 1.3-2), injecting helium, reaching a second steady state, then shutting off the PCS l flow, and reaching a final steady state. Noncondensible measurements were taken to evaluate the effect of this scenario on helium mixing. The helium injection and the steam flow rate for test number 221.1 were based on a small loss of coolant accident (LOCA) with in-containment refueling water storage tank check valve failure. He test was not meant to simulate the prototypical accident, although the prototypical accident was used for guidance so that the conditions in the plant and in the large scale test would be similar. The steam blowdown for the plant is scaled by volume (1/8') for the I large scale test. After the blowdown, the flow rate maintains a low constant flow of approximately 0.15 lbm/sec. 1.3.2 Phase 3 Test Matrix Seven tests were identified as part of the phase 3 test program. The first four are rapid pressurization transients that investigate the effects of the steam discharge location and orientation, while.the last three characterize the effect of the initial internal atmosphere on condensation mass transfer. l 1.3.2.1 Test Series 222 LST data from baseline and phase 2 tests suggest that noncondensible concentrations increase dramatically below the elevation of steam injection with considerable steam mixing above the operating deck. The effect of the higher steamline elevation could be to create a larger volume of rich air mixture which extends above the operating deck, and reduces the active heat transfer area. The higher break elevation is representative of a steamline break. This series of tests addresses the impact of the elevation and direction of the steam break on the response of the test vessel and includes the
- transient blowdown behavior (Figure 1.3-3) to an ultimate steady-state condition.
The four configurations in this test series were: 222.1 Low velocity steam flow from under the operating deck 222.2 Low velocity steam flow ( ]" elevation above the operating deck 222.3 kiigh velocity steam flow with horizontal discharge [ ]" above the operating deck } 222.4 High velocity steam flow at [ ]" elevation upward mus78wmn:1b 08209s 1-11 Rev.2
FINAL Two steam injection directions were run with both pipe exits at the [ ]" elevation, which is linearly scaled (1/8th) to the location of a steamline coming off the top of the AP600 steam generator. The tests are run with nominal 75 percent water coverage and 12 ft/sec air flow. 13.2.2 Test 223.1 This test permits a direct measurement of the liquid film heat transfer coefficient by reducing the noncondensible concentrations to a very low level by evacuating the test vessel. The large dome in the large-scale test vessel produces data for non-vertical surfaces that are more prototypical and will provide a link to similar data from the Wisconsin condensation tests with pure steam and test the validity of the Chun and Seban liquid film heat transfer model used in the WGOTHIC code. 13.2.3 Test Series 224 These tests pennit measurement of the effect of a higher noncondensible concentration on the transient i l and steady-state performance of the test vessel for validating the noncondensible partial pressure effect in WGOTHIC models at two different steam flow rates. The vessel pressure is increased to 2 atmospheres of air prior to the start of steam flow. mA3578w.non:lbO82098 1-12 Rev.2 l
FINAL f l TABLE 1.3-1 AP600 LARGE SCALE CONTAINMENT COOLING TEST BASELINE TEST MATRIX Water Steam Supply Annulus Air Pressure Flow Distribution Flow Test Number (psig) (gpm) (%) (ft/sec) BASELINE TEST NO INTERNALS: L-201.1 10 FLOOD 100 9 L-202.1 30 FLOOD 100 9 L-203.1 40 FLOOD 100 9 L-207.1 30 FLOOD 75 9 L-207.2 30 STRIPE 75 9 BASELINE TEST WITH INTERNALS: L-201.2 10 FLOOD 100 12 L-202.2 30 FLOOD 100 12 L-203.2 40 FLOOD 100 12 L-204.1 30 FLOOD 100 16 L-205.1 30 FLOOD 100 8 L-206.1 30 FLOOD 100 FREE L-207.3 30 FLOOD 75 12 L-208.1 30 FLOOD 50 12 L-207.4 30 STRIPE 75 12 L-210.1 40 FLOOD 100 12 (l10'F) L-211.1 40 FLOOD 100 FREE (l10*F) NOTES:
- 1) All tests performed at steady-state conditions at ambient atmospheric conditions.
- 2) Vessel pressures are targeted steady-state values.
m:uS78w.non:1b-081898 1 13 Rev.I
FINAL TABLE 1.3-2 AP600 PHASE 2 TEST MATRLX Steam Control Test Pressure Flow Air Flow Long Term , Number (psig) (Ibm /sec) (ft/sec) Water Coverage Heat Sinks Helium Sampling 202.3 30 - 12 100 % NO NO NO 203.3 40 - 12 100 % NO NO NO 212.1 0.25/0.5/0.75 12 75% STRIPED NO NO YES 213.1 0.25/0.5/0.75 12 25% STRIPED NO NO NO 214.1 . 1. NCl2 75% STRIPED NO NO NO 215.1 - 1. NCl2 75% STRIPED NO NO NO 1/2 AIR BLOCKAGE 216.1 - 0.5 12 75%/25 % NO NO NO QUADRANTS
- - u 217.1 1. 12 75% STRIPED NO YES 218.1 - 1. 12 75% STRIPED YES YES 219.1 - 0.2 12 DRY /50% YES YES STRIPED 220.1 - BLOWDOWN 12 75% STRIPED YES NO YES 221.1 - BLOWDOWN 12 50 % YES < 10 VOL % YES STRIPED / DRY l
l I mA3578w.non:lb-081898 1 14 Rev.1
FINAL TABLE 1.3-3 LST PIIASE 3 TESTS Flow Rate Air Flow Test Number Configuration (Ibm /sec) (fthec) Water Coverage Sampling 1.0 Blowdown Tests 1.2 Test 222.1 Diffuser under SG 6/3/05, 12 75% Stnped YES run to SS 1.3 Test 222.2 Diffuser 6 ft. above deck, 6/3M.5, 12 75% Stnped YES pointed up run to SS CT 1,30 12 75% Stnped YES psig. SS 1.4 Test 222.3 3 in, steam source,6 ft. 6/34.5. 12 75% Senped YES above deck, jet pointed at run to SS near wall CT 1, 12 75% Sinped YES 30 psig. SS 1.5 Test 222.4 3 in. steam source,6 ft. 6/3/0.5 12 75% Stnped YES above deck, jet pointed up CT I 12 75% Stnped YES 30 psig. SS 2.0 Evacuated. 001 Atmospheres of Noncondensables 2.1 Test 223.1 Diffuser under SG 0.25 to 10 12 75% Stnped YES psig ss, 100% wet max now to 12 75% Senped YES SS 3.0 Pressurized. 2 Atmospheres of Noncondensatsles 3.1 Test 224.1 Diffuser under SG 0.25 12 75% Sinped YES 3.2 Test 224.2 Diffuser under SG 0.5 12 75% Stnped YES mA3578w.non:lb-081898
}.15 Rev.I
FINAL. I 2.5 2
' 1.5 i
E E a {. 1 " rn 0.5 -" 0 O.0 100.0 200.0 300.0 400.0 500.0 600.0 700.0 800.0 900.0 1.000.0 Trne (sec) Figure 1.31 Steam Flow Transient for Test 220.1 nt\3578w.non:1M81898 ] .16 Rev.I
FINAL l I 10 l 8 o. 6 -- 7 a e - b g4 _ . . i 2 -- 0 . , , , 0.0 50.0 100.0 150.0 200.0 250.0 300.0 350.0 400.0 Time (sec) Figure 13-2 Steam Flow Transient for Test 221.1 m:us78w.non: t b-081898 1-17 Rev.1
FINAL 8 ,. . m . Q . 0 7 _ - rn . N . :
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10 30 50 70 90 110 130 150 170 TIME (seconds) i Figure 1.3-3 Steam Flow Transient for Test Series 222 m:\3578w.non:lb 081898 1 18 Rev.1
- - - - - - - - - - - - ~
FINAL 2.0 TEST FACILITY DESCRIPTION The AP600 large-scale containment cooling tests were performed using the large scale test facility , (Figure 2.0-1), located at the Westinghouse Science and Technology Center in Churchill, PA. This ) facility, constructed for the HWRF containment testing program, is shared under contractual agreement with the Westinghouse / DOE (NE) commercial plant passive containment cooling system (PCS) test program. The large-scale PCS test facility uses a [ ]" diameter pressure vessel to simulate the steel containment shell, with a lieight to diameter ratio more typical of the actual containment shell than was available for the small scale tests (Reference 6.16). The larger vessel makes it possible to study in-vessel phenomena, such as noncondensible mixing, steam release jetting, and condensation, as well as now patterns inside containment. The vessel contains air at atmospheric pressure when cold and is supplied with steam at pressures up to 100 psig. A transparent acrylic cylinder installed around the vessel fenns the air-cooling annulus. Air flow up the annulus outside the vessel cools the vessel surface, resulting in condensation of the steam inside the vessel. A summary of the vessel surface areas and volume is presented m Table 2.0-1. Figure 2.0-2 is a schematic diagram of the test apparatus used during this test series. Superheated steam from a boiler is throttled to a variable, but at a controlled pressure, and supplied to an off-center compartment below the operating deck of the facility test vessel, initially containing two atmospheres of air. A steam distributor provides low-velocity steam at a scaled height commensurau with that of the operating deck of the reactor plant. Table 2.0-2 presents a list of the test facility drawings contained in Appendix A. These provide the as-built configuration of the test facility. To establish the total heat transfer from the test vessel, measurements are recorded for steam inlet pressure, steam flow, temperature, and condensate flow and temperature from the vessel. Seventy-eighty thermocouple, located on both the outer and inner surfaces of the vessel's 0.875-in.-thick steel wall, indicate the temperature distribution over the height and circumference of the vessel. Additional thermocouple, placed throughout the inside of the pressure vessel on internal heat sinks (32), adjacent to the vessel wall (27), and throughout the intemal volume (47), provide a measurement of the vessel bulk team temperature as a function of position. An axial fan at the top of the annular shell allows the apparatus to be tested at higher air velocities than can be achieved during purely natural convection. 'Ihe temperature of the cooling air is measured at the entrance of the annular region and upon exiting the annulus in the chimney region prior to the fan. The cooling air velocity is determined by calibration of the fan controls by conducting a velocity traverse on the cooling annulus using a heated wire anemometer at various fan rpm control settings. A fixed vane anemometer is also located below the fan in the air exit stream to provide a continuous output of the annulus air velocity. The heat transfer to the cooling air (i.e., its temperature rise multiplied by its specific heat and its measured flow rate) and the water evaporated provides a measurement of the total heat transfer. mA3578w.non:lb-o82098 2.} Rev.2
FINrt. I TABLE 2.01 PCS DRAWING LIST Title Drawing Identification Sheet No. PCS Test Pressure Vessel 2021E31 REV. 2 1 of 12 PCS Test Pressure Vessel Air Shield 2021E31 REV. 2 2 of 12 PCS Test Pressure Vessel Operating Deck Supports and Grating - No Internals 2021E31 REV. 2 3 of 12 PCS T.:st Pressure Vessel Operating Deck Supports and Grating with Internals 2021E31 REV. 2 4 of 12 PCS Test Pressure Vessel Penetration Elevation 2021E31 REV. 2 5 of 12 PCS Test Pressure Vessel Instrumentation Penetrations 2021E31 REV. 2 6 of 12 PCS Test Pressure Vessel Thermocouple Locations for Upper Head 2021E31 REV. 2 7 of 12 PCS Test Pressure Vessel Thermocouple Locations for Air inlet & Baffle Side Wall 2021E31 REV. 2 8 of 12 PCS Test Pressure Vessel Air Inlet and Outlet and Diffuser Thermocouple 2021E31 REV. 2 9 of 12 PCS Test Pressure Vesse: Velocity and Air Temperature Traverse Locations 2021E31 REV. 2 10 of 12 PCS Test Pressure Vessel Water Film Distributor 2021E31 REV. 2 11 of 12 PCS Test Pressure Vessel Internal Heatsinks 2021E31 REV. 2 12 of 12 Sketch - Large Scale PCS Rotating TC Rake Frame 07/20/92 WAS Rev 1 l Assembly & TC Locations mM578w.non:lb 081898 2-2 Rev.I l.
FINA1, TABLE 2.0-2
SUMMARY
OF AREAS AND VOLUMES FOR THE LARGE-SCALE TEST TESSEL Surface Areas and Flow Areas 2 Area (ft ) Vessel 5 'Jace Area, Above Gutter Top - a.c l Dome 0 to 21 in. Radius l Dome 42 in. Radius Dome 63 in. Radius Dome 84 in. Radius Level A Level B 1 l Level C I l Level D j 1 l Level E Vessel Surface Area, Below Gutter Top Level F Baffle Surface Area, Dome Diffuser Aluminum Deflector l Plexiglass Dome Level A Level B l l Level C j Level D j Level E
- Inlet Flow Area
~,
l Outlet Flow Area Volumes Total Vessel Volume Above Operating Deck Below Operating Deck _ _ mA3578w.non Ib 081898 2-3 Rev.1
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[$ j k[# Y Figure 2.01 Large Scale PCS Test Apparatus mu57sw.non b-081898 24 Rev.I
FINAL
- Exhaust ran O Atto P Cettl Duttet T/C's Located by- 4C Equal Circumferental Areas Vater Dstrepution Systen F r Dffuser i
Portable Anemoneter for Traversing Ptexiglass Baffle Traversmg T/C 1 Portable Anenometerg for Traversmg g J L Gas Sanptmg l A N , Traversmg T/C's m m a.= l transparent Baffle I \ _y Portable Anenometerg for Traversmg g u. a. % [- y i s aw
" "% V Fixed Intet T/C J- - ,
r ;n._ 1 i s= m = l Steam Flow Meter l l Helium Injection l l Figure 2.0-2 Section View of AP600 Large Sca'e PCS Test Phase Two Configuration 1 m:\3578w.non:lb-081898 25 Rev.I
FINAL 2.1 Facility Component Description De following paragraphs provide a description of the various components in the test facility. Some of the components have a combined mechanical and test data function, and therefore will appear in both locations. 2.1.1 Foundation and Tower The large-scale test article is supported on a reinforced concrete foundation, capable of supporting the weight of the test vessel and test tower under normal operating conditions (33 tons) and completely filled with water for hydro test (<140 ton total). 'Ihe test tower provides support for the air baffles, piping, and instrumentation, as well as platforms for workmen and test operators. The test tower is displaced approximately 12 in. from the side of the test article to provide clearance for an air baffle. The entire assembly is capable of withstanding 100-mph winds. 2.1.2 Pressure Vessel The AP600 test article was manufactured in accordance with the specification identified in Reference 6.17 and detailed in the as-built drawings presented in Appendix A, Drawing 2021E31 Sheet 1. The vessel design is summarized below: The containment tank is an ASME Division 1 Section XIII vessel, built to 1/8th linear scale of the AP600 full-sized containment and constructed of carbon steel with a minimum wall thickness of 0.815 in. The tank is designed for internal pressures of 5; 100 psig, while operating at temperatures up to 350*F. I The [ ]"in diameter with 2:1 elliptical heads at each end. Small penetrations (up to 3/8 NPT) are provided in the upper head for instrumentation or sampling probes, and a central 4-in. weld neck flange is provided for venting and instrument tree connections. The surfaces of the upper head and walls provide prototypical sur' aces for the condensate film. 'Ihe tank interior and exterior surfaces were sandblasted prior to painthg with G-40 size steel shot. The tank was spray-coated to a thickness of 4 to 6 mi's [ . l
]".
A 24-in. manway for personnel access is provided in the side of the tank, using appropriate welding necks and flanges. The tank bottom is equipped with a 20-in. flange for connection of the condensate drains and instmmentation lines. A separate 4-in. flange is mounted on the bottom flange to facilitate connection of the steam supply piping approximately 40-in. from the vessel centerline. m:u578uon:ib-os209s 2-6 Rev.2
FINA1. Intemal " gutters" provide a simulation of the crane rail and can be used separately to collect the condensate from the inside sidewall (straight length) and from the dome region during testing. The bottom of the two gutters for the dome region are located 70.38 in. from the top of the vessel, and the side wall gutter is located at the operating deck level. Both gutters are drained into the condensate handling system through the flange in the bottom of the vessel. De bottom gutter also suppoits the superstructure for the internal structures. 2.1.3 Steam Supply Two steam supply systems were utilized during the operation of the PCS test program. The primary system was a 10,000-lbm/hr system located at the STC site, while the other was a 24,000-lbm/hr system rented from Indeck Corporation to perform high flow rate blowdown tests. He following
. paragraphs describe each of these systems and there connection to the test vessel.
2.1.3.1 Fwth,y Steam Supply
' Saturated steam is supplied by a 10,000-lbm/hr gas-fired boiler that is maintained between 80 and 100 psig during testing. Full firing is maintained at the boiler to minimize cycling and pressure swings that could result in unsteady operation of controls in the test apparatus. Excess steam is vented to ambient through a pressure-limiting relief valve and flow silencer above the boiler. Laboratory demineralized water is used for boiler water makeup.
The steam is supplied to the test tower through approximately 68 ft, of 4-in. Schedule 40 piping, insulated with 1.5 in, of glass fiber insulation and approximately 123 ft. of 3-in. Schedule 80 pipe.
' The 3-in. pipe is routed under the road separating the test facility from the control room through approximately % ft. of 8-in. " Perma-Pipe," equipped with trace heating to add superheat to the steam.
Electrical trace heaters are installed over 40 ft. of the 4-in. steam-supply piping to reduce piping heat losses and ensure that superheated steam conditions (after throttling from 100 psig to the lower test pressure) are maintained for all tests. At the test tower, steam is delivered from the main 4-in. supply to the test vessel inlet through a 3-m. insulated pipe. Figure 2.1-1 shows a schematic of the steam line installation. The 3-in. steam-supply pipe is connected to the 3-in. nipple welded into the 4-in. blind flange located 40 in. off the centerline of the pressure vessel on the bottom vessel dome. Steam flow is pneumatically controlled with a 2-in. flow-control valve. The steam flow is measured by a vortex flow meter just pdor to inlet into the tes: vessel and by a variable orifice flow meter in the steam line to handle high flow rates needed during blowdown testing. 2.1.3.2 High Capacity Boiler A 24,000-lbm/hr gas-fired boiler supplies saturated steam to the test vessel for this test. The steam supply system is maintained between 110 and 130 psig during testing. Full firing is maintained at the mA357sw.rmi:ib.osis9s 7 Rev.1
FINAL boiler to minimize cycling and pressure swings that could result in unsteady operation of controls in the test apparatus. Excess steam is vented to ambient through a bypass discharge system containing a flow silencer prior to the steam flow meter. A separate water treatment trailer is supplied with the boiler to maintain makeup water quality. The steam is supplied to the test tower through approximately 120 ft. of 6 in. Schedule 40 piping, insulated with 1.5 in. of glass fiber insulation with trace heating to maintain the steam superheat. At the test tower, steam is delivered from the main 6-in. supply to the test vessel inlet through a 3-in. insulated pipe. A schematic of the steam line configuration is shown in Figure 2.1-2. The 3-in. steam-supply pipe is connected to the 3-in. nipple welCJ into the 4-in. blind flange located 40 in, off the centerline of the pressure vessel on the bottom vessel dome. Steam flow is pneumatically controlled with a 3-in. flow-control valve. The steam flow is measured by a 6-in. vortex flow meter prior to inlet into the test vessel. 2.1.3.3 Steam Injection Steam injection into the test vessel was impleme..ted during the majority of the phase 2 tests through an 18-in.-diameter, conical steam-injection tube (Figure 2.1-3) located in the center of the steam generator compartment approximately 6 in. below the operating deck level. The top of the diffuser is covered with a two layers of 60 percent open stainless-steel mesh. Three alternate steam injection arrangements were tested during phase 3 of the test program that provide a steam discharge located [ ]" above the operating deck, as shown in Figure 2.1-4. One configuration (Test 222.2) is equipped with a 18-in.-diameter conical steam-injection tube discharge (Figure 2.1-3), located 6 ft. above the operating deck level. The second configuration (Test 222.3) provides a 3-in. elbow without the diffuser pointed at the side wall of the vessel. The final configuration (Test 222.4) provides a 3-in. discharge located 6 ft. above the operating deck pointed directly upward. 2.1.4 Vessel Internals 2.1.4.1 EMellne Test Series The initial series of baseline tests were performed in tb vessel with no intemal panitions so that the inemal gases were free to move over the entire volume of the test vessel. The steel superstructure that supports the internals partitions and galvanized operating deck grating was installed. The steam was injected into the vessel through a 3-in. Schedule 40 pipe with its outlet covered with a stainless steel mesh. The outlet was installed at a height equal to the height of the operating deck, approximately [ ]" above the bottom of the vessel in the center of the vessel. mA3578w.norrib 08209s 28 Rev.2
FINAr. The second series of baseline tests was performed in the vessel with intemal partitions providing open, closed, and steam generator companment volumes below the operating deck. The open areas provide venical communication with the' vessel solume above the operating deck. He closed areas provide a dead-ended volume with one entrance and no exits. The steam generator companment is equipped with the conical steam-injection tube described in Section 2.1.3.3 and located in the center of the sterm generator compartment, approximately 6 in. below the operating deck level. The top of the' diffui,cr is covered with a two layers of 60 percent open stainless-steel mesh. The steam generator compartment is open vertically to the vessel volume above the operating deck. He companment walls are made of 16 gauge galvanized sheet, i
\
2.1.4.2 Phase 2 and Phase 3 Test Series These tests were performed with intemal partitions installed in the vessel, as illustrated in Figure 2.0-2, providing open, closed, and steam generator corripartment volur=es below the operating deck. The open areas provide venical communication with the vessel volume above the operating deck. .ne closed areas provide a dead-ended volume with one entrance and no exits. The steam generator compartment is eqt.ipped with the conical steam-injection tube located in the center of the steam generator companment 6 in. below the operating deck level. A simulated steam generator structure [ ]" is inounted in the center of the steam generator companment [ ]" above the steam-injection tube at the level of the operating deck. He steam generator companment is open vertically to the upper vessel volume around the steam generator model. De companment walls are made of 16 gauge galvanized sheet. Heat sinks are installed in the open and dead-end compartments under and above the operating deck. A cross section view of the heat sinks is shown in Figure 2.1-5 and detailed in Appendix A, Drawing 2021E31 Sheet 12. He heat sinks provide a simulation of the short-term heat-sink effect (<100 seconds) of the structure surfaces and equipment. The heat sinks are made up of 0.375-in.-thick aluminum plates with [ ]" of surface area, each stacked together into two units of [ ]" plates for the dead-end compartment, [ ]" plates for the open compartment and ,[ ]" plates for the area above the operating deck. An internal structure called the " thermocouple rake" was added to support a matrix of thermocouple that monitored the internal temperatures of the test vessel at levels A, B, C and D. The rake was mounted in the center of the vessel with arms that supported the thermocouple at each level with an extension into the dome area. The rake was supported from the flanges in the top and the bottom of the test vessel and was designed to be capable of rotating during testing. He specific location of the thermocouple is identified in Table 2.3-1 according to the coding system described in Section 2.3. A drawing of the reke is provided in Appendix A. ) I 1 mA3578w. mon:Ib-08209s 2-9 Rev.2 i
FINAL 2.1.5 Condensate Har61ing , Condensate that is formed on the inside wall of the pressure vessui :s collected in five separate areas (Figure 2.1-6) and routed through penetrations in the 20-in. flange at the bottom of the vessel. The condensate is removed through a manifold under the test vessel that collects all of the condensate lines and directs the condensate flow from each area to one of two condensate measurement systems. Each syttem is equipped with a heat exchanger that cools the condensate below 90*F. Flow is controlled through a liquid drain trap (vapor trap or steam trap) that discharges condensate on a continuing basis to a weigh tank consisting of a 55-gallon drum that rests on an electronic scale. The mass of condensate collected in the weigh tank is measured by the electronic scale and this reading is continuously communicated to the data acquisition system (DAS) over an RS232 interface. A level probe installed in the weigh tank is connected to a solenoid valve installed in the weigh tank drain line and provides for automatic draining when the weigh tank is filled. The two tanks are set to collect condensate within limits of the scale capacity. The first tank, referred to as the small tank, measures condensate accumulations between 73 and 222 lbs. The second tank, or large tank, measures condensate between 82 and 372 lbs. 2.1.6 External Cooling Annulus and Air Ducting The AP600 large-scale test uses a plexiglass shell to provide a single 3-in. annulus width for all of the tests described herein (Figure 2.1-7). The details of the shell are shown in Appendix A (Drawing 2021E31 Sheet 2). The cooling air annulus is formed by a baffle made of a 0.25-in.-thick, transparent acrylic cylinder installed on steel standoffs 3 in. from the pressure vessel surface. Twelve 4-in. aluminum strips (0.25-in.-thick) were used to hold the vertical edges of the baffle panels. The panels were circumferentially stiffened using 1.5-in.-wide, flat aluminum bars. The components were assembled, using screws to fasten the acrylic to the aluminum supports, to form a cylinder 125 in. (10 ft. 5 in.) high and 186 in. inside diameter. TN bottom of the acrylic cyhnder was located at an elevation approximately 7 3/4 in. above the top of the gutter and approximately 65 in. from the bottom of the vessel. The air inlet to the cooling annulus domed diffuser and conical section is provided as a transition between the 186-in.-diameter annulus wall and the 48-in.-diameter axial fan housing. The transition is 98 in. high. The loss coefficient base on the cylindrical annulus flow area of the annulus was estimated at 12.8. The area beneath the outside gutter was insulated with 2 in, of fiberglass insulation for the majority of phase 2 testing. The insulation has a nominal thermoconductivity of 0.3 Btu-inJ(ft.2-hr *F) at 100 F. During specific tests, the bottom of the vessel is uninsulated to simulate long-term heat sinks. The top of the test vessel is equipped with a water film distributor shown in Figure 2.1-8 (see Appendix A, Drawing 2021E31 Sheet 11). The water film distributor consists of four independently controlled sectors of "J-Tubes" that distribute water evenly over the vessel dome at radii of 27 and 5 in. Each sector may be independently closed to produce a dry vessel in quaner intervals. The flow rate to the dome may also be reduced by adjustment of the flow control valve to produce additional rnA3378w.non.itro81898 2-10 Rev.I
4 FINAL water film striping effects. The excess water flowing off the vessel is collected and directed through a j flow meter prior to disposal. 2.1.7 Axial Fan
'Ihe axial fan is mounted in the annulus exit duct and provides controlled velocity air flow in the cooling air annulus for the AP600 tests requidng air velocities in excess of natural convection airflow.
The fan is 48 in. in diameter and 36 in. tall. I 2.1.8 Helium Addition A 0.25 in. port is provided in the steam-supply line near the bottom of the vessel to inject helium into i the test vessel to simulate light, noncondensible evolution in a containment vessel. The temperature, i l pressure, and flow rate of the helium are monitored to maintain constant flows during helium addition. l 1, I i 1 l l-i nrus7s..non ib.osis9s 2-11 Rev.I L____--- _---_- --_---.--_---- - - - - - - - - - - _ - - _ - _ _ _ - -
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--ete s INTERNAL HEAT SINKS Figure 2.15 Cross Section Internal Heat Sinks mA3578w.non.it481898 2-16 Rev.1
FINAL 1 l I , 1 1 \ LARGE SCALE PCCS TEST Vater Supply 8. Dnuo Sys%ns
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FL%L 2.2 Instrumentation and Measurements This section provides a description of each piece of instrumentation used on the facility. Table 2.2-1 summa:izes the instrumentation and accuracy of each measurement based on manufacture's data or upon operating experience (whichever is greater). 2.2.1 Condensate Flow Indirect measurement of the steam flow by condensate collection is only effective during steady-state conditions since there is some delay between when the steam enters the vessel and the steam condenses. The condensate-measurement system collects the condensed steam from the inside of the vessel in a weigh tank, where the mass of condensate is continuously measured using an electronic scale. The scale reading was communicated to the data acquisition system (DAS) over RS232 interface and recorded, along with the coinciding time, at the same sampling rate selected for recording temperature measurements. Condensate temperature was measured as it drained from the vessel. Note that the test record contains all the condensate weigh-tank values including those that occur during the collection tank drain cycles. The differential measurements are reviewed, and the negative values are thrown out along with any that would be affected by the drain cycle (i.e., a data point taken shortly after the start of draining or just prior to the stop of draining). Some additional data points are retained based on a review of the specific values and rate considerations. 2.2.2 Pressure System pressure was monitored in the vessel gas space and in the steam-injection line at the steam flow meter. 2.2.2.1 Vessel Pressure Vessel steam pressure was measured using a pressure transducer, attached with 0.25 in. copper tubing to the test vessel. For phase 2 tests, the transducer was moved from the control room to a location at the test vessel, thus eliminating the possibility of a water head in the communication lines. The
. pressure transducer has an accuracy of 1/4 percent (or 0.4 psi) with a output conversion:
Pinternal = 0.3083
- 1238 - 24.260 (1) where:
l Pintern j = internal vessel pressum (psia) ) I 1238 = data output channel (238) (mv) j nus78w.non:lb-081898 2-20 Rev.1 i- _ __
FINAL. 1 Differences between ambient pressure and the pressure transducer on the order of 1 to 2 psi were noted at the start of tests with the vessel vented as reported in the " Quick Look Reports"
)
(References 6.1 - 6.12). Comparison of the transducer output with the sampling apparatus transducers (4) indicate that the transducer is maintaining an average of -0.05 psi difference with the sampling j i apparatus transducers with a standard deviation of 0.29. Therefore, no correction is recommended. ) ? 2.2.2.2 Steam Inlet Pressure I For phase 2 tests, the pressure transducer is mounted directly below the vortex flow meter and is maintained in a water-filled condition that provides a 15.5 in, water head (0.56 psi) to the transducer i sensing element. During high steam flow tests ut lizing the rental boiler (See Section 2.1.3.2), the water head increases to 22.5 in. (0.81 psi). The pressure transducer has an output conversion as follows: P,i = 0.347
- I293 - 39.643 - C (2) l l,
where: P,i = steam line pressure (psia) 1293 = output channel (millivolts) l C = correction for water head (psi) Note: Equation used in data reduction was 0.3478
- 1293 - 39.72-C, which represents a deviation of less than 0.05% at test conditions.
Review of the calibration records indicates that the pressure transducer has an accuracy of 1/4 percent of full scale ( 0.25 psi) through the range of usage. Review of the transducer outputs at test conditions indicate that the pressure calculated from the above equation is approximately 1 psi below the pressure of the test vessel. Based on the difference between the two sensors (Channels 238 and 293) at atmospheric pressure it is estimated that Channel 293 may be reading low by approximately 2 to 3 psi. 2.2.3 Wind Speed and Direction A weather vace/ anemometer was mounted on the roof of the building 90 ft. to the west of the test i tower approximately 12 ft. above ground level. The wind speed and direction were recorded on the l
- sa:us7sw.non: b-osis98 2-21 Rev.1 L_--__-______-_-__-__________________-_-___-_____-_-________-__________-__--____________________-_-_--_
FINAL
. DAS and continuously monitored and recorded during all of the tests reported herein on DAS channels 240 and 241, respectively. The DAS values are in millivolts and are converted as follows: ;
Vwind = 100
- 1240 (3)
D ' = 360
- 1 241 (4) where:
Vwind = velocity of wind (miles /hr) 1240 = data output channel (240) (mv) D = direction of wind (*) 1241 = data output channel (241) (mv), O and 1 are west through the manway, clockwise. This dr.ta was used to confirm that the steady-state test data was not influenced by high-average local wind' conditions in excess of 5 mph during natural convection tests. Tests performed under forced convection (~8 ft/sec) were accepted at local conditions averaging less than 6 mph. The direction is defined relative to the coordinate system of the vessel as shown in Figure 2.2-1, 2.2.4' Vessel Water Cooling Flow
. The vessel cooling-water flow to the top of the vessel is measured with a Brooks "Maglite" magnetic flow meter that provides output to the DAS. The millivolt output signal is converted to pounds per second by the following relation:
F , = (0.01054
- 1242 - 0.016)
- p219 @
where: Fon = water flow to top of vessel (Ibm /sec) 1242 = data output channel (242) (mv) p219= water density at cooling water temperature (channel 219) (lbm/ft.3) s W578w.noa:1b 081898 2-22 Rev.I
~ .. . - _ _ _ _ - _ _ _ _ - - _ _ _ _ _ _ - _ _ _ _ _ _ _ -
r-I i FINAL l An automated tiow-measurement system collects the excess water into a standpipe installed below the test vessel that discharges through a Brooks "Maglite" magnetic flow meter that provides output to the l DAS. The millivolt output signal is converted to pounds per second by the following relation: 1 Fog = (0.01021
- 1243 - 0.016)
- p220 (6) 1 I
where: l Fog = excess water flow to bottom of vessel (lbm/sec) 1243 = data output channel (243) (mv) p220= water density at water discharge temperature (channel 220) (Ibm /ft.3) Various water cooling flow rates result in a striped wetting of the test vessel. When complete wetting does not occur, the width of the dry strips are measured along the circumference of the vessel at the bottom of the baffle during the test. This data is converted into a percent value for reporting herein. 2.2.5 Steam Flow Steam flow rates to the vessel were measured by three methods:
- directly by a vortex shedding flow meter e directly by a variable orifice flow meter e
indirectly by measurement of the rate of condensate collection (discussed in Section 2.2.1). 2.2.5.1 3-In. Vortex Meter The steam meter measures the velocity of the steam in the steam line just prior to the vessel. The steam flow is then calculated by combining the steam propenies with the meter output and line sizes to obtain the steam flow rate. The steam meter provides steam flows up to 22 ft.3/sec. Flows in I m0578w.non:lb 0 BIB 98 2-23 Rev.I l
FINAL excess of 22.4 ft.3/sec saturate the meter's amplifier. Steam meter output is converted by the following l equation: vonex , 40.781
- I24 - 3.272 g y,
where: Syon,, = steam flow rate (lbm/sec) V, = specific volume steam (ft.3/lbm) 124 = output channel 244 (volts) The specific volume is evaluated from the steam-line pressure transducer (Section 2.2.2.2), mounted near the vortex meter and the steam-inlet temperature (channel 216). The steam-inlet temperature is measured using a 1/16-in.-diameter, stainless-steel sheathed, chromel-alumel thermocouple located just upstream of the steam distributor inlet. I 2.2.5.2 Gilflo Variable Orifice Flow Meter A second direct measurement of the steam flow is provided by a "Gilflo"-variable orifice flow meter. The meter provides direct steam-flow measurement as a millivolt signal (channel 333), which is proportional to full scale of the instrument (10,000 lbm/hr). The unit output is converted to engineering units by the following equation: Saiino = 0.00891333 - 0.712 (8) where: Soilno = steam flow rate (Ibm /sec) 1333 = output channel (millivolts) neus78w.natib481898 2-24 Rev.I
FINAL. i i 2.2.5.3 6 In. Vortex Meter (Phase 3 Tests) i 1 l l The steam meter measures the velocity of the steam in the steam line just prior to the vessel. The steam flow is then calculated by combining the steam properties with the meter output and line sizes l to obtain the steam flow rate. Steam meter output is converted by the following equation: l l 0.10526 *1335 - 8.426 l Syon,x = (9) 1 where: S vonex = steam flow rate (Ibm /sec) V, = specific volume steam (ft.3/lbm) l 1335 = utput channel 335 (volts) De specific volume is evaluated from the steam-line pressure transducer (channel 293, See Section 2.2.2.2) mounted near the vortex meter and the steam temperature (channel 334) at the steam flow meter. The steam temperature is measured using a 1/16 in. diameter stainless-steel sheathed, chromel-alumel thermocouple located just upstream of the steam distributor inlet. i 2.2.6 Annulus Differential Pressure The annulus is instrumented with a differential pressure transducer mounted approximately 3 in. below the fan assembly. The pressure transducer measures the pressure differential between the inside and the outside of the baffle at the fan entrance location. The meter output conversion is shown below: l l APAnn = .003122
- 1294 - 0.249 (10) l where:
APAnn = annulus differential pressure (in. H2 O) i 1294 = data output channel (294) (mv) l l This output provides a positive pressure AP for operation with the fan on. m:\3578w.non:Ib-081898 2 25 Rev.1
Flut 2.2.7 Containment Annulus Air Flow and Temperature An ALNOR Thermo Anemometer was used to calibrate the air velocity in the cooling air annulus versus the fan shaft speed (rpm). AP600 testing with the water cooling film prevents velocity measurements during testing due to the high humidity in the annulus. The air velocity was obtained by performing air velocity traverses after the water cooling was terminated. The traverses were conducted at six circumferential positions at two elevations along the vertical annulus; each traverse consisted of eight velocity measurements across the annulus width. The ALNOR measures the mass velocity of the air referenced to standard atmospheric conditions and therefore, requires the velocity readings to be corrected to the actual conditions at the measurement site. To obtain the actual local annulus air velocities, the test velocity measurements were corrected as follows: V, = V gCf (11) where: V, = actual air velocity (ft/sec) V i= velocity indicated by Thermo Anemometer (ft./sec) Cf= correction factor = ds/da = 0.075*(459.7+Ti )/1.325*P, ds = air density (lb/cu ft) at standard calibration conditions da = actual air density at local temperature and barometric pressure P, = ambient pressure (in. Hg) T i = local air temperature (*F) at velocity measurement location The tests reported herein were setup using the fan ipm calibration determined above to provide a specific annulus velocity. The rpm calibration value provides a known volumetric flow under test conditions that will remain constant during the test. The velocities indicated in the test results in Section 4 are the exit velocities from the fixed anemometer. The calibration runs of fan rpm versus fixed anemometer and annulus velocity were correlated at ambient temperature to produce the following relationships: V,noujo, = 0.0232
- S rpm .01 (12)
V o= 0.0278
- S rpm - 0.87 (13) whe:e:
S,p, = fan shaft speed (rpm) V,nnuio, = velocity in annulus (ft/sec) m:\3578w.non:!b-o81898 2 26 Rev.I
DNA1. Vo = outlet air velocity (ft/sec) Comparison of the data from three or four test runs at each velocity (8.18,13.01, and 16.8 ftisec) indicate a standard deviation of approximately 1.7 percent for the rpm's tested (358,530, and 720). l' l No differences v'ere noted between dry calibration runs and ones with cold water flowing over the surface, l l The average air temperature entering the annulus was measured using four radiation-shielded thermocouple, spaced 90 degrees apart, located in the annulus inlet region. The average air l temperature leaving the annulus was measured using four sets of two thermocouple centered in equal areas at the outlet of the air annulus before the fan, with the two thermocouple in each set located l 90 degrees apart at radii of 12 and 20.78 in. in the 24-in.-radius fan inlet. Each thermocouple was , equipped with radiation shielding to obtain a truer air temperature reading. l l The fixed anemometer (Pacer) is installed in the outlet stack below the fan that is outputted to the DAS (channel 295). This unit measures the bulk air velocity at a position 7 in. from the wall of the outlet duct with a diameter of 2.75 in. The meter output conversion is shown below: l Vo = 66.125
- 1295 (I4) where:
Vo = outlet air velocity (ft/sec) 1295 = data output channel (295) (vohs)
- The local air temperature measurements for the inlet velocity correction were obtained by averaging l the four radiation-shielded thermocouple, spaced 90 degrees apart, located in the annulus inlet region.
The average air temperature leaving the baffle was measured using four sets of two thermocouple centered in equal areas at the outlet of the air annulus before the fan, with the two thermocouple in each set located 90 degrees apart. Each thermocouple was equipped with radiation shielding to obtain , a true air temperature reading.
)
2.2.8 Internal Velocity Five velocity sensors are used within the large-scale test vessel to monitor the flow of gas. All units are vane-type anemometers from two different manufactures: Pacer and H6ntzsch. I 2.2.8.1 Pacer l The second set of sensors (channels 296,297 and 298) are also vane-type anemometers (Pacer) but without integral directional output. The sensors have a throat diameter of 2.75 in, and are located with m:us78..non:ib-081898 2-27 Rev.I
FrNAL their centerlines approximately 2 in. from the vessel wall with their throats parallel to the wall. The sensors are located at E-90 degrees and D-180 degrees along the vertical wall and parallel to the dome at 345* (42-in.-radius). The elevation definition is shown if Figure 2.2-2. Direction of the gas flow was determined during operation by directing a small nitrogen flow at the anemometer vanes (Figure 2.2-3) while the output was monitored on a strip chart recorder; decreases in sensor output indicated that intemal velocities were in the opposite direction of that applied by the nitrogen flow, whereas, increases indicated flow in the same direction. Sensor output is converted to engineering units by the following relation: Vp = 66.125
- I) (15) where:
V p= " Pacer" anemometer velocity (ft/sec) I) = data output channel (j) (volts) Experience with the Pacer anemometers indicates that their performance is degraded by exposure to the steam environment inside the large-scale test vessel. Crude estimates indicate that the sensor dead band has shifted to approximately 5 ftisec after exposure to steam. 2.2.8.2 Huntzsch The units from H6ntzsch Instruments provide a directional output (channels 299 and 300) where negative is downward and positive is upward. The sensors are mounted with their throat parallel to the wall at A-90 degrees and Dome-165 degrees, respectively, approximately 0.5 to 1.5 in. from the vessel wall. The throat of the H6ntzsch is approximately 1 in. in diameter. Data is converted to engineering units by the following relation: (16) VH = 13.124
- I) - 65.62 where:
VH= H6ntzsch anemometer velocity (ft/sec) data output channel (j) (volts) I) = m:uS78w.non ib.osis9s 2-28 Rev.1
l FINAL 2.2.9 Containment Vessel Wall Temperatures Seventy-eight 0.032-in.-diameter, stainless-steel sheathed, chromel-alumel thermocouple attached to the outer vessel wall provided a measure of vessel surface temperature. Each thermocouple junction end was installed in a 1/32-in.-deep,1/32-in.-wide groove approximately 3/4 in. long and peened into place. The grooves were filled with solder and finished to provide a smooth outer surface. A matching thermocouple is located on the inside wall at each location to provide heat flux measurements. Figure 2.2-4 illustrates the installation of the wall temperature thennocouples. 1 2.2.10 Annulus Wall Temperatures The inner surface temperature of the 3-in. annulus wall was measured using fifteen 0.032-in.-diameter, I stainless-steel sheathed, chromel-alumel thermocouple attached to the inner surface of the acrylic cylinder. The wall thermocouple were located at each elevation where heat flux meters were placed; l wall thermocouple located on the diffuser section were located nearly opposite the 84-in.-radius flux meters (-79-in.-radius). 2.2.11 Vessel Fluid Temperatures Temperatures were measured inside the vessel and away from the vessel walls. Channels 66 through 79 and channels 170 through 186 record the intemal fluid temperatures approximately 1 in. inside the vessel wall. An additional 39 0.032-in.-diameter fluid thermocouple are mounted on an instrumentation rake mounted in the center of the test vessel. The rake thermocouple provide temperature data on the intemal fluid temperature distribution under the dome and at elevations A, B, C, and D (channels 245 through 283). An additional eight thermocouple are suspended under the operating deck (channels 284 through 291) to monitor the temperatures in the heel of the vessel. 2.2.12 Gas Sampling The gas sampling apparatus samples the atmosphere inside the test vessel to measure the ratio of non-condensables to condensables. The apparatus (Figure 2.2-5) consists of a heated sample tube, sample l bomb, purge bottle, and sample bottles. The sample tube is made up of concentric tubes with a l 0.01875-in.-diameter,400-watt heater down the center of the inside tube creating a 0.055-in.-wide l annulus around the heater for the gas sample to flow. Thermocouple are routed in the annulus to monitor the temperature of the gas being sampled and the temperature of the tube at various locations along the length of the tube. The sample bomb is a 5.37-in.3 volume that is instrumented with a thermocouple and a diaphragm isolated pressure gage *, The bomb is contained in a cylindrical baffle to allow hot and cold air to be directed at the bomb for heating and cooling operations. The purge bottle provides a 4.58 in.3 throw away volume to purge the lines prior to taking the actual gas sample. From test mn RC048 to the completion of testing the pressure gage was replaced with a pressure transducer, mA3578 v.non:lb.o81898 2 29 Rev.1
f ' FINAL. The sample bottles (4.58 in.3 each) collect samples for air / helium ratio analysis. Three helium samples are taken with most of the helium concentration measurements, and any value significantly different from the other two is discarded and not iacluded in the average value. The connecting piping is trace. heated to prevent the water vapor in the sample from condensing. A complete description and data reduction presentation are presented in Appendix B. The apparatus is capable of providing the concentration of air at the sampling location within 0.9 psi partial pressure of Gr. Up to four sample locations (dome 90 degrees at 63-in. radius, A-270 degrees, E-90 degrees and F-0 degrees) were employed during the phase 2 and phase 3 testing at positions approximately 6 in. inside the wall of the test vessel. The sample locations were identified by the cross-section dere the penetration was located (Drawing 2021E31, Sheets 5 and 6). 4 m:us78w.non:it>.osis9s 2-30 Rev.1
FINA1, TABLE 2.21
SUMMARY
OF TEST INSTRUMENTATION Calibration Sensor Description Model No. Channel No. Range Accuracy Pressure Transducer FOXBORO 238 0 to 117 0.26 psi SN-30031 psia YOUNG Wind Monitor (speed) AQ-05305 240 0 to 100 20.6 mph mph YOUNG Wind Monitor AQ-05305 241 0 to 360* z3' j (direction) l Water Flow Meter (Magmeter) BROOKS 242 0 to 30 gpm 20.1 gpm 4 SN-9201-19355 l Water Flow Meter (Magmeter) BROOKS 243 0 to 30 gpm 10.1 gpm SN-9306TH38497 3-in. Vortex Flow Meter BROOKS 244 0 to 22.55 0.23 E83W acfs acfs I SN-5422879 I l Pressure Transducer HONEYWELL 293 0 to 120 :0.25 psi ' NO. 3%14 psia l Differential Pressure Transducer OMEGA 294 0 to 1 in 0.006 in l PX656 HO 2 HO 2 Pacer Velocity Meter DTA 4000 295 0 to 33 20.5 ft/sec fusec Pacer Velocity Meter DTA 4000 296 0 to 33 0.5 ft/see ft/sec Pacer Velocity Meter DTA 4000 297 0 to 33 :0.5 ft/see ft/sec Pacer Velocity Meter DTA 4000 298 0 to 33 0.5 ft/sec ft/sec H6ntzsch Anemometer Velocity ZSR 30 GE 299 1 to 66 0.20 (ft/sec) MD 20728 ft/sec ft/sec H6ntzsch Anemometer Velocity ZSR 30 GE 300 1 to 66 0.15 (ft/sec) MD 20729 ft/sec ft/sec Gilflo Steam Flow Meter 4 IN. B 333 0 to 2.78 0.04 l SN-E0193 lb/sec lb/sec i nd3578w.non:lb-081898 2 31 Rev,1
FINAL TABLE 2.2-1 (cont.)
SUMMARY
OF TEST INSTRUMENTATION Calibration Sensor Description Model No. Channel No. Range Accuracy Endress Hauser 6-in. Vortex FTV1836-06-Al-2-HO 335 0 to 33.7 z0.25 Steam Flow Meter SN-1836-026873293 acfs acfs Fluke Data Logger Fluke 2286A NA 0 to 2372*F 0.8'F Scale #1, and FV 150KAl CONDM 0 to 300 lb 0.05 Scale #2, CARDINAL 738 CONDM2 0 to 400 lb 0.1 DETECTO MARLIN Thermocouple KK NUMEROUS 0 to 400*F 2'F I Ainor Hot Wire Anemometer 8500 NA 0.3 to 25 0.75 ft/see ft/sec EXTECH RPM meter - NA 300 to 1800 0.1 MTI Gas Chromatograph MT100 NA 0 to 50% 5% reading Sample Apparatus Data Logger ECD MODEL 50 NA 0 to 400'F $0.4*F FISHER - Helium Flow Meter 10A4555 NA 0- 4.6 CFM 0.07 CFM FOXBORO - Pressure 861 AM-BD1 NA 0-70 psia 0.14 psi Transducers - Gas Sampling Apparatus MARSHALL TOWN Pressure 91706 NA 0-300 psig 1.5 psi Gage Helium Injection MARSHALL TOWN - Pressure VDO NA 0-75 psia 20.4 psi Gage Early Gas Sampling Note:
- 1) Twelve thermocouple were calibrated with a resulting deviation of <2.05'F. Statistical analysis shows a maximum potential error band of 24'F. Thermocouple were purchased to premium grade
( 2*F). mM578w.non:lb.o81898 2 32 Rev.I
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FINAL, i l 2.3 Data Acquisition i Thermocouple temperature measurements and collected condensate weight were processed by a DAS and stored as part of the computer-generated portion of the test record Thermocouple were connected to the system by 20 AWG, chromel-alumel special limit (controlled-purity) duplex extension wires with solid PVC insulation. All thermocouple outputs were recorded using an electronic data logger unit. Thermocouple extensions were connected to isothermal terminal blocks that plugged into sets of low-level input cards on the data logger or an extender chassis that connected with the data logger. The voltage signals were converted to digital temperature as the data logger sequentially samples the inputs. The data acquisition was done according to a pre-selected sequence programmed into the data logger in accordance with the channel assignment shown in Table 2.3-1. The data logger acquires a set of data within an 8-second interval, but requires an additional 8 seconds to store the data to an internal floppy disk or approximately 30 seconds to store to the computer. Short term transient data is therefore accumulated on the intemal fioppy disk, while the remainder of the <iata is accumulated on the computer. Condensate weigh-tank output is only obtained during computer-controlled data acquisition and the data transformation program inserts a constant value during all times when the condensate data is unavailable. The locations of the thermocouple are identified in Table 2.3-1 by a code that identifies the vertical position (Figure 2.2-2) and the azimuth (Figure 2.21) at the vertical section. The dome of the vessel is divided into 5 levels, designated by their radius [ ]" and the side wall into cross sections A through F. In addition, thermocouple we'e added to the wall and air space below the operating deck. Thermocouple installed on the inside wall of the lower dome are identified with the prefix *BD" and are located between the existing thermocouple at the "F" cross-section and the operating deck, thereby dividing the area into approximate thirds; "H" indicates high and "L" indicates low. Thermocouple were also installed on the operating-deck grating (OD) and in the air space below the operating deck. Th thennocouples mounted below the operating deck are designated as "FH" and *FL" and again divide the vertical space below the operating deck into thirds from the vessel wall to the operating deck at the indicated radius and the angular orientation. Thermocouple installed on the heat sinks are identified by an "HS" prefix followed by a location code that identifies the heat sink group (A, B, C or D, see Figure 2.1-5), a plate designation "I," "O," and "M" (inside or short radius, outside or long radius and middle plate) and the location on the plate centerline top (T), center (C) and bottom (B). mA3578w.non !b-082098 2-38 Rev.2
FINrt. TABLE 2.31 LIST DATA CHANNEL ASSIGNMENT j Fluke Sensor Channel No. Tag No. Sensor Description Location 0 1 TC HEAT FLUX INSIDE DO-180-21 in. l 1 2 TC HEAT FLUX OUTSIDE DO-180-21 in. 2 3 TC HEAT FLUX INSIDE DO-210-42 in. 3 4 TC HEAT FLUX OUTSIDE DO-210-42 in. l 4 5 TC HEAT FLUX INSIDE DO-180-42 in.
$ 6 TC HEAT FLUX OUTSIDE DO-180-42 in. ;
1 6 7 TC HEAT FLUX INSIDE DO-150-42 in. l 7 8 TC HEAT FLUX OUTSIDE DO-150-42 in. 8 9 TC HEAT FLUX INSIDE DO-210-63 in. I 9 10 TC HEAT FLUX OUTSIDE DO-210-63 in. 10 11 TC HEAT FLUX INSIDE DO-180-63 in, i' l 11 12 TC HEAT FLUX OUTSIDE DO-180-63 in. 12 13 TC HEAT FLUX INSIDE DO-150-63 in. 13 14 TC HEAT FLUX OUTSIDE DO-150-63 in. 14 15 TC " BROKEN" DO-210-84 in. 15 16 TC HEAT FLUX OUTSIDE DO-210-84 in. 16 17 TC HEAT FLUX INSIDE DO-180-84 in. 17 18 TC HEAT FLUX OUTSIDE DO-180-84 in. 18 19 TC HEAT FLUX INJIDE DO-150-84 in. Let 19 20 TC HEAT FLUX OUTSIDE DO-150-84 in. l 20 21 TC HEAT FLUX INSIDE DO-120-21 in. 21 22 TC HEAT FLUX OUTSIDE DO-120-21 in. 22 23 TC HEAT FLUX INSIDE DO-120-42 in. mA357Sw.non:]b-08I898 2-39 Rev.I
FINAL l TABLE 2.31 (cont.) LIST DATA CHANNEL ASSIGNMENT Fluke Sensor Channel No. Tag No. Sensor Description Location 23 24 TC HEAT FLUX OUTSIDE DO-120-42 in. 24 25 TC HEAT FLUX INSIDE DO-60-42 in. 25 26 TC HEAT FLUX OUTSIDE DO-60-42 in. 26 27 TC HEAT FLUX INSIDE DO-105-63 in. 27 28 TC HEAT FLUX OUTSIDE DO-105-63 in. 28 29 TC HEAT FLUX INSIDE DO-90-63 in. 29 30 TC HEAT FLUX OUTSIDE DO-90-63 in. 30 31 TC HEAT FLUX INSIDE DO-60-63 in. 31 32 TC HEAT FLUX OUTSIDE DO-60-63 in. 32 33 TC HEAT FLUX INSIDE DO-120-84 in. 33 34 TC HEAT FLUX OUTSIDE DO-120-84 in. 34 35 TC HEAT FLUX INSIDE DO-60-84 in. 35 36 TC HE.AT FLUX OUTSIDE DO-60-84 in. 36 37 TC HEAT FLUX INSIDE DO-0-00 in. 37 38 TC HEAT FLUX OUTSIDE DO-0-00 in. 38 39 TC HEAT FLUX INSIDE DO-0-21 in. 39 40 TC HEAT FLUX OUTSIDE DO-0-21 in. 40 41 TC HEAT FLUX INSIDE DO-0-42 in. 41 42 TC HEAT FLUX OUTSIDE DO-0-42 in. 42 43 TC HEAT FLUX INSIDE DO-30-63 in. 43 44 TC HEAT FLUX OUTSIDE DO-30-63 in. 44 45 TC HEAT FLUX INSIDE DO-0-63 in. 45 46 TC HEAT FLUX OUTSIDE DO-0-63 in. 46 47 TC HEAT FLUX INSIDE DO-330-63 in. 47 48 TC HEAT FLUX OUTSIDE DO-330-63 in, mA3578w.non:ll 081898 2-40 Rev.1
FINat. l TABLE 2.31 (cont.) LIST DATA CHANNEL ASSIGNMENT Fluke Sensor I Channel No. Tag No. Sensor Description Location 48 49 TC HEAT FLUX INSIDE DO-0-84 in. 49 50 TC HEAT FLUX OUTSIDE DO-0-84 in. 50 51 TC HEAT FLUX INSIDE DO-210-21 in. 51 52 TC HEAT FLUX OUTSIDE DO-210-21 in. 52 53 TC HEAT FLUX INSIDE DO-300-42 in. 53 54 TC HEAT FLUX OUTSIDE DO-300-42 in. 54 55 TC HEAT FLUX INSIDE DO-240-42 in. 55 56 TC HEAT FLUX OUTSIDE DO-240-42 in. l 56 57 TC HEAT FLUX INSIDE DO-300-63 in. 57 58 TC HEAT FLUX OUTSIDE DO-300-63 in. 58 59 TC HEAT FLUX INSIDE DO-270-63 in. 59 60 TC HEAT FLUX OUTSIDE DO-270-63 in. 60 61 TC HEAT FLUX INSIDE DO-240-63 in. 61 62 TC HEAT FLUX OUTSIDE DO-240-63 in. 62 63 TC HEAT FLUX INSIDE DO-300-84 in. l 63 64 TC HEAT FLUX OUTSIDE DO-300-84 in. 64 65 TC HEAT FLUX INSIDE DO-240-84 in. 65 66 TC HEAT FLUX OUTSIDE DO-240-84 in. 66 67 TC FLUID DO-180-21 in. 67 68 TC FLUID DO-180-42 in. 68 69 TC FLUID DO-210-63 in. 69 70 TC FLUID DO-180-63 in. 70 ?I TC FLUID DO-150-63 in. 71 72 TC FLUID DO-180-84 in. 72 73 TC FLUID (INACTIVE) DO-195-63 in. m:\3578w.non:lb-081898 2-41 Rev.I
FINAt. TABLE 2.31 (cont.) LIST DATA CHANNEL ASSIGNMENT Fluke Sensor Channel No. Tag No. Sensor Description Location 73 74 TC FLUID (INACTIVE) DO-195-63 in. 74 75 TC FLUID DO-0-00 in. 75 76 TC " BROKEN" DO-0-21 in. 76 77 TC FLUID DO-0-42 in. 77 78 TC FLUID (INACTIVE) DO-15-63 in. 78 79 TC FLUID (INACTIVE) DO-15-63 in. 79 80 TC FLUID DO-0-84 in. 80 81 TC HEAT FLUX INSIDE A-210 81 82 TC HEAT FLUX OUTSIDE A-210 32 83 TC " BROKEN" A-180 83 84 TC HEAT FLUX OUTSIDE A-180 84 85 TC HEAT FLUX INSIDE A-150 85 86 TC HEAT FLUX OUTSIDE A-150 86 87 TC " BROKEN" B-180 87 88 TC HEAT FLUX OUTSIDE B-180 88 89 TC HEAT FLUX INSIDE B-150 89 90 TC HEAT FLUX OUTSIDE B-150 90 91 TC HEAT FLUX INSIDE C-210 91 92 TC HEAT FLUX OUTSIDE C-210 92 93 TC HEAT FLUX INSIDE C-180 93 94 TC HEAT FLUX OUTSIDE C-180 94 95 TC HEAT FLUX INSIDE D-180 95 96 TC HEAT FLUX OUTSIDE D-180 96 97 TC HEAT FLUX INSIDE D-150 97 98 TC HEAT FLUX OUTSIDE D-150 m:\3578w.non:Ib-08I898 2-42 Rev.I
FINAL TABLE 2.3-1 (cont.)
- LIST DATA CHANNEL ASSIGNMENT I
Fluke Sensor Channel No. Tag No. Sensor Description Location 98 99 TC HEAT FLUX INSIDE E-180 99 100 TC HEAT FLUX OUTSIDE E-180 100 101 TC HEAT FLUX INSIDE A-120 101 102 TC HEAT FLUX OUTSIDE A-120 102 103 TC HEAT FLUX INSIDE A-90 103 IN TC HEAT FLUX OUTSIDE A-90 IN 105 TC HEAT FLUX INSIDE A-60 105 106 TC HEAT FLUX OUTSIDE A-60 106 107 TC HEAT FLUX INSIDE B-120 i 107 108 TC HEAT FLUX OUTSIDE B-120 108 109 TC HEAT FLUX INSIDE B-90 109 110 TC HEAT FLUX OUTSIDE B-90 110 111 TC HEAT FLUX INSIDE B-60 111 112 TC HEAT FLUX OUTSIDE B-60 112 113 TC HEAT FLUX INSIDE C-120 113 114 'It HEAT FLUX OUTSIDE C-120 114 115 TC HEAT FLUX INSIDE C-90 115 116 TC HEAT FLUX OUTSIDE C-90 116 117 TC HEAT FLUX INSIDE C-60 I17 118 TC HEAT FLUX OUTSIDE C-60 118 119 TC HEAT FLUX INSIDE D-120 119 120 'I C HEAT FLUX OUTSIDE D-120 120 121 TC HEA FL73X INSIDE D-60 121 122 TC HEAT FLUX OUTSIDE D-60 . 122 123 TC HEAT FLUX INSIDE E-120 l mA3578w.non:Ib-081898 2-43 Rev.1
FINAL TABLE 2.3-1 (cont.) LIST DATA CHANNEL ASSIGNMENT Fluke Sensor Channel No. Tag No. Sensor Description Location 123 124 TC HEAT FLUX OUTSIDE E 120 124 125 TC HEAT FLUX INSIDE E-60 125 126 TC HEAT FLUX OUTSIDE E-60 126 127 TC HEAT FLUX INSIDE A-0 127 128 TC HEAT FLUX OUTSIDE A-0 128 129 TC HEAT FLUX INSIDE A-300 129 130 TC HEAT FLUX OUTSIDE A-300 130 131 TC HEAT FLUX INSIDE B-0 131 132 TC HEAT FLUX OUTSIDE B-0 132 133 TC HEAT FLUX INSIDE B-300 133 134 TC HEAT FLUX OUTSIDE B-300 134 135 TC HEAT FLUX INSIDE C-0 135 136 TC HEAT FLUX OUTSIDE C-0 136 137 TC HEAT FLUX INSIDE C-300 137 138 TC HEAT FLUX OUTSIDE C 300 138 139 TC AMBIENT AIR
- 139 140 TC HEAT FLUX OUTSIDE D-30 140 141 TC HEAT FLUX INSIDE D-300 141 142 TC HEAT FLUX OUTSIDE D-300 142 143 TC HEAT FLUX INSIDE E-30 143 144 TC HEAT FLUX OUTSIDE E-30 l
144 145 TC HEAT FLUX INSIDE E-300 145 146 TC HEAT FLUX OUTSIDE E-300 146 147 TC HEAT FLUX INSIDE A-270 147 148 TC HEAT FLUX OUTSIDE A-270 m:\3578u .non:lt> 081898 2 44 Rev.I
BNAL {
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TABLE 2.31 (cont.) LIST DATA CHANNEL ASSIGNMENT Fluke Sensor Channel No. Tag No. Sensor Description Location 148 149 TC HEAT FLUX INSIDE A-240 149 150 TC HEAT FLUX OUTSIDE A-240 150 151 TC HEAT FLUX INSIDE B-270 { 151 152 TC HEAT FLUX OUTSIDE B-270 152 153 TC HEAT FLUX INSIDE B-240 153 154 TC HEAT FLUX OUTSIDE B-240 154 155 TC HEAT FLUX INSIDE C-270 155 156 TC HEAT FLUX OUTSIDE C-270 ! 156 157 TC HEAT FLUX INSIDE C 240 157 158 TC HEAT FLUX OUTSIDE C-240 158 159 TC HEAT FLUX INSIDE D-240 159 160 TC HEAT FLUX OUTSIDE D-240 160 161 TC HEAT FLUX INSIDE E-240 161 162 TC HEAT FLUX OUTSIDE E-240 162 163 TC HEAT FLUX INSIDE F 120 163 164 TC HEAT FLUX OUTSIDE F-120 164 165 TC HEAT FLUX INSIDE F-30 165 166 TC HEAT FLUX OUTSIDE F-30 166 167- TC HEAT FLUX INSIDE F 330 l 167 168 TC HEAT FLUX OUTSIDE F-330 168 169 TC HEAT FLUX INSIDE F-240 169 170 TC HEAT FLUX OUTSIDE F-240 170 171 TC FLUID A-210 171 172 TC FLUID A-180 172 173 TC FLUID A-90 l l mM578w.non:1b-ost s9s 2-45 Rev.I
FmAL l TABLE 2.31 (cont.) LIST DATA CHANNEL ASSIGNMENT Fluke Sensor Channel No. Tag No. Sensor Description Location 173 174 TC FLUID B-180 174 175 TC FLUID B-90 175 176 TC FLUID C-180 176 177 TC FLUID C-90 177 178 TC FLUID D-180 178 179 TC FLUID E-180 179 180 TC FLUID A-0 180 181 TC FLUID A-270 181 182 TC FLUID B-0 182 183 TC FLUID B-270 183 184 TC FLUID C-0 184 185 TC FLUID C-270 185 186 TC FLUID D-30 186 187 TC FLUID E-30 187 188 TC FLUID (INACTIVE) F-180 188 189 TC FLUID (INACTIVE) F0 189 190 TC AIR OUTLET "F" FI-180-12 in. 190 191 TC AIR OUTLET FI-180-20.75 in. 191 192 TC AIR OUTLET "I" FI-90-12 in. 192 193 TC AIR OUTLET FI-90-20.75 in. 193 194 TC AIR OUTLET "A" FI-0-12 in. 194 195 TC AIR OUTLET FI-0-20.75 in. 195 196 TC AIR OUTLET "J" FI-270-12 in. 196 197 TC AIR OUTLET FI-270-20.75 in. 197 198 TC DOME BAFFLE DO-180 m:\3578w.non:Ib-081898 2 46 Rev.I
FINAt.
)
TABLE 2.3-1 (cont.) LIST DATA CHANNEL ASSIGNMENT Fluke Sensor Channel No. Tag No. Sensor Description Location 198 199 TC DOME BAFFLE DO-90 199 200 TC DOME BAFFLE DO-O 200 201 TC DOME BAFFLE DO-270 201 202 TC ANNULUS BAFFLE B-203 202 203 TC ANNULUS BAFFLE D-203 203 204 TC ANNULUS BAFFLE A-113 204 205 TC ANNULUS BAFFLE B-113 205 206 TC ANNULUS BAFFLE C-ll3 206 207 TC ANNULUS BAFFLE D-113 207 208 TC ANNULUS BAFFLE E-113 208 209 TC ANNULUS BAFFLE B-23 209 210 TC ANNULUS BAFFLE D-23 210 211 TC ANNULUS BAFFLE B-293 211 212 TC ANNULUS BAFFLE D-293 212 213 TC AIR INLET "B" AI-203 213 214 TC AIR INLET Al-113 214 215 TC AIR INLET "C" AI-23 215 216 TC AIR INLET Al-293 216 217 TC STEAM INLET VESSEL "H" S-1 1 217 218 TC CONDENSATE OUT #2 "G" 218 219 TC COOLED CONDENSATE ! 219 220 TC FILM WATER IN "D" 220 221 TC FILM WATER OUT "E" 221 222 TC TRAVERSE KNUCKLE TK-203 222 223 TC TRAVERSE KNUCKLE TK-113 1 mA3578w.non.lb 081898 2 47 Rev.I
FINAL TABLE 2.31 (cont.) LIST DATA CHANNEL ASSIGNMENT Fluke Sensor Channel No. Tag No. Sensor Desen ition Location 223 224 TC TRAVERSE KNUCKLE TK-23 224 225 TC TRAVERSE KNUCKLE TK-293 225 226 TC TRAVERSE MID TM-203 226 227 TC TRAVERSE MID TM-I l3 227 228 TC TRAVERSE MID TM-23 228 229 TC TRAVERSE MID TM-293 229 230 TC TRAVERSE LOWER TL-203 230 231 TC TRAVERSE LOWER TL-113 231 232 TC TRAVERSE LOWER TL-23 232 233 TC TRAVERSE LOWER TL-293 233 234 TC STEAM PIPE S-2 234 235 TC STEAM PIPE S3 235 236 TC STEAM PIPE S-4 236 237 TC STEAM PIPE S-5 237 238 TC STEAM PIPE INLET S-6 4 238 239 MV VESSEL PRESSURE P-1 l 239 TC CONDENSATE OUT #1 240 MV WIND VELOCITY " 241 MV WIND DIRECTION " 242 MV WATER FLOW METER " 243 MV FILM WATER OUT I 244 MV 3 INCH STEAM METER Vortex 245 TC INTERNAL TC RAKE DO-9 in.-0 in.-0 246 TC INTERNAL TC RAKE DO-28 in.-18 in.-180 247 TC INTERNAL TC RAKE DO-28 in.-0 in.-0 m:us78w.non:1b-081898 2-48 Rev.I
FINAL ' TABLE 2.31 (cont.) LIST DATA CHANNEL ASSIGNMENT ' Fluke Sensor Channel No. Tag No. Sensor Description Location l 248 TC INTERNAL TC RAKE DO-28 in.-18 in.-0 249 TC INTERNAL TC RAKE A-78 in.-180 250 TC INTERNAL TC RAKE A-66 in.-180 l I 251 TC INTERNAL TC RAKE A-54 in.-210 252 TC INTERNAL TC RAKE A-54 in.180 253 TC INTERNAL TC RAKE A-54 in.-150 254 TC INTERNAL TC RAKE A-36 in.-180 255 TC INTERNAL TC RAKE A-18 in.-180 256 TC INTERNAL TC RAKE A-0 in.-0 257 TC INTERNAL TC RAKE A-78 in.-0 258 TC INTERNAL TC RAKE B-78 in.-180 259 TC INTERNAL TC RAKE B-66 in.180 260 TC INTERNAL TC RAKE B-54 in.-210 261 TC INTERNAL TC RAKE B-54 in.-180 262 TC INTERNAL TC RAKE B-54 in.-150 263 TC INTERNAL TC RAKE B-36 in.-180 264 TC INTERNAL TC RAKE B-18 in.-180 265 TC INTERNAL TC RAKE B-0 in.-0 266 TC INTERNAL TC RAKE B-78 in.-0 267 TC INTERNAL TC RAKE C-78 in.-180 268 TC INTERNAL TC RAKE C-66 in.-180 l 269 TC INTERNAL TC RAKE C-54 in.-210 270 TC INTERNAL TC RAKE C-54 in.-180 271 TC INTERNAL TC RAKE C-54 in.-150 272 TC INTERNAL TC RAKE C-36 in.-180 mM578w.non:Ib-081898 2-49
FINAL TABLE 2.31 (cont.) LIST DATA CHANNEL ASSIGNMENT Fluke Sensor Channel No. Tag No. Sensor Description Location 273 TC INTERNAL TC RAKE C-18 in.-180 274 TC INTERNAL TC RAKE C-0 in.-0 275 TC INTERNAL TC RAKE C-78 in.-0 276 TC INTERNAL TC RAKE D-78 in.-180 277 TC INTERNAL TC RAKE D-66 in.-180 278 TC INTERNAL TC RAKE D-54 in.-210 279 TC INTERNAL TC RAKE D-54 in.-180 280 TC INTERNAL TC RAKE D-54 in.-150 281 TC INTERNAL TC RAKE D-18 in.-180 282 TC INTERNAL TC RAKE D-0 in.-0 283 TC INTERNAL TC RAKE D-78 in.-0 284 TC LNTERNAL TC RAKE FH-45 in.-0 285 TC INTERNAL TC RAKE FL-45 in.-0 286 TC INTERNAL TC RAKE FH-45 in.-90 287 TC INTERNAL TC RAKE FL-45 in.-90 288 TC INTERNAL TC RAKE FH-26 in.-180 289 TC INTERNAL TC RAKE FL-26 in.-180 290 TC INTERNAL TC RAKE FH-45 in.-270 291 TC INTERNAL TC RAKE FL-45 in.-270 292 MV STEAM VALVE PRESSURE na 293 MV STEAM LINE PRESSURE At Vortex Meter 294 MV ANNULUS DELTA P Below Fan 295 MV BULK AIR VELOCITY Below Fan DISCHARGE 296 MV VELOCITY METER Pacer E-30* 297 MV VELOCITY METER Pacer D-180* m.us78w.non:ib-081898 2-50
l FINAL l I l TABLE 2.3-1 (cont.) l LIST DATA CHANNEL ASSIGNMENT I Fluke Sensor i Channel No. Tag No. Sensor Description Location 298 MV VELOCITY METER Dome-345'-42 in. I 299 MV VELOCITY METER A-90' 300 MV VELOCITY METER Dome-165'-42 in. 301 TC HEAT SINK TEMPEP.ATURE HS-C-I-C 302 TC HEAT SINK TEMPERATURE HS-C-M-T 303 TC HEAT SINK TEMPERATURE HS-C-M-C 304 TC HEAT SINK TEMPERATURE HS-C-M-B , l 305 TC HEAT SINK TEMPERATURE HS-C-O-C 306 TC HEAT SINK TEMPERATURE HS-A-I-C 307 TC HEAT SINK TEMPERATURE HS-A-M-T 308 TC HEAT SINK TEMPERATURE HS-A-M-C 309 TC HEAT SINK TEMPERATURE HS-A M-B 310 TC HEAT SINK TEMPERATURE HS-A-O-C l 311 TC HEAT SINK TEMPERATURE HS-D-I-C 1 312 TC HEAT SINK TEMPERATURE HS-D M-T 313 TC HEAT SINK TEMPERATURE HS-D-M-C 314 TC HEAT SINK TEMPERATURE HS-D-M-B 315 TC HEAT SINK 'EMPERATURE HS-D-O-C l 316 TC HEAT SINK TEMPERATURE HS-B-1-C l 317 TC HEAT SINK TEMPERATURE HS-B-M-T 318 TC HEAT SINK TEMPERA TURE HS-B-M-C 319 TC HEAT SINK TEMPERATURE HS-B-M-B t 320 TC HEAT SINK TEMPERATURE HS-B-O-C 32! TC INSIDE WALL BD-330*-H TEMPERATURE mA3578w.non:Ib-081898 2-51 C_ _ _ _____ _ _ _
1 FINAt. f TABLE 2.31 (cont.) LIST DATA CIIANNEL ASSIGNMENT Fluke Sensor Channel No. Tag No. Sensor Description Location TC INSIDE WALL B D-330*-L 322 TEMPERATURE 323 TC INSIDE WALL BD-30*-H TEMPERATURE 324 TC INSIDE WALL BD-30*-L TEMPERATURE 325 TC INSIDE WALL BD-120 -H TEMPERATURE 326 TC INSIDE WALL B D-120'-L TEMPERATURE 327 TC INSIDE WALL B D-210*-H TEMPERATURE 328 TC INSIDE WALL BD-210*-L TEMPERATURE 329 TC GRATING TEMPERATURE OD-O'-45 in. 330 TC GRATING TEMPERATURE OD-90*-45 in. 331 TC GRATING TEMPERATURE OD-180*-75 in. 332 TC GRATING TEMPERATURE OD-270'-45 in. 333 MV GILFLO STEAM METER FACILITY STEAM LIST 334 TC HIGH CAPACITY STEAM HIGH CAPACITY TEMPERATURE 3 STEAM LINT 335 MV 6 In. VORTEX STEAM HIGH CAPACITY METER 2 STEAM LINT Note:
- 1) Used only for the high capacity boiler tests.
mA3578w.non:lb-081898 2-52
i FINA1. 2.4 Facility Operation All the large-scale tests reported herein were essentially performed in the same manner. Specific j differences, such as vessel pressure, steam flow rate, degree of water coverage, rate of annulus air I flow, and presences of light noncondensables are noted in the description of the individual tests. The following is a summary of the detailed test procedure used for the tests reported.
- 1. Test instrumentation calibration and setup were verified prior to the start of the test. Three strip chart recorders were setup to receive real-time signals throughout the test for key va iables, such as steam flow rate and temperature, vessel pressure, and internal velocity meter outputs. The anibient conditions of pressure and humidity are recorded. Tests are conducted only when the ambient air relative humidity is 100 percent or less at 88*F and lower temperature,80 percent at 95*F or 68 percent at 100 F.
- 2. The test vessel is closed up and the DAS is cycled to provide the initial vessel conditions prior to test.
- 3. De steam boiler is fired up to produce steam at approximately 100 psig, and pipe trace heating is activated to prevent condensation in the steam supply lines to the test section. Prior to starting the test, the steam is vented to atmosphere to get to full operating conditions.
- 4. Water flow is established to the top of the dome, as prescribed by the test conditions. The water flow rate for specific striped coverage conditions was predetermined with a reference 1 lb/see steam flow rate. He required air flow rate was established, as prescribed by the test condition on the basis of the required fan rpm level.
- 5. The DAS is activated prior to the start of steam flow to the test section. In the majority of tests, the DAS was operated in local mode for the first 10 minutes of each transient before reverting to computer mode with data accumulated approximately every 2 minutes. He data is stored to unique file names for later data handling. The steam system is opened to provide the reqfred steam flow to the test vessel.
- 6. During performance of the test, the distribution of water coverage at the bottom of the baffle was recorded during the steady state portion of the test. Noncondensible and helium samples were taken at approximately one hour intervals, as required by the individual test, to determine the concentration of noncondensables.
I l I l l l m:\3578w.non:Ib-o81898 2-53
FINA1. 1 3.0 DATA REDUCTION This section describes the data handling activities and test evaluations performed on the PCS Large Scale Test data. 3.1 Data Acquired 1 i . l The data is accumulated during the tests in the following forms: l j 1. The Test Record Book, which provides documentation of the conduct of the test, includes any anomalies that may be experienced during the conduct of the test, and contains a record of the history of the test facility. l
- 2. The Fluke Data Acquisition System (DAS) output, which is stored directly to disk i'
(note that no data reduction is performed during these operations. The thermocouple are directly recorded in degrees Fahrenheit and all others in actual millivolt or volt j signals. '
- 3. Strip Chart recorders which provide a qualitative description of the conduct of the test for selected channels.
- 4. Data recorded by hand on data sheets and on the individual test procedures. This data includes gas sampling data, helium concentration data, atmospheric pressure and weather conditions.
3.2 Data Handling The primary source of the test data is that recorded on the Fluke DAS. The Fluke data is an ASCII file containing the values of the 335 chaimels used for each data recording. The data is recorded in two modes as described in Section 2.3. The computer data is separated at the times where data acquisition on the internal floppy takes over. The separated data is then rejoined to produce the complete test record file using the unique time-indexed records. Data relating to the hand input data is inserted at the beginning of the test file. There are two types of hand input data. Test identification and prerequisite data, which must be included in each hand input data set; and recorded data, which is data recorded by the test engineer and may or may not exist for a given test. Only the initial set of conditions is recorded in the hand input data. Failed charmels are identified and are zeroed out by the i Fortran code to avoid misinterpretation of the data. l The LPCCS Fortran code is written to transform the data recorded by the Fluke data acquisition l equipment of the test facility into a Foxpro data base and/or Lotus spreadsheet format. Figure 3.2-1 ! shows a simplified flow chart of the operations performed. A final data base provides the reduced data calculated on the basis of the equations noted in Section 2.2. l l mM578w.1.non:Ib421898 3-1 ___ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ . _ _ _ _ _ . _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ __ _ _ _ _ _ . - __ ]
FINAL The reduced data from start to completion of these tests is presented as compressed ASCII files in i Appendix D of this document. The data files are identified as "RC0xxFl.PRN", "RC0xxF2.PRN",
"RC0xxF0.PRN", and (where appropriate) "RC0xxTR.PRN" and are contained within the archive file "RC0xx. ZIP" where the "xx" identifies the specific run number of the test in question. Files ending in "Fl" contain reduced data from channels 0 through 243; files ending in "F2" contain reduced data from channels 244 through 335; files ending in "F0" contain selected manually recorded data and test descriptions, and average, maximum and minimum temperatures for each level as a function of time.
A definition of the outputs and their units is contained in Appendix C, Table C.1-3. The non-DAS (noncondensible) data is collected and where appropriate is entered into files with the DAS-generated data. Noncondensible data is acquired separately and evaluated in accordance with the procedure identified in Appendix B. m:\3578w.l non:lb-081898 3-2 Rev.I
i FINAL I l l l l l l l z , , c
! 8 ! 8 X i.
s 5 a g l. k g l
! l l i I! E g!
! [3 1 I! 8 !
[-
=
i i l i li l 1 l gi1:i 1:i i.j n 1 i a t , is : !:!! - B 3 E I:_l ,l lli llll i_ l _ i i_ ll1 "! i
-l:!
e 5 5 n lvI <5^> - g g __ _ . _ _ _ _ . _ _ . _ _ a a a 1 5 I I l l s 8 a l I I i 1 I g I a a , i a 'i : ; 8 ll l -<^>i- 1 i l l
- Figure 3.21 Data Handling Process i
l m:\3578w 1.non:Ib 08I898 33 Rev.1 l
FINAL 3.3 Test Evaluation 3.3.1 Test Acceptance The following test acceptance criteria were established for the tests reported herein: 1, Data on forcing functions are available, i.e. steam flow rate, fan speed, water flow rates, inlet temperatures of steam, water and air. Strict adherence to the specific absolute pressures and flow rates is not necessary but values should be nearly constant as defined in the test matrix.
- 2. Data on response variables are available, i.e. condensate flow rates, excess water flow rates, air, water md steam outlet temperatures, vessel pressure, 80 percent of the vessel and fluid temperatures, and vessel water coverage measurements were taken.
- 3. Unplanned excursions must be evaluated on a case by case basis. Failures that may result in faulty data outputs are not acceptable.
- 4. The vessel pressure is maintained within the specified pressure limits during the constant pressure portions of these tests.
3.3.2 Test Analysis ne LST steady state data presented in Section 4 was obtained through a review of the test history recorded by the data acquisition system. De data representing steady state pressure conditions ( 0.5 psig over a minimum of 15 minutes) was isolated for further review. This portion of the data was further scanned for best overall steady state conditions (e.g. calm winds, steady vessel wall temperatures, internal fluid temperatures, etc.). Condensate drain weights in the isolated data were reviewed to ensure that only condensate weight values corresponding to tank fill periods were considered in calculation of the condensate flow rates, i.e. values affected by the start and stop of condensate tank draining were excluded. In some cases, due to very large condensation rates, it was necessary to select the beginning and end of fill periods by use of specifically identified fill times or by inspection of the time history data. He isolated data was then averaged ar.d the overall results are tabulated in the average steady sate tabulations of Section 4. This data reflects the averages of the temperatures at the various test vessel elevations. De temperature distribution of each elevation was also reviewed to provide a comparison of the average, maximum and minimum temperatures on the inside and outside vessel walls together with the maximum, minimum and average differential temperatures. De individual outside wall temperatures and differential temperatures at each cross section can vary significantly due to locally high heat flux resulting from subcooled water (50 to 110*F) applied to the top of the vessel and due to a non-uniform distribution of water over the vessel surface (striped surface). De high differential temperatures are most likely the result of subcooled fluid on the vessel, whereas, the low differential temperatures and heat fluxes are the result of dry vessel surface areas. All differential temperatures reported were corrected for the calibration offset mus7sw.i.non:ttros1898 34 Rev.1
FINAL (Table 3.3-1) obtained by monitoring the vessel over a 48 hour period at ambient conditions. Data recorded in the "FO" files of Appendix C and D also contain maximum, minimum, and average I temperatures and differential temperatures as a function of time. The differential temperatures reported I in the "FO" files were not corrected for the calibration offset of Table 3.3-1. Table 3.3-2 presents a summary of the tests performed during Phase 2 and Phase 3 of the PCS test program. Repeat test runs were performed where tests did not meet the test requirements or pertinent , test data was missing. The reasons for repeating tests are also indicated in Table 3.3-2. l l l 3.3.2.1 Heat Balance l Table 3.3-3 provides a rough comparison of the heat loads as calculated from the various measurements listed below: 1
- i. Condensate mass flow rate
- External heat loss (water, air and radiation) l
- Heat flux across the wall J
Figure 3.3-1 illustrates the various heat balance calculations relative to the heat loss calculated from the condensate measurement. Table 2.0-1 provides estimates of the test vessel and baffle surface areas and the applicable flow areas for use in evaluation of the test data. The indicated position of the area j is approximately at the middle of the identified area. The condensate heat load was calculated from the enthalpy of the steam entering minus the enthalpy of the condensate leaving while the system was at steady state; condensate flow was used for both the steam flow into the vessel and the condensate l flow out of the vessel. The external heat loss sums the heat pickup of the coolmg water, the heat of vaporization of water, the heat pickup of air and the estimated heat losses to the environment due to l corivection and radiation from the vessel bottom and baffle sides using the ambient temperature as T . 2 The convection losses were estimated using a heat transfer coefficient of 1 BTURhr*ft **F). The convective and radiation heat losses from the bottom of the vessel were assumed negligible for all tests with an insulated bottom (Test runs less than RC053). The equations used are shown below: l 9cond " cond (H steam -Hcond) U) l 9env " 9 air + 9 water
- 9 bottom
- 9 baffle (2) 9wan = { A (f,,,
j Atma.i + (I - fwet) ATmin.i) (3) l N i I air + Hwatervapor.out (W,,,,,,jn - W,,,,,,,,,) 9 air " air Cp. air (Iair,out
- I .in) (4) m:us78w.i.non:ib-081898 3-5 Rev.1
l FINAL l 9 water =H water.out W,,ter,out -H water.in W water.in (5) where: 9cond
= heat loss calculated from the condensate flow (BTU /hr)
Wcond = mass flow of condensate (Ib/hr) H,te,, = enthalpy of steam into vessel (BTUAbm) H eond = enthalpy of condensate leaving vessel (BTUAbm ) 9env
= estimate of heat lost to environment via air and water (BTU /hr) gair = estimate of heat lost to air in annulus (BTU /hr) q ,,,,, = estimate of heat lost to water flowing over the vessel and collected in the gutter (BTU /hr) qbottom = estimate of heat lost from convection and radiation on the bottom of the vessel (BTU /hr) qbaffle = estimate of heat lost from convection and radiation on the outside surface of the baffle (BTU /hr) q,,ii = the heat loss calculated from temperature drop across the wall (BTU /hr)
W,i, = mass flow of air through the annulus (lb/hr) 2 Ai = area of the cross section of interest (ft ) k = thermal conductivity of steel (BTU *in/(ft2 *hr**F)) I = thickness of vessel wall (in) f ,, = estimate of the fraction of circumference that is wetted ATmax.i = maximum temperature difference of cross section i (*F) ATmin.i = minimum temperature difference of cross section i (*F) Cp,,i, = heat capacity of air (BTU /(Ib**F))
= temperature at inlet to baffle Tair.in T,ir,,,, = temperature at outlet of baffle H ,,t,,y,por,,,, =enthalpy of water vapor leaving the annulus (BTUAb)
H ,,,,,,,,, = enthalpy of water leaving the vessel outside gutter (BTUAb) Wwater.in = mass flow of water to the top of the vessel (Ib/hr) W,,,,,,oot = mass flow of water out of outside vessel gutter (lb/hr) H ,,,,,i, = enthalpy of water onto the top of the vessel surface (BTUAb) i Equation 3 assumes that the maximum and minimum temperatures differences for a cross section are representative over the cross section and that the percentage of wet versus dry surface stays constant I from top to bottom. Equation 4 assumes that all evaporated water leaves the annulus as vapor and therefore does not provide any correction for condensation of water vapor prior to exit from the I annulus. The heat losses calculated from the condensate (equation 5) are considered to be the most I reliable since they depend on the least number af assumptions and represent a closed system. These I values are used as the abscissa on Figure 3.3-1. m \3578w.l.non:lb 081898 3-6 Rev.1
FINAt. l 3.3.2.2 Pressure Check l Table 3.3-4 presents a summary of the overall performance of each of the tests described herein. Each test was reviewed by comparing the check pressure calculated from the vessel average inside wall temperature to the measured pressure conditions. 'Ihe check pressure is calculated from the following relationship: Pp = P ,i ( ) + P,,r (6)
8.1 where
l Pp = check Vessel Pressure (psia) P,,i = Initial Pressure of Vessel Internal (psia) T = Average Inside Wall Temperature at Test Conditions ( R) ; T ,i = Average Initial Air Temperature at Stanup (*R) l P,,g = Saturation Pressure of steam at average vessel inside wall temperature (psia) 4 A ratio of the predicted (equation 6) to the measured test pressure less than or equal to unity provides an assurance that there was no large amount of air leakage from the vessel during testing. All tests performed during the baseline tests displayed ratios less than unity and therefore are considered to have maintained their integrity during the test run. 3.3.2.3 Steam Flow Measurement As discussed in Sectiori 2.2.6, three steam flow measurement techniques were utilized during conduct of the majority of the tests reponed herein. Each method has limitations:
=
Condensate measurement is not instantaneous and is only effective during steady state steam flow. The vonex meter's (Channel 244) range is limited. The meter is designed to function from 0.08 to 0.40 volts for flows of 0 to 13 acfs. Actual operation of the meter indicates that the meter's amplifier does not saturate until outputs of 0.633 are attained or 22.5 acfs which limits the maximum measured flow rate below system capacity at very low line pressures (0.94 lb/sec at 2 psig).
. The Gilflo meter is upstream of the bulk of the steam line heaters (see Figure 2.1-1) and is relatively close coupled to the steam boiler. The meter is subjected directly to the pressure fluctuations of the steam boiler which tends to make the indicated flow fluctuate significantly during the test. The meter outputs directly in values proportional to mass flow rate so there is no direct output of the pressure and m:u578w.i.non:itrosis9s 3-7 Rev.1 l
FINAL temperature conditions of the meter during testing. The meter is programmed to adjust it's output for changes in the fluid density from those of the initial calibration setup (2.778 lb/sec at 400 F and 100 psig), but it assumes that the steam quality is 100 percent. Table 3.3-5 presents a comparison of the indicated steam flows for the three measurement techniques under steady state conditions. In general, it appears that the condensate measurement and *he vortex meter measurements agree at steady state within 0.7 percent. The Gilflo measurements are on the average 18 percent lower than the other measurements. Post test calibration of the meters indicated no significant deviation in the performance of the two flow meters. The Gilflo did have a problem with it's internal computer on the handling of the meter's steam line pressure, but the estimated correction was to increase the steam flow by 2.5 percent and the numbers reponed in Table 3.3-5, equation 8 of Section 2 and throughout this report include this adjustment. Based on these observations and the post test calibration of the meter the only consistent conclusion must be that the steam quality at the steam meter is less than 100 percent (at least during steady state operation). Review of the Gilflo during transient periods shows that it generally indicates a higher flow for the first minute or so of the transient (Figure 3.3 2). It is recommended that the vortex meter measurement be used as the actual steam flow unless the amplifier becomes saturated. 3.3.2.4 Internal Velocity Intemal velocity meters provide an indication of the behavior of the condensibles and noncondensibles within the test vessel. Section 2.2.9 describes the meters. The " Pacer" anemometers were of limited utility since they did not provide continuous directional information and provided a limited operational life. The pulse pickup on the " Pacer" tended to become oxidized and thereby reduced the clearance with the anemometer blades and thereby increase the threshold velocity where the meter would operate. The initial effect was observed during pretests where the velocity threshold was estimated to increase to approximately 3 to 5 ft/sec. All the intemally mounted " Pacer's" failed during testing. The only Pacer to survive was the one mounted below the fan assembly. The meter located in the dome of the vessel seemed to provide meaningful outputs for a significantly longer period than the others. This may be due to a lower rate of oxidation of the pickup due to the lower oxygen concentration in the dome of the vessel; the high steam concentration in this area may also have increased the lubrication of the meter's bearings. i The two "H6ntzsch" anemometers survived until the start of high capacity blowdown testing when the meter located at Dome-165 failed due to the anemometer blades becoming deformed. Post test calibration of the remaining anemometer indicated that the less sensitive performance was observed. mA3578*.1.non:Ib-081898 3-8 Rev.1
FINAL The overall behavior of the internal velocity meters is indicated in Table 3.3-6. In general the internal flow path was observed to be down along the wall and up along the wall in the dome area. Available data indicates that both the anemometers located in the dome were in agreement in speed and direction I of the gas movement. i No consistent flow indications were observed from the meter located at E-90'. 3.3.3 Test Summary l Table 3.3-7 presents a summary of the channels that are considered as failed during Phase 2 and Phase 3 testing. Table 3.3-2 presents a summary of all the test runs performed during Phase 2 and Phase 3 of the PCS test program. Test runs identified with an asterisk identify the qualified matrix tests reported herein. In addition, tests identified by "$" contain partially completed tests that did not meet the specific test requirements but do contain useful test data. The reduced data from these tests I is also presented in Appendix D. i l l l l l l I nt\3578w.l.non:lb-o81898 39 Rev. I
FINAL TABLE 3.3-1 I DIFFERENTIAL TEMPERATURE CALIBRATION Location Inside CH Outside CH Delta T Cal DO-180-21 in. CHO CHI -0.015 DO-210-42 in. CH2 CH3 0.283 DO-180-42 in. CH4 CHS -0.573 DO-150-42 in. CH6 CH7 -0.485 DO-210-63 in. CH8 CH9 -0.025 DO-180-63 in. CH10 CHI 1 DO-150-63 in. CH12 CH13 0.110 DO-210-84 in. CH14 CHIS 0.212 DO-180-84 in. CH16 CH17 0.515 DO-150-84 in. CH18 CH19 0.021 DO-120-21 in. CH20 CH21 -0.090 DO-120-42 in. CH22 CH23 0.302 DO 60 42 in. CH24 CH25 -0.435 DO-105-63 in. CH26 CH27 -0.433 DO-90-63 in. CH28 CH29 -0.094 DO-60-63 in. CH30 CH31 0.010 DO-120-84 in. CH32 CH33 0.285 DO-60-84 in. CH34 CH35 DO-0-00 in. CH36 CH37 -0.017 DO-0-21 in. CH38 CH39 -0.015 DO-0-42 in. CH40 CH41 -0.531 DO-30-63 in. CH42 CH43 -0.438 DO-0-63 in. CH44 CH45 -0.067 DO-330-63 in. CH46 CH47 -0.027 DO-0-84 in. CH48 CH49 0.233 DO-210-21 in. CH50 CH51 0.096 DO-300-42 in. CH52 CH53 0.300 DO-240-42 in. CH54 CH55 -0.423 mA3578w-1.non:lb-081898 3-10
FIN u. TABLE 3.31 (cont.) DIFFERENTIAL TEMPERATURE CALIBRATION Location Inside CH Outside CH Delta T Cal DO-300-63 in. CH56 CH57 -0.377 DO-270-63 in. CH58 CH59 -0.115 DO-240-63 in. CH60 CH61 -0.081 DO-300-84 in. CH62 CH63 0.233 DO-240-84 in. CH64 CH65 0.208 A-210 CH80 CH81 -0.121 A-180 CH82 CH83 A-150 CH84 CH85 -0.496 B-180 CH86 CH87 B-150 CH88 CH89 -0.112 C-210 CH90 CH91 0.113 C-180 CH92 CH93 0.235 D-180 CH94 CH95 0.244 D-150 CH96 CH97 0.444 E-180 CH98 CH99 0.063 A-120 CH100 CH101 -0.027 A-90 CH102 CH103 0.269
- A-60 CH104 CH105 -0.487 l
B-120 CH106 CH107 -0.377 B-90 CH108 CH109 -0.035 B-60 CHI 10 CHI 11 0.052 C-120 CHI 12 CHI 13 0.246 C-90 CH1:: CHI 15 0.208 C-60 CH116 ' CHI 17 0.477 D-120 CH118 CH119 0.083 D-60 CH120 CH121 0.035 E-120 CH122 CH123 0.210 E-60 CHI 24 CHI 25 -0.442 m:\3578w.l.non:1b-081898 3-11
~ _ _ _ - _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _
FINAL TABLE 3.3-1 (cont.) ] DIFFERENTIAL TEMPERATURE CALIBRATION Location Inside CH Outside CH Delta T Cal A-0 CH126 CH127 0.010 A-300 CH128 CH129 0.190 B-0 CH130 CH131 -0.381 B-300 CH132 CH133 -0.156 C-0 CH134 CH135 0.035 C-300 CHI 36 CH137 0.060 D-30 CH138 CH139 D-300 CH140 CH141 0.142 E-30 CH142 CH143 0.446 E-300 CHI 44 CHI 45 0.065 A-270 CH146 CHl47 -0.029 A-240 CH148 CH149 0.194 B-270 CH150 CH151 -0.335 B-240 CH152 CH153 -0.308 C-270 CH 1.*4 CHI 55 0.042 C-240 CH156 CH157 0.006 D-240 CH158 CH159 0.198 E-240 CH160 CH161 0.167 F-120 CH162 CH163 -0.021 F-30 CH164 CH165 0.142 F-330 CH166 CH167 -0.438 F-240 CHI 68 CHI 69 -0.413 m:\3578w l.non.lb-081898 3 ]2
FINAt, I l TABLE 3.3-2 SU51 MARY OF PHASE TWO AND THREE TEST RUNS l Test Run No. Test Afatrix No. Comments RC039* 202.3 RC040 203.3 Boiler would not operate properly RC041
- 203.3 Repeat of RC040 RC042% 212.1 Boiler shutdown prior to minimum steady state at final (of three) steam flow rates. Incomplete data on water distribution.
RC043t 213.1 Power outage prior to minimum steady state at final (of three) steam flow rates. Steam flow erratic at final steam flow. RC044* 214.1 RC045* 215.1 RC046* 216.1 1 RC047 Cold helium distribution 1 ' RC048
- 212.1 Repeat of RC042 RC049t 217.1 Two boiler shutdowns prior to helium injection.
Only two sets of noncondensible measurements. RC050* 213 1 Repeat of RC043 RC051$ 217.1 Residual helium concentration in vessel. RC052* 217.1 Repeat of RC051 RC053* 218.1 RC054* 219.1 Vessel pressure too high and insufficient condensible gas sampling prior to start of water cooling. RC055% 221.1 Steady state not achieved after water was turned off. Dorne sampling apparatus failed. f RC056* 221.1 Repeat of RC055 i l RC057
- 219.1 Repeat of RC054 RC058 Rental boiler system checkout RC059 Rental boiler system checkout i RC060 Rental boiler system checkout i
l i l Notes: l
- 1) Not reported herein.
l I 1 mA3578w-1.non:Ib-081898 3.] 3
FINA1. TABLE 3.3 2 (cont.)
SUMMARY
OF PHASE TWO AND THREE TEST RUNS Test Run No. Test Matrix No. Comments RC061
- 222.1 RC062* 220.1 RC063t 222.3 Transient was not recorded on the strip chart recorders with sufficient sensitivity to track the transient.
RC064* 222.3 Repeat of RCM3 RC065* 222.2 RC066* 222.4 RCM7* 224.1 RC068* 224.2 RC069* 223.1 Initial pressure at low flow below atmospheric pressure. Water backing into he test vessel until pressure was raised above ambient. No rapid l data acquisition taken during transient to higher pressures. RC070 223.1 No Data Acquisition. RC069 was acceptable
- Matrix tests.
- Incomplete tests.
m.\3578w.1.non:Ib-08I898 3-14
FINAL TABLE 3.3 3 COMPARISON OF HEAT LOSS ESTIMATES FROM THE PHASE 2 AND PHASE 3 LARGE SCALE TEST SERIES Heat Loss Estimate Run and Test Number Condensate Air / Water Side Wall Heat Flux (mbtu/hr) (mbtu/hr) (mbtu/hr) j RC039-202.3 4.35 5.10 4.72 RCO41-203.3 5.42 5.74 6.11 RCN4A-214.1 4.20 4.40 4.59 t RCN4B-214.1 4.15 4.36 4.64 RCN5A-215.1 3.87 4.32 5.02 RCW5B-215.1 4.17 4.33 4.77 RC046A-216.1 2.25 2.N 2.62 RCN6B-216.1 2.19 2.31 1.83 RC048A-212.1 1.38 1.59 1.69 RCN8B-212.I 2.N 2.56 2.43 l RC048C-212.1 3.I 1 3.33 3.54 RC050A-213.1 1.29 1.43 1.57 l RC050B 213.1 2.05 2.37 2.38 RC050C-213.1 3.05 3.11 2.88 RC052A-217.1 4.14 4.56 4.44 RC052B-217.1 4.08 4.49 4.30 RC053A-218.1 4.17 4.57 4.68 i RC053C-218.1 3.93 4.52 4.69 RC056A-221.1 0.61 0.77 0.75 RC056B-221.1 0.63 0.85 0.76 RC056C-221.1 0.57 0.69 0.42 RC057A-219.1 0.46 0.51 0.33 RC057B-219.1 0.46 0.51 0.32 l RC057C-219.1 0.48 0.66 0.63 l l l mA3578w-1.non:lb-081898 3-15 i _ _ _ _ - _ _ _ - _ _ - - _ _ _ - _ _ _ _ _ _ _ _ _ _ _ - .__ _ _ - _ . _-_ .1
FINAL TADLE 3.3 3 (cont.) COMPARISON OF HEAT LOSS EST151ATES FRO 51 THE PHASE 2 AND PHASE 3 LARGE SCALE TEST SERIES Heat Loss Estimate Run and Test Number Condensate Air / Water Side Wall Heat Flux (mbtu/hr) (mbtu/hr) (mbtu/hr) RCM1 A-222.1 2.34 2.88 2.90 RC064A-222.3 2.81 3.07 4.22 RC064B-222.3 4.77 5.00 6.62 _ RC065A-222.2 2.84 3.20 3.64 RC%5B-222.2 6.05 6.62 7.81 RC066A-222.4 3.45 3.69 4.34 RC066B-222.4 4.44 4.89 6.13 RC067-224.1 1.03 1.19 1.27 RC068-224.2 2.27 2.70 2.52 RC069-223.1 5.63 6.55 3 6.24 Notes: (1) Vortex meter amplifier is saturated. I mA3578w.l.non:1b-081898 3-16 o
l l FINA1. I TABLE 3.3-4 j OVERALL TEST PERFORMANCE Check Test Pressure Air Flow Pressure Ratio Check to l Test Number (psia) (ft/sec) (psia) Measured RC039-202.3 44.55 12.26 27.80 0.62 ; RCN 1-203.3 52.39 13.39 32.48 0.62 i RC044 A-214.1 47.25 7.67 33.21 0.70 1 RC044B-214.1 44.63 14.63 29.27 0.66 RC045A-215.1 48.07 5.40 33.88 0.70 RC045B-215.1 46.00 12.66 30.37 0.66 RC046A-216.1 31.45 12.84 20.46 0.65 RC046B-216.1 49.71 13.71 41.14 0.83 RC048A-212.1 24.91 13.79 17.56 0.70 RCM8B-212.1 30.25 14.31 19.93 0.66 RC048C-212.1 37.54 14.35 23.95 0.64 RC050A-213.1 24.61 14.00 18.70 0.76 RC050B-213.1 29.78 12.36 21.57 0.72 RC050C-213.1 40.94 9.I9 28.66 0.70 RC052A-217.1 42.86 15.16 27.16 0.63 RC052B-217.1 51.29 15.21 28.76 0.56 RC053A-218.1 42.81 15.09 27.23 0.64 RC053B-218.1 50.35 15.22 28.53 0.57 RC056A-221.1 20.37 13.68 16.93 0.83 RC056B-221.1 26.56 13.68 17.09 0.64 RC056C-221.1 63.81 14.77 56.03 0.88 RC057A-219.1 35.80 14.80 35.05 0.98
- 057B-219.1 42.66 14.23 37.68 0.88 RC057C-219.1 23.24 14.45 16.58 0.71 RC061 222.1 33.43 14.61 22.17 0.66 RC064A-222.3 31.42 13.91 19.99 0.64 RC064B-222.3 43.93 13.91 26.99 0.61 mA3578w.l.non
- lt>.081898 3-17
FINAL TABLE 3.3-4 (cont.) OVERALL TEST PERFORMANCE Check Test Pressure Air Flow Pressure Ratio Check to Test Number (psia) (ft/sec) (psia) Measured ' RC065A-222.2 29.31 13.91 24.38 0.83 RCMSB-222.2 44.08 13.91 37.26 0.85 RC066A-222.4 37.45 13.91 27.34 0.73 RC066B-222.4 47.98 13.91 34.74 0.72 RC067-224.1 45.71 13.94 16.70 0.37 RC068-224.2 56.30 13.96 19.13 0.34 RC069-223.1 25.36 13.98 36.55 1.44 Notes: (1) Natural Convection - no velocity measurement taken l 4 m:\3578w.ImortIb-081898 3.I 8 . I _ _ _ _ _ _ . _ --_____________._____._________._______o
i l l FINAL ' l l TABLE 3.3 5 i COMPARISON OF STEAM FLOW MEASUREMENTS Run Number Condensate Vortex Meter Gilflo Meter and Test (ib,/sec) (Ib /sec) (Ib,/sec) RC039-202.3 1.206 1.2 1.06 RCO41-203.3 1.52 1.54 1.38 l RC044A-214.1 1.176 1.14 1.00 RC044B-214.1 1.15 1.14 1.00 1 RC045A-215.1 1.085 1.14 0.99 I RC045B-215.1 1.163 1.15 1.00 RC046A-216.1 0.612 0.6 0.5 RC046B-216.1 0.618 0.61 0.51 ! RC048A-212.1 0.365 0.36 0.25 l l RC0488 212.1 0.551 0.56 0.5 l l l RC048C-212.1 0.854 0.84 0.73 l RC050A-213.1 0.342 0.34 0.27 RC050B-213.1 0.554 0.54 0.49 . l l RC050C-213.1 0.851 0.84 0.72 l RC052A-217.1 1.15 1.14 1.00 i RC052B-217.1 1.135 1.14 0.98 l RC053A-218.1 1.16 1.14 0.99 RC053C-218.1 1.09 1.16 1.00 RC056A-221.1 0.159 0.15 0.1 RC056B-221.1 0.163 0.16 0.11 RC056C-221.1 0.161 0.17 0.12 RC057A-219.1 0.I25 0.I 1 0.07 RC057B-219.1 0.127 0.12 0.08 RC057C-219.1 0.123 0.12 0.08 RC%7-224.1 0.265 0.27 0.21 RC068-224.2 0.606 0.59 0.5 RC%9-223.1 1.26 1.36 1.56 mA3578w.1.non:Ib-08I898 3-19
FINA1. TABLE 3.3-6 SUMA1ARY OF INTERNAL VELOCITY METER PERFORMANCE Test Run Test Matrix Pacer Pacer Pacer Huntzsch H5ntzsch No. No. E 90 D-180 Dome-345 A-90 Dome-165 RCO39* 202.3 No Functional Output No consistent - consistent - No Functional up down Functional Output Output RC040 203.3 RC041* 203.3 No Functional Output No No consistent - No Functional Functional down Functional Output Output Output RC042* 212.1 RC043* 213.1 RC044* 214.1 No Functional Output iI to 11.2 magnitude consistent - magnitude high value consistent down consistent 27.7 with do-165 with do-345 carly only early only RC045* 215.1 No Functional Output No No consistent - early Functional Functional down positive Output Output response RC046* 216.1 No Functional Output No No consistent - early Functional Functional down positive Output Output response RC047 l RC048* 212.1 No Functional Output No magnitude consistent - magnitude l Functional consistent down consistent l Output with do 165 with do-345 RC049$ 217.1 RC050* 213.1 No Functional Output No No consistent - early Functional Functional down positive Output Output response RC051* 217.1 RC052* 217.1 No Functional Output No No consistent - early Functional Functional down positive Output Output response RC053* 218.1 No Functional Output wild No consistent - early swings Functional down positive throughout Output response test more intensive after He addition RC054* 219.1 RC055t 221.1 m:\3578w-1.non:Ib.081898 3-20 Rev.1
l FINAL I TABLE 3.3-6 (cont.)
SUMMARY
OF INTERNAL VELOCITY METER PERFORMANCE Test Run Test Matrix Pacer Pacer Pacer Huntzsch Huntzsch No. No. E-90 D 180 Dome-345 A-90 Dome 165 RC056* 221.1 No Functional Output No activity on No early t Functional He addition Functional positive l Output and on Output response l l stoppage of I water I cooling j l RC057* 219.1 No Functional Output No No consistent - early i Functional functional down positive l Output Output response j l RC058 RC059 RC060 RC061* 222.1 No Functional Output No No consistent - No Functional Functional down Functional Output Output Output l RC062* 220.1 No Functional Output No consistent - consistent - No I I Functional up down Functional 1 Gutput Output RC063t 222.3 RC064* 222.3 No Functional Output No No consistent - No Functional Functional down Functional Output Output Output RC065* 222.2 No Functional Output No No consistent - No Functional Functional down Functional Output Output Output , RC066* 222.4 No Functional Output No No consistent - No Functional Functional down Functional Output Output Output RC067* 224.1 No Functional Output No No No No Functional Functional Functional Functional Output Output Output Output RC068* 224.2 No Functional Output No No No No Functional Functional Functional Functional Output Output Output Output RC069* 223.1 No Functional Output No No No No Functional Functional Functional Functional Output Output Output Output RC070 223.1 m:\3578w 1.non:lM81898 3-21 Rev.I
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FrNAL l l i 4.0 TEST RESULTS This section contain a summary of each of the completed matrix tests considered acceptable. Each of the following sections presents: e description of the test performed a plots of the steam flow rate e plots of the vessel pressure
.e plots of the noncondensible concentrations (when available) summary tables of the average of the steady state condition of the test vessel l
summary tables of the average, maximum and minimum vessel temperatures and (L differential temperatures during the steady state periods. I Electronic files of the test data are contained in Appendix D. 4.1 Test Results 202 3 Test 202.3 was a constant pressure test designed to repeat the previous tests performed in the Baseline ! t Tests 202.1 and 202.2. The test featured an insulated vessel bottom, short term internal heat sinks and a steam generator volume located over the steam discharge nozzle. Additionalinstrumentation was 1 l added which includes: j e steam flow meter
- l. -e thermocouple rake e internal velocity meters e annulus differential pressure cell e fixed annulus exit velocity meter. ;
The test was conducted by establishing a steam flow sufficient to achieve the required vessel test
. pressure (approximately 30 psig) with the air cooling fan at 530 RPM and water cooling to the vessel at a 75 percent water coverage level. The test continued until the vessel pressure was constant within 0.5 psi for a minimum of a half hour. The extent of water coverage on the vessel was measured l during the study state period of the test.
! ~ A history of the vessel pressure and steam flow are shown in Figure 4.1-1. The steady state period is
- defined from 13.006 to 13.856 hours and the steady state behavior is tabulated in Table 4.1-1 and Table 4.1-2. Table 4.1-2 presents a comparison of the average, minimum and maximum temperatures on the inside and outside vessel walls at each cross section of the vessel. Also included are the maximum, minimum and average differential temperatures for the same cross sections.
The exit air anemometer failed during the conduct of Test 202.3. Velocity values from the calibration of the exit fan were used to estimate the resulting air flow at 530 RPM. This is an acceptable muS7s. 2.non:itwsis9s 41 Rev.1
FINAL accommodation since the exit velocity meter mainly provides an indication of the variation of the velocity through the annulus. Performance is confirmed throughout the test by the differential pressure cell located below the fan and by verification of fan RPM late in the test. The H6ntzsch anemometers were located at Dome-42"-165*-1.5" and A-90 -1.5". The H6ntzsch anemometer located in the dome of the vessel provided outputs during the initial transient but provided no outputs above its velocity thres'r.old during the steady state period whereas, the meter at A-90*-1.5" provided outputs that indicated that the velocities down along the sidewall while at steady state. Limited outputs were also available from 1e Pacer anemometers (Dome-42"-345*-1.5", D-180*-2" and E 30*-2"), but only the anemometer at Dome-42"-345*-1.5" provided outputs above the sensor threshold and sufficient enough to determine the direction as upward in the same manner as the H6ntzsch anemometer at Dome-42"-165*-1.5", Table 4.1-3 contains a summary of the indicated flows for the velocity sensors and Figure 4.1-2 shows a history of their performance over the entire test. The negative values for the H6ntzsch meter indicate downward flow. Condensation collection during the steady state portion of the test was performed with the condensate collection to tank 1 (small tank) from the open and closed area in the heel of the test vessel and the remainder to condensate collection tank 2 (large tank). Water distribution around the circumference at the bottom of the bsfile was taken after steady state was established at 1325 hours. The distribution of dry stripes around the circumference total to a 89 percent water coverage witn an average width of 3.1 in. Figures 4.1-3 and 4.1-4 provide an indication of the average temperature history of the inside wall of the test vessel and the fluid adjacent to the vessel wall as a function of elevation throughout the test. m:\3578w-2.non:1t481898 42 1
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FINAL l t _ Ac TABLE 4.1-1 TEST 202.3
SUMMARY
DATA RUN RC039 AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES , INTERNAL INSIDE I INSIDE OUTSIDE FLUID WALL AT BAFFLE (*F) ('F) (*F) (*F) ( F) i l l J l l m:\3578w-2.non.lb481898 47 l
FINAL 1,C TABLE 4.1 1 (cont.) TEST 202.3
SUMMARY
DATA RUN RC039 AVERAGE TEST DATA , 2-= l ' _ . , .i l mus78w.2.non:1b-osis9s 4-8
l FINAL _ a,C TABLE 4.12 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 202.3 AVERAGE WALL MAXIMUM WALL MINIMUM WALL TEMPERATURE TEMPERATURE TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION F F F F F F F F F l l I m:\3578w-2.non:Ib-081898 49 L----__ . _ _ _ - - - _ _ - - _ _ _ _ _
FINAL a,c TABLE 4.13 I TEST 202.3, RUN RC039, INTERNAL VELOCITY TEST DATA STANDARD AVERAGE MAXIMUM MINISIUM DEVIATION LOCATION (fusec) (fusec) (fusec) (fusec) NOTES i l I 1 l m:\3578w-2.non:Ib481898 4 10
l FINrt. l i i 4.2 Test Results 203.3 l l l Test 203.3 was a constant pressure test designed to repeat the previous tests performed in the Baseline Test series 203.1 and 203.2. The test featured an insulated vessel bottom, short term intemal heat l sinks and a steam generator volume located over the steam discharge nozzle. Additional I instrumentation was added which includes: a steam flow meter e thermocouple rake e internal velocity meters e annulus differential pressure cell
- fixed annulus exit velocity meter.
A history of the vessel pressure and steam flow throughout the test are shown in Figure 4.2-1. The steady state period is defined from 11.615 hours to 12.590 and the steady state results for 203.3 are tabulated in Table 4.21 and Table 4.2-2. Table 4.2-2 presents a comparison of the average, minimum i and maximum temperatures on the inside and outside vessel walls at each cross section of the vessel. Also included are the maximum, minimum and average differential temperatures for the same elevations. The data presented is representative of approximately one hour of test operation; plots of the pressure and steam flow (vortex meter) are shown in Figure 4.2-1. Internal velocity meters were located in five internal locations in the test vessel as indicated in Table 4.2-3. The H6ntzsch anemometer (A-90*-1.5") provided outputs that indicated that the veloc. ties were down along the sidewall. All other velocity meter outputs were too low during steady state operation to evaluate the outputs. Figure 4.2-2 shows the history of the H6ntzsch meters throughout the test. The H6ntzsch anemometer located in the dome (Dome-42"-165*-1.5") initially provided both up and down velocities but produced no velocity indications during the steady state period. Water distribution around the circumference at the bottom of the baffle was taken after steady state was established at 1340 hours. The distribution of dry stripes around the circumference that total to a 86 percent water coverage with an average width of 3.5 in. l Condensation collection during the steady state portion of the test was performed with the condensate l collection to tank 1 (small) from the open and closed area in the bottom of the test vessel and the remainder to condensate collection tank 2 (large). Figures 4.2-3 and 4.2-4 provide an indication of the temperature distribution on the inside wall of the test vessel and of the inside fluid temperature approximately 1 inch away from the wall as a function of elevation. l nr\3578w.2.non:Ib-081898 4-11
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i FINAL a,c TABLE 4.21 TEST 203.3
SUMMARY
DATA RUN RC041 AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE OUTSIDE FLUID WALL AT BAFFLE INSIDE ('F) ('F) ('F) ('F) ('F)
~
m:\3578w 2.non.lb.081898 4.]6
FINAL l a,c TABLE 4.2-1 (cont.) TEST 203.3
SUMMARY
DATA I RUN RC041 AVERAGE TEST DATI l i l t l l l i l I 1 i L i l l J l l i l ! I ! m\3578w 2.non:Ib-081898 4-17 i
FINAL a,c i TABLE 4.2 2 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 203.3 l AVERAGE WALL MAXIMUM WALL MINIMUM WALL TEMPERATURE TEMPERATURE TEMPERATURE INSIDE OUTSIDE DELTA LNSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) 1 m:\3578w 2.non:lb 081898 4. ] g
FINAL j ( l 1 _ a,C l TABLE 4.2 3 TEST 203.3 RUN RC041, INTERNAL VELOCITY TEST DATA STANDARD l AVERAGE MAXIMUM MINIMUM DEVIATION LOCATION (ft/sec) (ft/sec) (ft/sec) (ft/sec) NOTES 4 l 1 i l I m:\3578*-2.non:lb-081898 4-19 l t L________-__-_____-__ _ - - _ - . _ - - . _ . - _ _ _ - - - - - - . - - - - - - - - - - - -
FmAL 4.3 Test 212.1 Test 212.1 was a constant flow test conducted by establishing a steam flow at a constant rate and maintaining the flow until the vessel arrived at a constant pressure with the air cooling fan on at 530 RPM, with water cooling to the vessel maintained at a predetermined uniformly distributed water coverage. After the vessel reached a constant pressure the steam flow was increased and maintained until the vessel again reached a steady pressure. Again after the vessel reached a constant pressure the I steam flow was increased to a third level and was allowed to come to a steady pressure. The extent of water coverage on the vessel was measured during each steady state period. The steady state results for Tests 212.1 for each of the three flow levels are tabulated in Tables 4.3-1 through 4.3-6 and are representative of the average performance during approximately one hour of test operation. The tables are identified by the test mn number "RC048" followed by an alpha suffix "A,"
"B" or "C" to indicate the intended steam flow rate of 0.25,0.5 and 0.75 lbm/sec, respectively. The steady state times are defined as 8.722 to 10.307 hours for "A",11.121 to 12.096 hours for "B," and 13.214 to 14.289 hours for "C " Tables 4.3-4 through 4.3-6 present a comparison of the average, minimum and maximum temperatures on the inside and outside vessel walls at each cross section of the vessel for each of the steam flow conditions. Also included are the maximum, minimum and average differential temperatures for the same elevations. The plots of the pressure and steam flow (vonex meter) are shown in Figure 4.3-1. The results of the non-condensible sampling are shown on Figure 4.3-2 at the two sampling locations (Dome-90 -63"-3" and F-0 -6"). The data shows that the air tends to concentrate below the operating deck level.
Intemal velocity meters were located in five internal locations in the test vessel as indicated in Table 4.3-7. The II6ntzsch anemometers (Dome-42"-165*-1.5" and A-90*-1.5") provided outputs that indicated that the velocities were generally upward, parallel to the dome wall, i.e. toward the center in the vessel dome and toward the center in the vessel dome and down along the sidewall while at steady I state. The pacer at Dome-42"-345*-1.5" provided data of a magnitude consistent with the dome
! H6ntzsch. The remaining pacer units either failed or had velocities below the current sensor threshold.
Table 4.3-7 contains a summary of the indicated flows for the velocity sensors for the entire test run. I Figure 4.3-3 presents the history of the anemometers for the test. Condensation collection during the steady state ponion of the test was performed with the condensate collection to tank i from the open and closed area in the bottom of the test vessel and the remainder to condensate collection tank 2. Water distribution around the circumference at the bottom of the baffle was taken during each steady state portion of the test. During the two lower steam flow portions of the test the water distribution was measured at 100 percent; coverage reduced to 95.3 percent during the 0.75 lb/see ponion of the test at 13.75 hours. The distribution of dry strips around the circumference had an average width of 2.5 in. muS78w.2.non:ib osis9s 4-20 Rev.!
FINAL
- Figures 4.3-4 and 4.3-5 provide an indication of the temperature distribution on the inside wall of the test vessel and of the inside fluid temperature approximately 1 in, away from the wall as a function of elevation.
! i l i i i I l 1 i l l l m:us7sw 2.non:t><> sis 9s 4-21 l
FINAL
- a,c
~
l I I I U M s a A .\ d N W D H h
.1 a:
k io E ' 1 E i> i M v E
.5$
w m:0578w-2.non:Ib-081898 4,37
' FINA1, t.
t l
- _ a,c i ..
l l N s s a el - N E B u 1 ' E 0 l
- 1 L Z i
N i l 4 i ! E i l l mos7s--2.non:ib.osis9s 4-23 Rev.I
FINAL _ Ac at E z J d N I" fI i 1e 3 m 4 2 h mA357:w-2.non:ibast:9s 4-24 Rev.1
FINAL a,C f I. U M s s K 1 . I e4 M H l-i ' c I 2 K E 1 b
- =
es N l> e 1 t 1 i n n 8
.E h
mV578w-2.non:Ib-081898 4-25
FINAL
~
Ac ) l N E u 4 e4 M i b i c > e a a am E F 3 E 1 an E v E
.5 m:0578w-2.nortiWI898 4,gg
FINAL _ a,e TABLE 4.31 TEST 212.1
SUMMARY
DATA RUN RC048A AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE ' INSIDE OUTSIDE FLUID WALL AT BAFFLE ('F) (*F) ('F) ('F) ('F) i l i l m:uS7sw-2.non: basis 98 4-27 Rev.1 1 1
FmAL a,c TABLE 4.3-1 (cont.) TEST 212.1
SUMMARY
DATA RUN RC048A AVERAGE TEST DATA l l mA3578w-2.non:Ib481898 4-28
l FINAL _ a,c TABLE 4.3 2 l TEST 212.1
SUMMARY
DATA RUN RC048B AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES i INTERNAL INSIDE l INSIDE OUTSIDE FLUID WALL AT BAFFLE ('F) ('F) (*F) ('F) ('F) I i l l l l l m:\3578w 2.non:Ib-08I898 4 29 L . .
FtNAL a,c TABLE 4.3-2 (cont.) TEST 212.1
SUMMARY
DATA RUN RC048B AVERAGE TEST DATA
)
I m:\3578w 2mn:IbO81898 4 30 l I _- _ _ _ ______________________--____--_---____E
FtNAt. { _ a,c TABLE 4.3-3 TEST 212.1
SUMMARY
DATA RUN RC048C AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE ('F) ('F) ('F) ('F) (*F) l
\
I I l mA3578w-2.non:Ib41898 4-31
FINAL t
- a,c l
TABLE 4.3 3 (cont.) TEST 212.1
SUMMARY
DATA RUN RC048C AVERAGE TEST DATA l l l m:u57s. 2.non:t b.os1898 4-32 Rev.1
)
l l l i FINAL i I a,e l _ l l TABLE 4.3 4 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 212.1, RUN RC048A AVERAGE WALL MAXIMUM WALL MINIMUM WALL TEMPERATURE TEMPERATUR E TEMPERATURE , INSIDE OUTSIDE DELTA INSIDE OUTFIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) < i l l l l 1 1 1 l i I 1 { i I i l I I l m:\3578w-2.non:lt481898 4-33
FINAL _ 3,C TABLE 4.3-5 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 212.1, RC048B AVERAGE WALL MAXIMUM WALL MLNDfUM WALL TEMPERATURE TEMPERATURE TEMPERATURE LNSIDE OUTSIDE DELTA LNSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) (*D ('D ('D (*F) (*F) (*F) (*F) (*F) 1 mA3578w 2.non:Ib-08tB98 4-34 i
l l l FINAL 1 I l I _ ac TABLE 4.3-6 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 212.1, RC048C I l l AVERAGE WALL MAXIMUM WALL MINIMUM WALL ' i TEMPERATURE TEMPERATURE TEMPERATURE 1 l ' INSIDE OUTSIDE DELTA LNSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) (*F) (*F) t*F) (*F) (*F) (*F) (*F) (*F) l l l I l I mt1578w 2.non:lb-081898 4-35
FINAL Ac f _ TABLE 4.3-7 TEST 212.1 RUN RC048, INTERNAL VELOCITY TEST DATA STASVARD AVERAGE MAXIMUM MINIMUM DEVIATION (ft/sec) (fusec) (ft/sec) NOTES LOCATION (ft/sec) 1 l l 1 m:\3578w.2.non:Ib-081898 4-36 I
FINAL. l l 4.4 Test Results 213.1 Test 213.1 was a constant flow test conducted by establishing a steam flow at a constant rate and maintaining the flow until the vessel arrived at a constant pressure with the air cooling fan on at 530 RPM with water cooling about 50 percent less than that employed in Test 212.1 to the vessel maintained at a predetermined uniformly distributed water coverage. After the vessel reached a constant pressure the steam flow was increased and maintained until the vessel again reached a steady l pressure. Again after the vessel reached a constant pressure the steam flow was increased to a third level and was allow to come to a steady pressure. The extent of water coverage on the vessel was j measured during each steady state period. l The steady state results for test 213.1 for each of the three flow levels are tabulated in Tatus 4.4-1 through 4.4-6 and are representative the average performance during approximately one hour of test l operation. Tables 4.4-4 through 4.4-6 present a comparison of the average, minimum and maximum temperatures on the inside and outside vessel walls at each cross section of the vessel for each of the steam flow conditions. The tables are identified by the test run number "RC050" followed by an alpha suffix "A," "B" or "C" to indicate the intended steam flow level of 0.25,0.5 and 0.75 lbm/sec, l respectively. The steady state times are defined as: 8.519 to 9.539 hours for "A," 9.950 to 10.871 ! hours for "B," and 12.280 to 13.030 hours for "C." Plots of the pressure and steam flow (vortex l meter) are shown in Figure 4.4-1. As noted on Table 4.4-3, the outlet velocity of the annulus air is low when compared to the other air velocities reported herein. The only significant variation from the other portions of the test was the I increase in the water evaporated into the annulus. Review of previous tests would indicate a minimal impact on the air velocity at constant fan speed of 530 rpm. It is recommended that a nominal value of 13.9 ft/sec be used for the exit air velocity based on the fan calibration value at 530 rpm and the maintenance of an annulus AP of 0.11 in. H2 0. The results of the non-condensible sampling are shown on Figure 4.2 2 at the two sampling locations l (Dome-90*-63"-3" and F-0*-6'). The data shows that the air tends to concentrate below the operating l deck level. l l Intemal velocity meters were located in five internal locations in the test vessel as indicated in Table 4.4-7. The H6ntzsch anemometers (Dome-42"-165"-1.5" and A-90*-1.5") provided outputs that
- indicated that the velocities were generally up and toward the center in the vessel dome and down j along the sidewall. No useable outputs were available from the Pacer anemometers. All these units l have either failed or velocities below the current sensor threshold. Table 4.4-7 contains a summary of the indicated flows for the ve!ocity sensors for the entire test run. Plots of the performance of the I anemometers during the test performance are shown in Figure 4.4.3.
mus78w.2.non:t b-081898 4-37 Rev.I
FINAL
?
Water distribution around the circumference at the bottom of the baffle was taken after steady state was established at each of the required flow rates. Table 4.4-8 summarizes the water distribution around the circumference of the vessel at each of the steady state. Condensation collection during the steady state portion of the test was performed with the condensate collection to tank I from the heel of the test vessel and the remainder to condensate collection tank 2. Figures 4.4-4 and 4.4-5 provide an indication of the temperature distribution on the inside wall of the test vessel and of the inside fluid temperature approximately 1 in. away from the wall as a function of elevation. mA3578w.2.non Ib-o81898 4-38
FINAt. I a,c I' r R. U M 1 a 3 M J d. e4 e
.I.
.E lll 5
k E l e 5
@ l 3a I
A 7 M 9 0 m oc IE. l 1 m:\3578w-2.non:lb-081898 4 39
FLNAL a,C i l 1 R 8 g } E a N b E E M I i E a o 1 Z N Y T n is. m.\3578w-2.non:lt481898 4-40
FINAL a,C I l l l l l l-I i R o-O M s s M d N h t b ia
- It !
i s E i s E b
> 4 9
9 ? I i I f- 3
.Y h
l m:\3578w-2.non:Ib481898 44}
. _ _ _ _ - . . . .-_____ _=-_. ______ _ _-___-_____ _ -__ ____- _ _ -
FINAL l
~
2,C E S
=
E a 5 O N b b h 8. b i k l 2 4 N t.$8 an:0578E-2.non:lW1393 4-42
FINAL a,C I f e. O M s 8 [ M J J d N ! b P i E a e b 2 E m 4 4 0 m es E m-0578w-2.non:!b-081898 4-43 t
FINAL a,c j TABLE 4.41 TEST 213.1
SUMMARY
DATA RUN RC050A AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT SAFFLE ('F) ('F) ('F) ('F) (*F)
.I m:0578w 2.non:Ib481898 4 44
FINAL i ( ac f i TABLE 4.41 (cont.) l TEST 213.1
SUMMARY
DATA RUN RC050A AVERAGE TEST DATA { l I l r 1 I l I I i l I m.\3578w-2.non:lt>-081898 4-45
FLNAL u j - ! TABLE 4.4 2 TEST 213.1
SUMMARY
DATA RUN RC050B AVERAGE TEST DATA WALL TEh1PERATURES TESIPERATURES LNTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE ('F) ('F) (*F) ('F) ('F) B 1 I l
]
l i m:uS78w 2.nowlb-os2098 4-46 Rev.2
)
FINAL _ a,e l TABLE 4.4-2 (cont.) TEST 213.1
SUMMARY
DATA RUN RC050B AVERAGE TEST DATA l ? m:u578w-2.non:Ib.os2098 4 47 Rev.2
FINAt. f t 1 a,c TABLE 4.4-3 TEST 213.1
SUMMARY
DATA RUN RC050C AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE ('F) ('F) ('F) ('F) (*F)
~ _
m\3578w-2.non:Ib-08I898 4 4g
i l FINAL l
- _ a,c TABLE 4.4-3 (cont.)
TEST 213.1
SUMMARY
DATA RUN RC050C AVERA 3E TEST DATA m:\3578w-2.non:lb-081898 4-49
FINAL a,c i TABLE 4.4 4 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 213.1, RC050A AVERAGE WALL MAXIMUM WALL MINIMUM WALL TEMPERATURE TEMPERATURE TEMPERATURE DELT
' UTSIDE DELTA INSIDE OUTSIDE A INSIDE OUTSIDE DELTA INSIDE ,
(*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) LOCATION (*F) a. m:\3578w 2.non:lb481898 4-50
r l l t INAL a.c TABLE 4.4-5 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 213.1, RC050B AVERAGE WALL MAXIMUM WALL MINIMUM WALL TEMPERATURE TEMPERATURE TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) l l I nt\3578w.2.non:Ib-081898 4-51
FINAI. a,c l l TABLE 4.4-6 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 213.1 RC050C AVERAGE WALL MAXIMUM WALL MINIMLSI WALL TEMPERATURE TEMPERATURE TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) m'\3578w 2.non:lb-0818*9 4 52
l FINAL
- _ a,c TABLE 4.4-7 TEST 213.3 RUN RC050, INTERNAL VELOCITY TEST DATA STANDARD AVERAGE MAXIMUM MINLMUM DEVIATION LOCATION (fusec) (ft/sec) (ft/sec) (ft/sec) NOTES l
l l l I l nt\3578w 2.non.Ib-081898 4 53 l
FINAL I l a,e TABLE 4.4-8 TEST 213.1, RUN RC050, DISTRIBUTION OF DRY STRIPS I STEAM FLOW WET AVERAGE DRY WIDTH (Ib/sec) (%) (in) l l l l 1 l l l l mA3578w 2.non:Ib-081898 4-54
l FINA1, 4.5 Test 214.1 Test 214.1 is a constant steam flow test featuring an air flow transient between natural convection air flow and a fan speed of 530 RPM. The steam flow was set at a constant rate of approximately I lbm/see while maintaining the flow until the vessel arrived at a constant pressure with the air cooling fan off and water cooling to the vessel set at a predetermined level. After the vessel reached a 1 constant pressure the fan is turned on to 530 rpm and maintained until the vessel again reached a steady pressure. 'Ihe extent of water coverage on the vessel was measured during each of the steady state periods. l The steady state results for Test 214.1 for each of the two air flow levels are tabulated in Tables 4.5-1 through 4.5-4 and are representative of approximately one hour of test operation. The tables are identified by the test run number "RC044" followed by an alpha suffix "A" or "B" to indicate the intended air flow of natural or forced convection, respectively. The steady state times are defined as 10.750 to 11.751 hours for "A" and 13.265 to 14.265 for "B." Tables 4.5-3 and 4.5-4 present a comparison of the average, minimum and maximum temperatures on the inside and outside vessel walls at each cross section of the vessel for each of the air flow conditions. Plots of the pressure and steam flow (vortex meter) are shown in Figure 4.5-1. Internal velocity meters were located in five internal locations in the test vessel as indicated in Table 4.5-5. The H6ntzsch anemometers (Dome-42"-165"-1.5" and A-90*-1.5") provided outputs that indicated that the velocities were generally up and toward the center in the vessel dome and down along the sidewall while at steady state. All the Pacer anemometers functioned satisfactorily during this test. The anemometer located at D-180* provided outputs in the range of 20 ft/see over a 20 minute period during the initial phase of natural convection testing where there was no contributing behavior observed. No directional information was available from the Pacer anemometers. Table 4.5-5 contains a summary of the response for the velocity sensors for the entire test run. Plots of the behavior of the internal velocity meters is shown in Figure 4.5-2. Condensation collection during the steady state portion of the test was performed with the condensate collection to tank I from the heel (open and closed areas) of the test vessel and the remainder to condensate collection tank 2. Water distribution around the circumference at the bottom of the baffle was taken after steady state was established at each of the required flow rates. Table 4.5-6 summarizes the water distribution around the circumference of the vessel at each of the steady state conditions. Figures 4.5-3 and 4.5-4 provide an indication of the average temperature distribution on the inside wall of the test vessel and of the average inside fluid temperature approximately 1 in. away from the wall as a function of elevation, mA3578w-2.non:lb-081898 4-55
I
!1 1liiiI u
?z t' l
I Po 4 4 0 C _ R - n u R 1 4 1 2 t s e T y _ r t o i s H w l o F m a t e S d n a e r u s s e r P l e s s e V 1 5 4 e r u g i F I l
?M R&34h5ak1&
FLNA1, i a,C j 1 I l i l l l l l l I I V M e 3 Df. 4 m N b b n. c
. 5
=
c
.5 e
a E s i i
.a.e N.
9 j w o. 6 > 3 N b
~ m.11578w-2.non:1b-081898 4 57
FINAL a,C i Q M E u 5 2 N t 1 2 k 1
~
9 Y e mM578w 2.non:lb-081898 4,$g
l l FINAL l l l a,C l t l l i I t 1 l l i i l-t E s s E 4 i i N b h L l E l F i 3 ? , i< trl ! 0 1 l l 1 I I I i i l l l i 1 i nt\3578w-2.non:Ib41898 4-59 l
}
l FINAL I a.c T:ble 4.5-1 TEST 214.1
SUMMARY
DATA RUN RC044A AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE (*F) ('F) ('F) (*F) ('F) l
)
i i mM578w-2.non:lt>081898 4,69 b
FINAL I
._. _ a,c
! Table 4.51 (cont.) l TEST 214.1
SUMMARY
DATA RUN RC044A AVERAGE TEST DATA l l m:0578w-2.non:Ib 081898 4-61
l l l j FINAL a,c Table 4 *-2 TEST 214.1
SUMMARY
DATA RUN RC0448 AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL WALL INSIDE INSIDE OUTSIDE FLUID AT BAFFLE ('F) ('F) ('F) ('F) (*F) m:\3578w.2.non.lb-081898 4 62
I FINAL 1
- _ a,c Table 4.5 2 (cont.)
TEST 214.1
SUMMARY
DATA RUN RC044B AVERAGE TEST DATA l j mM578w.2.non:lb-081898 .$.63 L_____.________ _ _ . _ _ _ . . . _ . _ _
FINAL _ 3.C TABLE 4.5.3 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 214.1, RC044A AVERAGE WALL MAXIMUM WALL MINLMUM WALL TEMPERATURE TEMPERATURE TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION FF) PF) CF) (*F) (*F) (*F) (*F) (*F) (*F) m:\3578w 2.non.lb-081898 4 64
l FINAL a.c TABLE 4.5-4 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 214.1, RC044B l l AVERAGE WALL MAXIMUM WALL MINLMUM WALL TEMPERATURE TEMPERATURE TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELT INSIDE OUTSIDE DELTA (*F) ('F) (*F) (*F) ('F) A (*F) ('F) (*F) OCATION ! (*F) l l { i I l l l 4 1 i l l ~ i l \ l 1 i l l l l l l m \3578w-2.non:!b-081898 4-65 u_________________________._____________._____.___...
l lll1 1 , ;IlllI 5? l I S E T O N A T A D T S E T Y DN T RO ) I C AI T c e O D NIA u s L E AV f ( V TE SD 5 L A 5 4 N R M U ) e E c l M e ba T I N us r T N I I ( 4
, M 4
0 C M R U ) c N M e s U I X v r R A ( 1 M 4 1 2 E T G ) c S A e E R s T E u f V ( A N O I T A C O L I l aG5ei5t _b! ' 8 i NE '
FINAL _ a,c TABLE 4.5-6 TEST 214.1, RUN RC044, DISTRIBUTION OF DRY STRIPS l l AIR FLOW WET AVERAGE DRY WIDTH (%) (IN) l l i l l l l i l l i l i mM578w-2a.non:!b-081898 4-67
I FINAL I 1 4.6 Test 215.1 1 Test 215.1 is a constant steam flow test featuring an air flow transient between natural convection air flow and a fan speed of 530 RPM with a baffle installed at the bottom of the air annulus from 90' through 270* to restrict air flow into the annulus at this point. The steam flow was set at a constant rate of approximately I lb/sec until the vessel arrived at a constant pressure with the air cooling fan off and water cooling to the vessel set at a predetermined level. After the vessel reaches a constant pressure the fan is turned on to 530 rpm and maintained until the vessel again reaches a ster.dy i pressure. The extent of water coverage on the vessel was measured during each of the steady state periods. The steady state results for 215.1 for each of the two air flow levels are tabulated in Tables 4.6-1 through 4.6-4 and are representative of approximately one hour of test operation.. The tables are identified by the test run number "RC045" followed by a alpha suffix "A" or "B" to indicate the air flow level for natural and forced convection, respectively. The steady state times are defined as 11.624 to 12.6211 for "A" and 13.293 to 14.293 for "B." Tables 4.6-3 and 4.6-4 present a comparison l of the average, minimum and maximum temperatures on the inside and outside vessel walls at each cross section of the vessel for each of the air flow conditions. Plots of the pressure and steam flow (vortex meter) are shown in Figure 4.6-1. A shutdown of the steam supply system occurred at approximately 11.15 hours while test 215.1 was achieving the initial steady state conditions. The steam supply system was restarted and the system was brought to steady state as defined in the test procedure prior to activation of the annulus air fan. The data system and sensors continued to document the event and the test control settings were i undisturbed during this excursion. This test was considered acceptable since the recovery was well documented and steady state was achieved prior to the continuation of the test. Intemal velocity meters were located in five internal locations in the test vessel as indicated in Table 4.6-5. The H6ntzsch anemometers (Dome-42"-165'-1.5" and A-90 -1.5") provided outputs that indicated that the velocities were generally up and toward the center in the vessel dome and down along the sidewall. No useable outputs were available from the Pacer anemometers. All these units have either failed or velocities below the current sensor threshold. Table 4.6-5 contains a summary of the time dependent response of the indicated flows for the velocity sensors for the entire test run. Plots of the behavior of the internal velocity meters is shown in Figure 4.6-2. Condensation collection during the steady state portion of the test was performed with the condensate collection to tank i from the heel of the test vessel and the remainder to condensate collection tank 2. l Water distribution around the circumference at the bottom of the baffle was tr. ken after steady state was established at each of the required flow rates. Table 4.2-6 summarizes the water distribution around the circumference of the vessel at each of the steady state. Figures 4.6-3 and 4.6-4 provide an indication of the average temperature distribution as a function of level for the inside vessel wall and the fluid temperature approxirr.ately 1 in. inside the vessel, mN1578w-2a.non:lb-081898 4-68
7. i [ l' FINAL i ,
~
a,c . i i m M e a M J wi N 5 , s :' x l $ l
.1 i m !
k k E a 3 m 1e. 8 s i>
~
4 4 8 s
.!L8 A
i l l m:\3578w-2a.non:lb-081898 4-69
FmAL .
~l a,C l
l l en M s s
. M i
e N vt a i s I e 2
.5
$e a
E e b n 4 4 E E m:\3578w-2a,non:1b-081898 4 70
l Fmrt a.C an E U M e s N J vi N 5' H d a 3 E e H , a N o l > r o 3m
~
7 w 4 E s I
.Y b
i l' I l. F m:\3578w-2a non:lt-081898 4 71 i - l
FINAL a,c m b U M c s E vi 5 O E-Y s k E. E 5 s E 7w 4 8 s
.F En.
MMS 78w-2a.non:lb-081898 4-72
FINAL l i l
- _ a,c l TABLE 4.61 TEST 215.1
SUMMARY
DATA RUN RC045A AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE
- INSIDE OUTSIDE FLUID WALL AT BAFFLE i ('F) ('F) ('F) ('F) ('F) 1 -. _
m:\3578w-2a.non:]b-081898 4-73 l l
--___ __ _____________________ - . _ _ - . - - - - _ _ _ _ _ _ __ 1
FINAL _ a.c TABLE 4.61 (cont.) TEST 215.1
SUMMARY
DATA RUN RC045A AVERAGE TEST DATA mA3578w-2a.non:lt481898 4-74 Rev.1 J
FINAL l I a,c TABLE 4.6 2 ! TEST 215.1
SUMMARY
DATA RUN RC045B AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE l INSIDE OUTSIDE FLUID WALL AT BAFFLE (*F) ('F) (*F) ('F) (*F) l l l l l l l
~ h m:\3578w-2a.non:lb-081898 4 75 Rev.I
FINAL _ a.c TABLE 4.6 2 (cont.) TEST 215.1
SUMMARY
DATA RUN RC045B AVERAGE TEST DATA I m:\3578w 2 anon.Ib-081898 4 76 Rev.1
)
FINAL _ a,C TABLE 4.6-3 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 215.1, RC045A AVERAGE WALL MAXIMUM WALL TEMPERATURE TEMPERATURE MINIMUM WALL TEMPERATURE i DELT INSIDE OUTSIDE DELTA INSIDE OUTSIDE A INSIDE OUTSIDE DELTA l LOCATION (*F) (*F) ('F) (*F) ('F) (*F) (*F) (*F) (*F) l l l 3 r l [ t 1' t l i j i 1 f ' j t ( l l m:\3576w.2a.non:IME1898 4 77 Rev.1
FINAL a,c TABl.E 4.6-4 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 215.1, RC045B AVERAGE WALL MAXIMUM WALL MINIMUM WALL TEMPERATURE TEMPERATURE TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) i m11578w-2a.non:lb481898 4 78 Rev.I
S E T O N A T A DN D R O ) T AIT D A c e s S NI v E r T AV ( TE Y S D T I C M O U ) L c E M e s V I N v r 5- I ( L M 6 A 4 N ER L E M B T U ) c AN M e TI I u s 5 X f 4 A ( 0 C M R N E U G ) R A c e 1 R vs E r 5 V ( 1 2 A T S E T N O I T _ A C O L I i _ $a?I! tb! u l
FINAL j TABLE 4.6-6 TEST 215.1, RUN RC045, DISTRIBUTION OF DRY STRIPS AIR FLOW WET AVERAGE DRY WID1H (%) (IN) srr\3578w-2a rm:Ib-08I898 4-80 Rev.I
l FINAL i 4.7 Test 216.1 i l l l The constant flow test reported herein was conducted by establishing a steam flow at a constant rate and maintaining the flow until the vessel arrived at a constant pressure with the air caoling fan on and with water cooling to the vessel set to cover three quadrants. After the vessel reached a constant I pressure, the water was turned off to two of the wetted quadrants and the vesselis allowed to again reach a steady pressure. The extent of water coverage on the vessel was measured during each of the steady state periods. The steady state results for Test 216.1 at the two water coverages are tabulated in Tables 4.7-1 through 4.7-4 and are representative of approximately one hour of test operation. The tables are identified by the test run number "RC046" followed by an alpha suffix "A" or "B" to indicate the steady state conditions at 75 percent and 25 percent coverage, respectively. The steady state times are defined as l 10.656 to 11.651 for "A" and 13.239 to 14.253 for "B." Tables 4.7-3 and 4.7-4 present a comparison j of the average, minimum and maximum temperatures on the inside and outside vessel walls at each ! cross section of the vessel for each of the air flow conditions. Plots of the pressure and steam flow (vortex meter) are shown in Figure 4.7-1. Although not required for this test, the gas sampling apparatus was used during each of the steady state periods of the test. The results of the non-condensible sampling are shown on Figure 4.7-2 at the two sampling locations (Dome-90 -63"-3" and F-0*-6"). The data shows that the air tends to concentrate below the operating deck level. The sampling apparatus used during this test utilized pressure gages rather than pressure transducers; this increased the uncertainty in the noncondensible concentration to 1.0. Internal velocity meters were located in five internal locations in the test vessel as indicated in Table 3.0-1. The H6ntzsch anemometers (Dome-42"-165* 1.5" and A-90*-1.5") provided outputs that indicated that the velocities were generally up and toward the center in the vessel dome and down along the sidewall while at steady state. None of the Pacer anemometers provided outputs in excess of their minimum sensitivity during this test. Table 4.7-5 contains a summary of the indicated flows for the velocity sensors for the entire test run. Plots of the behavior of the internal velocity meters is shown in Figure 4.7-3. Condensation collection during the steady state portion of the test was performed with the condensate collection to tank 1 from the heel (open and closed creas) of the test vessel and the remainder to condensate collection tank 2. Water distribution around the circumference at the bottom of the baffle was taken after steady state at 75 percent water coverage was established and again after steady state at 25 percent coverage was achieved. Table 4.7-6 summarizes the water distribution around the circumference of the vessel at each of the steady state conditions. Figures 4.7-4 and 4.7 5 provide an indication of t he average temperature distribution as a function of } level for the inside vessel wall and the fluid temperature approximately 1 in. inside the vessel. ntus78. 2a.non;ib-osis9s 4-81 Rev.1
FINAL a,C l 4 r i E E N N N I e i
!k !
I f E a 2 re 1a E 6 w 2 h h m \3578w-2a.non:1b481898 4-82 Rev 1
7____.___ l l FmA1. i i-t I i l a,c i l 1 l t t l t 3 m i s i M A 1 4 i N I P= E li - U 2 11e U. s o Z 4 h v 2 m oc iT f l. ntusnw 2a.non:ib-osis9s 4 83 Rev,1
FINAL a,C U M c s
,J N
b b da e E 2 m E e 2 x
.5 e
a E e c
==
9 h 9 N s DC 5 m13578w-2a.non:Ib-081898 4-84 Rev.I
FINAL a,C i l i I U l N 1 c 3 l lllC ! ? A w e4 Yv b d 6 i 3 l E 8. E b
=
a N l-e i 3
.E T
h v 8 3
.Y I.m.
l l l m:\1578w-2a.non:lb-081898 4 85 Rev.I c- _ _ _ _ _ - - _ - _ - _ _ _ - - _ _ _ _ _ - _ - _ - _ _ _ _ - _ _ - _ _ _ _ _ _ _ _ . _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ - _ _ _ __
1 FINAL 1
- l a,C l
E E a
,J n
I H 1-E 5 1 m N e 2 i-mus7s 2a.non:1b-osis9s 4-86 Rev.?
FINAL a,c TABLE 4.71 TEST 216.1
SUMMARY
DATA RUN RC046A AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE ('F) ("F) ('F) (*F) ('F) i I m\3578w.2 anon-lM81898 4 87 Rev.1
FINAL _ a,c TABLE 4.7-1 (cont.) TEST 216.1
SUMMARY
DATA RUN RC046A AVERAGE TEST DATA l l l m:us78w.2 anon:ib-os1898 4 88 Rev.I j i
l l FINAL
- _ a,c TABLE 4.7-2 TEST 216.1
SUMMARY
DATA RUN RC046B AVERAGE TEST DATA i I l WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE I (*F) (*F) ('F) (*F) ('F) l l I l l l I l l l 1 mA3578w-2a.non.IN)81898 4-89 Rev.1
FLNAL _ a,c TABLE 4.7-2 (cont.) TEST 216.1
SUMMARY
DATA RUN RC046B AVERAGE TEST DATA v~me mA3578w-2a.non:Ib-081898 4 90 Rev.1
l FINAL
~
l i 1 _ a,c l TABLE 4.7-3 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 216.1, RCG46A AVERAGE WAi,L MAXIMUM WALL MINIMUM WALL TDIPERATURE TEMPERATURE TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) t mM578.-2a non. ib-081898 4 91 Rev.1 l
FINAL a.c TABLE 4.7 4 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 216.1, RC046B AVERAGE WALL MAXIMUM WALL TEMPERATURE TEMPERATURE MINIMUM WALL TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) rnesw-2 awn:ibais9s 4-92 Rev.1 !
l l l FINAL l
- _ a,c TABLE 4.7 5 TEST 216.1 RUN RC046, INTERNAL VELOCITY TEST DATA l
STANDARD AVERAGE MAXIMUM MINIMUM DEVIATION LOCATION (ft/sec) (ft/sec) (ft/sec) (fusec) NOTES t i 1 rrcuS78w-2a non:Ib-081898 4-93 Rev.1
FLNAL a.c TABLE 4.7 6 TEST 216.1 RUN RC046, DISTRIBUTION OF DRY STRIPS WET (%) TEST CONDITION OVERALL LOCATION DESCRIPTION nt\3578w-2a.non:Ib-081898 4-94 Rev.I
FINAL 4.8 Test 217.1 i The constant flow test reported herein were conducted by establishing a steam flow at a constant rate I and maintaining the flow until the vessel arrived at a constant pressure with the air cooling fan on and l with water cooling to the vessel set at a predetermined level. After the vessel reached a constant pressure, approximately 20 mole percent of helium was injected into the test vessel over a half hour time period and the vessel is allowed to again reach a steady pressure. The extent of water coverage on the vessel was measured during the steady state periods and gas sampling was performed to determine the concentration of noncondensibles. The steady state results for Tests 217.1 for the test before and after helium addition are tabulated in l Tables 4.8-1 through 4.8-4 and is representative of approximately one hour of test operation each. The l tables are identified by the test run number "RC052" followed by a alpha suffix "A"or "B" to indicate the steady state conditions before and after helium addition, respectively. The steady state times are ! defined as 8.860 to 9.863 for "A" and 12.877 to 13.872 for "B." Tables 4.8-3 and 4.8-4 present a comparison of the average, minimum and maximum temperatures on the inside and outside vessel walls at each cross section of the vessel for each of the air flow conditions. Plots of the pressure and steam flow (vortex meter) are shown in Figure 4.8-1. The helium was injected between 9.87 and l 10.37 hours at a flow rate of 3.48 x 104 lb/sec. The results of the non-condensible sampling are shown on Figure 4.8-2 at the four sampling locations (Dome-90 -63"-3", A-270 -6", E-90 -6"and F-0*-6"). The data shows that the air tends to concentrate below the operating deck level and that the helium concentration over the entire vessel reaches a well mixed condition after approximately 2 hours. The helium concentration is reported as a percent of the noncondensible concentration (air plus helium). The noncondensible partial pressure for the A elevation at approximately 11.7 hours appears to be a data recording error which is not supported in any way by the remaining data. Intemal velocity meters were located in five internal locations in the test vessel as indicated in Table 4.8-5. The H6ntzsch anemometers (Dome-42"-165 -1.5" and A-90*-1.5") provided outputs that indicated that the velocities were generally up and toward the center in the vessel dome and down along the sidewall while at steady state. None of the Pacer anemometers provided outputs in excess of their minimum sensitivity during this test. Table 4.8-5 contains a summary of the indicated flows for the velocity sensors for the entire test run. Plots of the behavior of the internal velocity meters is shown in Figure 4.8-3. Condensation collection during the steady state portion of the test was performed with the condensate collection to tank i from the heel (open and closed areas) of the test vessel and the remainder to condensate collection tank 2. I i m.u578w-za.non:id-osis9s 4 95 Rev.I
FINAt. I
~ Water distribution around the circumference at the bottom of the baffle was taken after steady state was established prior to and after the addition of helium. Table 4.8-6 summarizes the water distribution around the circumference of the vessel at each of the steady state conditions.
Figures 4.8-4 and 4.8-5 provide an indication of the average temperate.e distribution as a function of level for the inside vessel wall and the fluid temperature approximately 1 in. inside the vessel. I m:\3578w-2a.non:Ib-081898 4-96 Rev.1
FINAL a,C N U N e 3 5 J N b t'e 5 z k k E
! I E
1a 0 l = An e r l 7 a; 9 0 s as I. I I' l .. l m:\3578w-2a.non:Ib-08189s 4 97 r ( ..
FINAL
~
a,C E. U u E' x 5 t-t$ 1 F 1n 1 U i E s i E 1a R Z ea ab 4 h a m m:us7sw-2a.non:ib4)sts9s 4-98 Rev.1
I
.i FINA1, a,C l
l i l l N-an O V ! 3 e s M s N ! H D s e s-E e 2 e a i 6 .! 2s s= m ab 4 I s in. 4 m:\3578w 2a.non:le-081898 4-99 Rev.I
F-FINAL a,c M 8 a E u *
~
r: M 1 l-l a k E 5 ii k l> 1 2 4 2 s
.tF A
l m:\3578w 2a.non:1b 081898 ' 4 100 Rev.1 l l J
FINAL 1 l I I a,c l 1 4 l N m o V aC e s ac n w C H d w 2 K B H 2s E ee 4 8 s oc , E l I. ms57sw.2a.non:imis98 4 101 Rev.1
FINAL _ a,c TABLE 4.8-1 TEST 217.1
SUMMARY
DATA RUN RC052A AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE ('F) ('F) ('F) ('F) (*F) 1 m:\3578w 2a.non:Ib-081898 4-102 Rev.I
FINAL l l - a,c TABLE 4.81 (cont.) TEST 217.1
SUMMARY
DATA RUN RC052A AVERAGE TEST DATA l l l I l i c. l I i , l I i 1 l r i t i w __ l i l l I I i 1 m:\3578w-2 anon:Ib-081898 4-103 Rev.1 1 1
FINA1. a,c TABLE 4.8 2 TEST 217.1
SUMMARY
DATA RUN RC052B AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE ('F) (*F) ('F) (*F) ('F) l m:\3578w-2a.non:lb-081898 4,} g p
FINAL
- a,C TABLE 4.8-2 (cont.)
TEST 217.1
SUMMARY
DATA RUN RC052B AVERAGE TEST DATA l i m:\3578w-2a.non:lb-081898 4-105 Rev.I
FINAL l
- a,C 1
TABLE 4.8-3 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 217.1.RC052A AVERAGE WALL MAXIMUM WALL MINIMUM WALL TEMPERATURE TEMPERATURE TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) I I
.A mM578w-2a.non:Ib481898 4 106 Rev.1
FINAL _ a,e ; TABLE 4.8-4 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 217.1, RC052B AVERAGE WALL MAXIMUM WALL TEMPERATURE TEMPERATURE MINIMUM WALL TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) 1 l 1 1 l 1 l f I mA3578w-2a.non:Ib-081898 4-107 Rev.I
FINAL 1 _ a,c TABLE 4.8-5 TEST 217.1 RUN RC052, INTERNAL VELOCITY TEST DATA STANDARD AVERAGE MAXIMUM MINLMUM DEVIATION LOCATION (ft/sec) (ft/sec) (ft/sec) (ft/sec) NOTES mA3578*-2a.non. lb-081898 4-108 Rev.I
FINAL _ a,c TABLE 4.8-6 TEST 217.1, RUN RC052, DISTRIBUTION OF DRY STRIPS WET AVERAGE DRY WIDTH TEST CONDITION (%) (in)
- l I
i i l l 1 l i 1 1 m:uS7sw.2a.non:lt>os1898 4 109
FINAL 4.9 Test 218.1 ne constant flow tests reported herein were conducted by establishing a steam flow at a constant rate and maintaining the flow until the vessel arrived at a constant pressure with the air cooling fan on and with water cooling to the vessel set at a predetermined level. After the vessel reached a constant pressure,20 mole percent of helium is injected into the test vessel over a half hour time period and the vessel is allowed to again reach a steady pressure. De extent of water coverage on the vessel was j measured during the steady state periods and gas sampling was performed to determine the concentration of noncondensibles and helium. De insulation was removed from the bottom of the i vessel below the open and deadend compartment areas to simulate long term heat sinks; insulation was left under the steam generator compartment. The steady state results for 218.1 for the test before and after helium addition are tabulated in Tables 4.9-1 through 4.9-4 and is representative of approximately one hour of test operation. The
' tables are identified by the test run number "RC053" followed by a alpha suffix "A" or "B" to indicate the steady state conditions before and after helium addition, respectively. The steady state times are -
defined as 9.064 to 9.971 hours for "A" and 12.923 and 13.923 hours for "B." Tables 4.9-3 and 4.9-4 present a comparison of the average, minimum and maximum temperatures on the inside and outside vessel walls at each cross section of the vessel for each of the air flow conditions. Plots of the pressure and steam flow (vortex meter) are shown in Figure 4.9-1. De helium was injected between 9.95 and 10.45 hours at a flow rete of 3.46 x 10'3 lb/sec. The steam flow in test 218.1 shows a larger spi ad than in test 217.1 but it is a regular cycle which stays within a 360 lb/hr range required by the test procedure. He results of the non-condensible sampling are shown on Figure 4.9-2 at the four sampling locations (Dome-90*-63"-3", A-270*-6", E-90*-6"and F-0*-6"). The data shows that the air tends to concentrate below the operating deck level and that the helium concentration over the entire vessel reaches a well mixed condition after approximately 2 hours. Internal velocity meters were located in five internal locations in the test vessel as indicated in Table 4.9-5. De H6ntzsch anemometers (Dome-42"-165*-1.5" and A-90*-1.5") provided outputs that indicated that the velocities were generally up and toward the center in the vessel dome and down along the sidewall. Some outputs were noted from the Pacer anemometers, particularly at D-180*. No outputs were steady enough to obtain a flow direction and the high velocity outputs are most likely the result of the sensor blade being hit with condensation droplets. Table 4.9-5 contains a summary of the indicated flows for the velocity sensors for the entire test run. Plots of the behavior of the internal velocity meters is shown in Figure 4.9-3. Water distribution around the circumference at the bottom of the baffle was taken after steady state was established before and after helium addition. Table 4.9-6 summarizes the water distribution around the circumference of the vessel during each steady state period. mA3578w.2a.non:1b-081898 4 110 Rev.1 l
FLNAL Condensation collection during the steady state portion of the test was performed with the condensate collection to tank i from the heel (open and closed aress) of the test vessel and the remainder to condensate collection tank 2. Figures 4.9-4 and 4.9-5 provide an indication of the average temperature distribution as a function of level for the inside vessel wall and the fluid temperature approximately 1 inch inside the vessel. l
\
i j m:us78w-2a.ruslW]g9g Rey,1 ) 4 111
FINAL l a,C ; G S a I E u 5 n w C H DC
.3 m
k E 05 1a E 1 4 w 2 fe E 1 m us78w-2a.non:lW1898 4-112 Rev.1
; illlilllii!!l ll ,1 y?
l ' I Po 3 5 _ 0 _ C R n _ u R 1 8 1 2 t s . e T _ s n i o t a r t n e c c o C m i u l . e H d n ._ a _ l e ~ b i - s n . e d n o C- _ n o N 2-9 _ 4 e r u g - i F l I Bc3IVI .k . E . e mw Wg-(lflI\l!'I ll
\' i1l;ll
'lli
<l;!>
1 1it ~ l Po 3 5 0 C R n u R 1 8 1 2 t s e T , t s n e n e r u s a e M y t i c l o e V l a n r t e I n 3-9 4 er u g i F l l R.S ei5 t Ee5. ?Ou c q* ~ lll l\ i l!1l1 ,ll
4 FmAL l J 8,C m m o V E s
!n M
.I e.d
=
N h i=' h a 2 E. E 5
=a N
$e s
==
T e w E s N 6 i l ntV578w-2a.non:Ib-081898 4 115 Rev.I l~ L - - - -
FINA1. l 1 1 1,C I l l J J J i i i n N l s : 8 i, 5 4 I g ., 1 N E 1 H ! { 2a k E e F 3s E 9 9 e E s k m:us7sw-2a.non:ib-osin9s 4-116 Rev.1
t I l ! FINAL I I l l l l 1
- _ a,e j TABLE 4.91 TEST 218.1
SUMMARY
DATA RUN RC053A AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL - INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE (*F) ('F) ('F) ' ('F) ('F) l l l l 1 t l i 1 l l m:us78 2a.non:ibos1898 4-117 Rev.I
FINAL _ a,c TABLE 4.91 (cont.) TEST 218.1
SUMMARY
DATA RUN RC053A AVERAGE TEST DATA m l 6 u__ ___ _ _ _
FINAL _ _ 3,C 1 l l TABLE 4.9 2 l TEST 218.1
SUMMARY
DATA ! RUN RC053B AVERAGE TEST DATA , l l WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE (*FJ (*F) (*F) (*F) ('F) , 1 I I l l l l l mA3578w-2a.non:1b-081898 4-119
FINAn _ a,c TABLE 4.9 2 (cont.) TEST 218.1
SUMMARY
DATA RUN RC053B AVERAGE TEST DATA i I m:us7 w-2a.non:Ib-osis9s 4 120 Rev.1
r FINAL 1 1 I
- a,C TABLE 4.9 3 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 218.1, RC053A AVERAGE WALL MAXIMUM WALL MINIMUM WALL TDIPERATURE TEMPERATURE TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) l l
I I l mV578w-2a.non:lt@81898
FINAL a,c TABLE 4.9-4 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 218.1, RC053B AVERAGE WALL MAXIMUM WALL MINL%IUM WALL TEMPERATURE TEMPERATURE TEMPERATURE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) ('F) IDCATION I I m:\3578w 2a.non:lb-081898 4 122
FINAL u 1 _., a,c l ! TABLE 4.9-5 l TEST 218.1 RUN RC053, INTERNAL VELOCITY TEST DATA STANDARD AVERAGE MAXIMUM MINIMUM DEVIATION LOCATION (ft/sec) (Wsec) (Wsec) (Wsec) NOTES I i I 1 i 1 i I l i I' l i l l m11578w 2a.non:!b481898 4-123
FINAL _ a.c j TABLE 4.9-6 TEST 218.1, RUN RC053, DISTRIBUTION OF DRY STRIPS WET AVERAGE DRY M1DTH TEST CONDITION (%) (in) m:us78w.2a.non:lt4) sis 9s 4 124
l FINAL 4,10 Test 219.1 The constant flow test reported herein was conducted by establishing a steam flow at a constant rate and maintaining the flow until the vessel arrived at a constant pressure with the air cooling fan on and no water flow to the vessel. The steam flow rate was lowered to approximately 0.12 lbm/sec to limit the vessel pressure and baffle temperatures to an acceptable range. Helium was then injected into the steam line and the vessel was allowed to come to steady state. The water was then tumed on to a predetermined level of 10 percent of its maximum output and again allowed to reach a steady pressure. The steady state results for Test 219.1 are tabulated in Tables 4.10-1 through 4.10-6 and are representative of approximately one hour of test operation. The tables are identified by the test run i number "RC057" followed by an alpha suffix "A," "B" or "C" to indicate the steady state conditions at dry, dry with helium and wetted with helium, respectively. The steady state times are defined as: 12.653 to 13.653 hours for "A," 16.080 to 17.071 hours for "B," and 18.414 to 19.381 hours for "C." Tables 4.10-4 through 4.10-6 present a comparison of the average, minimum and maximum tempe atures on the inside and outside vessel walls at each cross section of the vessel for each of the test conditions. Plots of the pressure and steam flow (vortex meter) are shown in Figure 4.10-1. The helium was injected between 13.43 and 14.13 hours at a flow rate of 0.0036 lbm/sec (72*F,70 psig). The gas sampling apparatus was used during each of the steady state periods of the test. The results of the non-condensible sampling are shown on Figure 4.10-2 at the four sampling locations (Dome-90 -63"-3", A-270*-6", E-90*-6"and F-0 -6"). The data shows that the air tends to concentrate below the operating deck level. The plot also shows the helium concentration at each sample location and time. The helium concentration is shown to become uniformly distributed in the test vessel almost immediately after the application of water cooling. Internal velocity meters were located in five internal locations in the test vessel as indicated in Table 4.10-7. The H6ntzsch anemometer located at A-90 -1.5" indicated a generally downward flow along the sidewall while at steady state. The H6ntzsch anemometer located at Dome-42"-165 -1.5" showed almost no change in output from before the test was started to the end and is assumed to have failed. The Pacer anemometer at Dome-42"-345 -1.5" did not provide any output and is considered not to be functional. The other two of the Pacer anemometers only provided a total of 5 output values above a nominal 0.4 ft/sec. The five higher values recorded are considered to be a result of condensate dropping onto the anemometer's blades. Table 4.10-7 contains a summary of the indicated flows for the velocity sensors fo'. the entire test run. Plots of the behavior of the internal velocity ! meters is shown in Fi;me 4.10-3. Condensation collection during the steady state portion of the test was performed with the condensate collection to tank i from the heel of the test vessel and the remainder to condensate collection tank 2. , mA3578wca.non:Ib-081898 4-125 t
FINAL Water distribution around the circumference at the bottom of the baffle was taken after steady state water coverage was established. The water flow was set to 10 percent of its range but the surface was l
. still observed to be 99.5 percent wetted. Only one 3 in. dry stripe was observed at approximately 340*.
Figures 4.10-4 and 4.10-5 provide an indication of the average temperature distribution as a function of level for the inside vessel wall and the fluid temperature approximately 1 inch inside the vessel. In\3578w-2a.non Ib-081898 4.]26
FINAL a,c I l l t- . 46 {
@ 4 V l l 3 m
M J
.iN=
s D C
.1
=
k E a N r.c la b s e b i o
=
0 m et l 1 muS7sw-2a.non:st>os1898 4-127
FINA1, a,C E 6 a
.E a
J d N 1 i li O U iO O E z N b 4 I s
.9 mA3578w 2a.non:Ib-081898 4-128
~ FINAL a,C I
l 6 f no o O
% i i
c n '
% I J
.M.
N U E-
$c 2
m U i 6 , m i v> M
.2 at b
.T.
z ,
> l 3m 6
3
.ma 7
o v v 6 m 0C F sie i mA3578w.2amn:Ib 081898 4 129 l L_____._____.._
FINAL I ac i l t N l 6 a E a I N l Y. b E as H I
)>
2 4
.tf h
m:\3578w-2a.non:lb-081898 4 130
., . . . , _ . =.. . .. FINAL EC 6 m O U K c s M
,Z e'
em N b b [ 6 2 K E-e b 2s E
=
b m A I 3
.tF b
m:\%78w-hnon:lN081898 q 3y i l
FINAL a,c TABLE 4.10-1 TEST 219.1
SUMMARY
DATA RUN RC057A AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE ('F) (*F) (*F) ('F) ('F) mA3578w-2a.non.lb-081898 4 132
FINA1.
- 3,C TABLE 4.101 (cont.)
TEST 219.1
SUMMARY
DATA RUN RCOS7A AVERAGE TEST DATA i I l
)
l l l l i I 1 I l l l I m:\3578w-2a.non:Ib-081898 4 133
FINAL j
- "'" f
- TABLE 4.10 2 TEST 219.1
SUMMARY
DATA RUN RC057B AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE (*F) ('F) ('F) ('F) (*F) l l _ m:\3578w-2a.non:lb-081898 4 134
FINAL _ a,c TABLE 4.10-2 (cont.) ) TEST 219.1
SUMMARY
DATA RUN RC057B AVERAGE TEST DATA 1 l l l l m:\357bw-2a.non:lb481898 4-135
FINAL ac TABLE 4.10 3 TEST 219.1
SUMMARY
DATA RUN RC057C AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE ('F) ('F) ('F) ('F) ('F) m:\3578w-2a.non:lb-081898 4 136
FINAL t
- a,c
'~
l TABLE 4.10-3 (cont.) TEST 219.1
SUMMARY
DATA RUN RC057C AVERAGE TEST DATA a l
~~~
i 1 m:\3578w 2a.non:ltw081898 4 137
~ FINAL a,c l[~ - TABLE 4.9-4 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 219.1, RC057A AVERAGE WALL MAXLNIUM WALL MINIMUM WALL TEMPERATURE TEMPERATURE TEMPERATURE DELT INSIDE OUTSIDE A INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*O (*D (*D (*D PD PD PD PD (*D I I i l l i l I l I 1 l m\3578w.h.non:Ib-081898 4 138 l J
FINAL a.c TABLE 4.9-5 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 219.1, RC057B MAXIMUM WALL MINIMUM WALL AYERAGE WALL TEMPERATURE TEMPERATURE TEMPERATURE IN5!!< OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) 1 I i l l l \ l I i l I m:\3578w 2a non:ltwo81898 4-139
- t. .-
f FINAL I 1 _ a,c TABLE 4.9-6 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 219.1, RC057C AVERAGE WALL MAXIMUM WALL TEMPERATURE TEMPERATURE MINL%fUM WALL TEMPERATURE LNSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) (*F) ('F) (*F) (*F) (*F) (*F) ('F) ('F) 1
'1 l
m:\3578w-2 anon.lbO81898 4 140
FINAL i _ a,c TABLE 4.10 7 TEST 219.1 RUN RC057, INTERNAL VELOCITY TEST DATA STANDARD AVERAGE MAXIMUM MINIMUM DEVIATION LOCATION (ft/sec) (ft/sec) (ft/sec) (ft/sec) NOTES m:\3518w-2tnon.lb-081898 4 141
F m t. 4.11 Test 220.1 l Re transient flow test reported herein was conducted by providing the maximum flow of steam 1 attainable to the test section for a 20 to 30 second period of time. The flow was then reduced to I approximately 0.5 lb/sec. for the remainder of the test until the vessel anived at a constant pressure I with the air cooling fan on and with water cooling to the vessel set at a predetermined level. The l extent of water coverage on the vessel was measured during the steady-state periods and gas sampling I was performed to detennine the concentration of noncondensibles. For Test 220.1, the insulation was I removed from the bottom of the vessel below the open and deadend compartment areas; insulation was I left under the steam generator compartment. l l Review of the steam flows from the condensate and vortex meters indicated that the vortex meter I consistently performed at a 15 to 20 percent lower flow than indicated by the condensate over the I steady state period. The vortex meter operates at 7.5 percent of its operational range and therefore its l I accuracy relative to reading is a large percentage (-10 percent). It is recommended that the vortex
! meter outputs be used for time-dependent performance and the condensate measurement for the steady I state performance characteristics (or 15 percent be added to the vortex measured steam flow rate for I all times greater than 10.9 hours to compensate for this difference).
I l Re initial transient steam flow to the test vessel is shown in Figure 4.11-1. De start of the transient i is back calculated from the data contained in Appendix D to 10.7122 hours or about 10 seconds before l the first transient data set. I I The steady state results for Test 220.1 are tabulated in Table 4.11-1; the steam state time is defined as I from 11.9814 hours to 12.9997 hours. A plot of the vessel pressure, steam flow (vortex meter), and I steam flow (condensate)is shown in Figure 4.11-2. The indicated pressures are corrected for an offset I of 0.12 psi at the start of the test to adjust the ambient pressure within the vessel to equal the recorded I pressure from the transducer. I I The results of the noncondensible sampling are shown in Figure 4.11-3 at the four sampling locations I (Dome-90*-63"-3", A-270*-6", E-90*-6"and F-0*-6"); note that the pressure axis is displayed in " psia" I rather than the "psig" used in Figure 4.11-1. The data show that the air tends to concentrate below the I operating deck level). I l Internal velocity meters were located in five locations in the test vessel as indicated in Table 4.11-2. I he H6ntzsch anemometer A-90*-1.5" provided output that indicated that the velocity along the wall I was down along the sidewall throughout the test. The H6ntzsch anemometer at Dome-42"-165* 1.5" l did not provide any useable output. The Pacer anemometers at E-300 -1" provided outputs in excess I of their minimum sensitivity over the first 6 minutes of the test and then read below their detection I The meter accuracy is quoted as I percent of full scale with the range extending f ,m 5 9 to .45 lb/sec. at the meter's test operating condatx t m:\3578w 3.non.lb-o81898 4 142 Rev.1
FINat. I limits. The Pacer located at Dome-42"-3450 -1" provided outputs over the majority of the test with I some high velocities noted (9,12,25, etc) on a sporadic basis; the c.ajority of outputs were on the I order of the average value shown in Table 4.11-2. Figure 4.11-3 contains a summary of the indicated l l flows for the velocity sensors for the entire test mn. I l Condensation collection during the steady state portion was switched to different collection tanks to I determine the distribution of condensate within the vessel. Table 4.11-3 documents the condensate I flows for the dome and sidewall during the steady state period. Review of the data indicates that only l
! 3 to 4 percent of the condensate collects as rainfall and bottom collection (steam generator f
I companment and remainder of bottom). The remainder of the condensate is almost equally divided
)
I between the side wall and dome. I l I Water distribution around the circumference at the bottom of the baffle was taken after completion of I the transient and after steady state was established. Table 4.11-4 summarizes the water distribution I around the circumference of the vessel at each of the steady state conditions. I I Figures 4.11-4 and 4.11-5 provide an indication of the average temperature distribution as a function I of level for the inside vessel wall and the fluid temperature approximately 1 in. inside the vessel. l l l 1 l l i mus78 -3.non:ib-osis9s 4-143 Rev.1
FmAL
- a,c I
N-at s-a at N N I H t k, E E li 3 3
'T C
4 E s
.3F sa.
m:us7sw.3.non: bats 9s . 4 144 Rev.1
FINAt,
"~
a,c N 8 U u a s x d N 1 D C
.1
=
is o E E a 3 m 1a 2 s A l 4 E s i [ l i I m:us78w-3.non:Ib-osis9s 4 145 Rev.1 , 1 1
FINAL
- a.c n
8 U M E a a N N 5 F b o V 1o Z-7 4 2
.Es 6
I i l 1 m:us78w.3.non:ib-osis9s 4-146 Rev.I f l i
1 FINAL , L - a,C I l l l h 1 N ' 5 a m x N N ia E e E w
.1::
2 ' 2 i 4 2 E i i-i mA3578w 3.non:tb-osis9s 4-147 Rev.I j
FINAL
- - a,e N
8 U N m 3 m J b a 3 H w 2 8. E e b a k 1 e 9 4 E h 1 l m:us7sw.3.ncaitrosis9s 4-148 Rev.1 ) l 4
I d FINAt. ; i a,c l l l l n as a s as
?
N N 5 F b a 1 2 E. I E l F i 3s ! E Ew 3e em
?
I gaul 4 2
.5 l 6 ;
m:us7sw.3.natib-osis9s 4 149 Rev.I
FINAL a,C TABLE 4.11.1 TEST 220.1
SUMMARY
DATA RUN RC062 AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE ('F) (*F) (*F) ('F) (*F) l m:\3578w 3.non:lb-081898 4-150 Rev.I
FINAL j l a.c TABLE 4.11.1 (cont.) TEST 220.1
SUMMARY
DATA l RUN RC062 AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES { INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE ('F) ('F) ('F) (*F) (*F) I m:U578w-3 non:Ib-081898 4 151 Rev.1
il 4 , 4l1l l l\il 3le. _ r" I l S E T O N A T A D T S E DN T RO ) . Y AIT c e T I D NIA /s AV t C f ( O TE SD L E V 2L 1 A M ) 1 N U c 4R M e l eE I
/t s
bT N aN I f ( TI . M 2 6 0 C R M N U ) c U M e R I
/t s
X 1 A f ( 0 2 M 2 T S - E T E G ) . A c e R /t s E V f ( A N O I T A C O L I l Ec$7c.$= f g *- - 11l(llIllll! l\ l l.
1 l ll l l il1i1I ;1 l1 1 iIii I !; l l,
's>Y
_ rn i I E _ R U ._ T A R oc . E P _ _ R M H E 0 T 3 1 . O _ T > 7 WE _ 3 2 O L A T _ 1 D F R w. ._ O . I m R E P _ E _ M N I T O I T A C D I E T A S E N R E U D T N O A R o c C E P F R H M O E N 3 T 2 O I 1 3- T 0 8 U 1 > 1 B 0 WE 4I ER 2 1 DA T m LT S D I F R w B M O A T I. 2 IR E 6 P W C E R MI N N T O I U T A R, C I. O 8 L 2 2 T S E T E R U T R A n c . E ._ P _ R M H E _. 5 T 8 __ 8 1 _ O WE O T T 5 1 LA F R w-o 1 D O I R E P E N M O I I T T _ A _ C D I _ m i I 5=i.9l {g . e W e. e
FINAL - a.c I TABLE 4.114 l TEST 220.1, RUN RC062, DISTRIBUTION OF DRY STRIPS l TEST CONDITION WET AVERAGE DRY WIDTH I (%) (in.) l l l l 1 m:\3578w-3 non:lb-081898 4 154 Rev.1
Ftut a,c a,c I TABLE 4.115 l VESSEL TEMPERATURE DISTRIBUTION FOR TEST 220.1 l AVERAGE WALL MAXIMUM WALL MINIMUM WALL l TDIPERATURE TEMPERATURE TEMPEL'4TURE I LOCATION INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA I en io ~ cn en en en en en en 1 I l l l l l l l T ' m.uS78w-3 non:Ib-081898 4-155 Rev.1
i l FINAL I l 1 I This page left intentionally blank 7
- nt\3578w.3m:Ib 081898 4-156 Rev.1
i FINA1. 4.12 Test 221.1 The transient flow test reported herein was conducted by introducing an initial high steam flow (2 lbm/sec) for approximately 40 seconds followed by a reduced steam flow of approximately I lbm/see for 5 minutes with a flow reduction to 0.1 lbm/see for the remainder of the test. Helium is added to the system through the steam line after steady state is reached at 0.1 lbm/sec steam flow. The water cooling is shut off after steady state is reached. The test is continued until the pressure stabilizes. A constant air flow is maintained through the test by maintaining the air cooling fan at a constant speed. The insulation was removed from the bottom of the test vessel below the open and I deadend compartment areas; insulation was left under the steam generator compartment. Review of the steam flows from the condensate, vortex and Gilflo meters indicates that the Gillio meter has consistently been performing at a 15 to 20 percent lower flow than indicated by the condensate and the vonex meter during steady state flows. The initial flow transient recorded by the vortex meter is about half of the flow recorded by the Gilflo meter during the initial transient. Review of the strip chans which continuously give an indication of the steam flow shows that the initial flow was held for approximately 48 seconds at 2.00 0.11 lb/see fellowed by 5.2 minutes where the average flow was 1.01 0.07 lb/sec as monitored by the "Gilflo" flow meter. The vortex meter produced outputs that were beyond its calibration range for the initial flow transient. The second portion of the transient is within output range of the vonex meter and indicates a steam flow rate of 1.18 0.06 lb/sec. It is recommended that the Gilflo output be used for the initial flow transient and the vortex meter outputs be used for time dependent performance after the initial transient and either the condensate measurement or the vortex meter for steady state performance characteristics. The steady state results for Test 221.1 are tabulated in Tables 4.12-1 through 4.12-6 and are representative of approximately one hour of test operation. The tables are identified by the test run number "RC056" followed by an alpha suffix "A," "B" or "C" to indicate the steady state conditions of wet, wet with helium present, and steady state dry, respectively. The steady state times are defined as: 8.516 to 9.516 hours for "A," 12.411 to 13.245 hours for "B," and 17.5389 to 18.538 hours for "C." Tables 4.12-4 through 4.12-6 present a comparison of the average, minimum ard maximum temperatures on the inside and outside vessel walls at each cross section of the vessel for ea;h of the air flow conditions. Plots of the pressure and steam flow are shown in Figure 4.12-1; the steam flow is a result of the combination of Gilflo and vortex meter outputs as recommended above. The helium was injected between 9.53 and 10.28 hours at a flow rate of 0.00385 lb/sec (75*F,70 psig). Although higher than the required flow rate, this flow is sufficient to accomplish the test purpose of addressing the effects of helium mixing on the long term cooling during post accident conditions. The gas sampling apparatus was used during each of the steady state periods of the test. The results of the non-condensible sampling are shown on Figure 4.12-2 at the four sampling locations (Dome-90 -63"-3", A-270*-6", E-90*-6" and F-0*-6"). The data shows that the air tends to concentrate below the operating deck level. The plot also shows the helium concentration at each sample location and time. The helium concentration is shown to become uniformly distributed in the test vessel during the mA3578w.3.non.lb-081898 4-157 Rev.1
l FLNAt. water cooling portion of the test after about three hours. The helium concentration difference between the volumes above and below the operating deck increased after stoppage of water flow to approximately 5 percent. Two helium concentration data points shown are inconsistent with the trends shown for the remainder of the test and it is recommended that they be ignored. Internal velocity meters were located in five internal locations in the test vessel as indicated in Table 4.12-7. The H6ntzsch anemometer located at A-90*-1.5" indicated a generally downward flow along the sidewall while at steady state. The H5ntzsch anemometer located at Dome-42"-165'-1.5" showed little change in output from before the test was staned to the end and is assumed to have failed. The Pacer anemometer at Dome-42"-345'-1.5" showed activity during the helium addition and during the dry portion of the test with few indications at other times. The Pacer anemometer at E-30 showed limited outpnts which were concentrated during the dry portion of the test. 'Ihe Pacer anemometers at D-180* showed very few indications higher than a nominal 0.4 ft/sec and is assumed to be nonfunctional. Table 4.12-7 contains a summary of the indicated flows for the velocity sensors for the entire test run. Plots of the behavior of the internal velocity meters is shown in Figure 4.12-3. Condensation collection during the steady state portion of the test was performed with the condensate collection to tank 1 from the heel (open and closed areas) of the test vessel and the remainder to condensate collection tank 2. Water distribution around the circumference at the bottom of the baffle was taken after steady state water coverage was established. Table 4.12-8 summarizes the water distribution around the circumference of the vessel at each of the steady state conditions. Figures 4.12-4 and 4.12-5 provide an indication of the average temperature distribution as a function of level for the inside vessel wall and the fluid temperature approximately 1 inch inside the vessel. mM578w-3.non:lb-o81898 4-]$g
1Il ill!ljl gs I l c 6 5 0 C R n u R 1 1 2 2 t s e T y r t o i s H w l o F m a t e S d n a e r - u s s e r P l e s s e V 1 2 1 4 e r u g i F ~ l l
$se45_b! t-@ xg w
FINAL a,C O aC e s DC 4 ' N h E
.2 1h I
h O i.O h z N N 4 as ii. m:uS78 -3.non:tbos209s 4-160 Rev.2 .f
FINAL a,c 3 6 cc c s oc J N ca is I 2 li E s n N 4 2 s u E l l l I l l l ntus7sw-3.non:tb-os209s 4-161 Rev.2 E _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ . _ _ _ _ _ _ _ . . _ _ _ . _ _ _ .
- - -- -,--r,-- ------m- - - , - - . - - - - - . - - - - . - . - , - - - - - . - - , - - - - - - - - - - - ------.---- - - - , - -- - , - , - - - - - - - - - - - - - - - - - - , . . - - - - - - FINAL
~
a,c E 6 x E a 5 5 m b f a. h E 5 ii k 1 n 9 9 U E
-L _
mA3578w.3mn:lb482098 4-162 Rev.2
FmAL a,c i l i w m o U i g 1 a s u a ! N N 5 i- , h 2 2 l 1 h 2s E N m 4 2 s
. 18 i
- r. . ;
l ntuS7sw-3.non: b-os209s 4 163 Rev.2
FINAL a,c TABLE 4.121 TEST 221.1
SUMMARY
DATA RUN RC056A AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE ('F) (*F) (*F) ('F) ('F) mA3578w-3 non:Ibo81898 4.} (4
l l FINAL a,c l TABLE 4.121 (cont.) TEST 221.1 SUM 51ARY DATA l RUN RC056A AVERAGE TEST DATA i l l l mA3578w 3 non.lb 081898 4.]65
_______ ____ _ _ _ l FINA1. 1 a,c i TABLE 4.12 2 TEST 221.1
SUMMARY
DATA
. RUN RC056B AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE '
INSIDE OUTSIDE FLUID WALL AT BAFFLE ('F) ('F) ('F) (*F) (*F) m:\3578w 3.non:lt481898 4.] g
FINAL
~
ac TABLE 4.12-2 (cont.) TEST 221.1
SUMMARY
DATA ) RUN RC056B AVERAGE TEST DATA I I 1 l i m:\3578w 3.non:Ib-081898 4.}67
FINAL i a,e TABLE 4.12-3 TEST 221.1
SUMMARY
DATA RUN RC056C AVERACE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE ('F) (*F) ('F) ('F) (*F) l' m:\3578w.3.non:tb 081898 4-168
FINAL ac TABLE 4.12 3 TEST 221.1
SUMMARY
DATA RUN RC056C AVERAGE TEST DATA l l 1 l l l 1 I
' m:\3578w 3 non:lt481898 4,} gg
\ ; w-_----_-_-- -- _ -.
i FINAL l
- a.c TABLE 4.12-4 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 221.1, RC056A AVERAGE WALL MAXIMUM WALL MINIMUM WALL
- TEMPERATURE TEMPERATURE TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION ('F) ('F) ('F) ('F) (*F) ('F) (*F) (*F) ('F) 1 l
m\3578w 3.non:1b481898 4.}70
FrNAL TABLE 4.12 5
] LC .
i VESSEL TEMPERATURE DISTRIBUTION FOR TEST 221.1, RC056B { AVERAGE WALL MAXIMUM WAi.L MINIMUM WALL TEMPERATURE TBiPERATURE TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) ('F) (*F) ('F) (*F) (*F) (*F) (*F) (*F) a i I l J I mA3578w-3.non:lb-081898 4.]7]
D.ut a.c TABLE 4.12-6 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 221.1, RC056C AVERAGE WALL 1EMPERATURE MAXIMUM WALL MINIMUM WALL 1EMPERATURE TEMPERATURE INSIDE OUTSIDE DU.TA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*D (*O (*D (*D (*D (*O (*O (*O (*O m:U$78w 3.non:IM81898 4 172 1
FINAL l l a,c l l l _ TABLE 4.12 7 TEST 221.1 RUN RC056, INTERNAL VELOCITY TEST DATA I i STANDARD AVERAGE MAXIMUM MINIMUM DEVIATION LOCATION (fusec) (fusec) (fusec) (fusec) NOTES l I I I _s I l l I l m.\3578w 3 non:lb481898 4-173
FLNAL a,c TABLE 4.12-8 TEST 221.1 RUN RC056, DISTRIBUTION OF DRY STRIPS TEST CONDITION WET AVERAGE DRY WIDTH (%) (in) l m:us78w 3.non:1b-osis9s 4.j74
l l FINA1, 4.13 Test 222.1 The transient flow test reponed herein was conducted by providing the maximum flow of steam attainable to the test section for a 15 second period of time. The flow was then reduced to approximately 3 lbm/sec for 30 seconds and then reduced to 0.5 lbm/sec for the remainder of the test until the vessel arrived at a constant pressure with the air cooling fan on and with water cooling to the vessel set at a predetermined level. The extent of water coverage on the vessel was measured during the steady state periods and gas sampling was performed to determine the concentration of noncondensibles. For test 222.1 the insulation was removed from the bottom of the vessel below the I open and deadend compartment areas; insulation was left in ;.. ace under the steam generator compartment. Review of the steam flows from the condensate and vortex meters indicates that the vonex meter consistently performs at a 8 to 12 percent lower flow than indicated by the condensate over the steady state period. It is recommended that the vortex meter outputs be used for time dependent performance and the condensate measurement for the steady state performance characteristics (or 8 percent be added to the steam flow rate for all times greater that i1.05 hours to compensate for this difference). The initial transient steam flow to the test vessel is displayed in Figure 4.13-1. The start of the I transient is back calculated from the data contained in Appendix D to 11.0302 hours or about 6 seconds before the first transient data set. i l The steady state results for Test 222.1 (Run RC061) are tabulated in Table 4.13-1 and 4.13-2 prior to the first pressure upset shown in Figure 4.13-2 and are representative of approximately one hour of l test operation. The steady state time is defined as from 12.434 to 13.432 hours. Table 4.13-2 presents a comparison of the average, minimum and maximum temperatures on the inside and outside vessel walls at each cross section of the vessel for each of the air flow conditions. Plots of the vessel pressure and steam flow (vortex meter) are shown in Figure 4.13-2. The pressure upsets shown around 13.5 and 14.1 hours were due to a direct discharge of condensate that had backed up into the test vessel. The vessel pressure transducer is closely coupled with the vessel sight gage line and is reacting to the localized decrease in pressure. The comparison of the condensate and vortex steam flow measurements are also illustrated in Figure 4.13-2. The vortex flow meter is operating at the lower end of its operational range during the third flow rate period (0.5 lbm/sec) and therefore the discrepancy noted is about 1.3 percent of full scale (6.7 lbm/sec) or about 8 to 12 percent lower than the condensate flow rate.2 The meter has a rated accuracy of 1 percent of full scale. The results of the non-condensible sampling are shown on Figure 4.13-3 at the four sampling locations (Dome-90*-63"-3" A-270*-6", E-90*-6"and F-0*-6"). The data shows that the air tends to concentrate below the operating deck level). 2 The meter accuracy is quoted as 1% of full scale with the range extending from 5.9 to .45 lb/sec at the meter's test operating conditions. m:\3578w 3.non:ltr081898 4-175 Rev.1
FIN 41. Intemal velocity meters were located in five locations in the test vessel as indicated in Table 4.13-3. l The H6ntzsch anemometer A-90*-1.5" provided output that indicated that the velocity was down along the sidewall throughout the test. The Huntzsch anemometer at Dome-42"-165'-1.5" did not provide any useable output. The Pacer anemometers at E-30* -1" and Dome-345*-1" provided outputs in excess of their minimum sensitivity over the first 10 minutes of the test and then read below their detection limits for the remainder of the test. The Pacer anemometer located at D-180*-1" provided outputs sporadically over the first hour of the test. The majority of outputs were on the order of the average value shown in Table 4.13-3. Table 4.13-3 contains a summary of the indicated flows for the velocity sensors for the entire test run. Plots of the behavior of the internal velocity meters is shown in Figure 4.13-4. Condensation collection during the steady state pottion was switched to different collection tanks to determine the distribution of condensate within the vessel. Table 4.13-4 documents the condensate flows for the dome and sidewall during the steady state period. Review of the data indicates that only 3 to 4 percent of the condensate collects as rainfall and bottom collection (steam generator compartment and remainder of bottom). The remainder of the condensate is almost equally divided i between the side wall and dome. Water distribution around the circumference at the bottom of the baffle was taken after completion of the transient and after steady state was established. Table 4.13-5 summarizes the water distribution around the circumference of the vessel at each of the steady state conditions. Figures 4.13-5 and 4.13-6 provide an indication of the average temperature distribution as a function of level for the inside vessel wall and the fluid temperature approximately 1 inch inside the vessel. i m:U578w.3.non:lb-o81898 4.]76
FINAs, a,c 8 U at s a as c4 m N 5 k k E a 3 m 1 l E 1 3
'?
m
- M i 9 j 2 !
5 i ra, i l r _. m:uS7sw-3.non:ibosta9s 4-177 Rev.1
FINAL R,C N
=
A h e O
.E
=c k
k E E-1 b 1 N 4 I Ec a mA3578w-3.non:lbGl898 4.]78
FLNAL a,c l l at a m. as e4 N N 5 b
.I a
J: a O
.8 i.
U k o Z
. 7 m
4 2 i i l l 1 l ntuS78w-3.non:t b-082098 4 179 Rev.2 L___ _ _ _ _ _ . _ _ _ _ _ _ _ _ _ _ _ _ . _ _ _ _ _ _ _ _ _ _ _ . _ _ _ . _ _ . _ _ . _ _ _ . _ _ _ _ _ _ . _ _ _ _ _ _
FINAL Ac I as a a aC N N i I H ia E e Ie 2 b e 1 E s 2 i O 4 2 s
.2f k
m us$sw-3.non:1ba2098 4-180 Rev.2
1 I FINA1. a,c f' l i l l l l som
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M s s E ei N N 5 H h 2* l L
.E H
==
a N j e Ne m 9 m
~.
w E s oc is nu57sw-3.non:ib.os209s 4-181 Rev.2
FINAL 8,C 1 i l M a 5 M c4 N h 1 5 h 2 d A. 4 U
.Es fan l
m13578w-3.non:Ib-082098 4-182 Rev.2
)
]
FINAL, a,C TABLE 4.131 TEST 222.1
SUMMARY
DATA RUN RC061 AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE OUTSIDE FLUID WALL AT INSIDE BAFFLE ('O ('F) ('F) ('F) ('F) I l i l l l m:\3578w 3.non Ib-081898 4-183 l- \ _ _ _ -
FINAL
~
a,C TABLE 4.13-1 TEST 222.1
SUMMARY
DATA RUN RC061 AVERAGE TEST DATA m \3578w-3.non. lb481898 4-184
FINAL i I 1 i a,c TABLE 4.13 2 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 222.1 I AVERAGE WALL TEMPERAR'RE MAXIMUM WALL MINIMUM WALL TEMPERATURE TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA IDCATION PO CO PO PO PO CO PO PD 06 1 l l l l 1 m.us78w.3.non: b-osi89s 4-185 Rev.I
FINAL a.c TABLE 4.13 3 TEST 222.1 RUN RC061, INTERNAL VELOCITY TEST DATA LOCATION AVERAGE MAXIMUM MINIMUM STANDARD DEVIATION NOTES (fdsec) (fvsec) (fusec) (fvsec) m:us7sw.3.non:Ib-osis9s 4 186 Rev.1
FINA1.
~
~
ac TABLE 4.13 4 TEST 222.1, RUN RC061, DISTRIBUTION OF CONDENSATE TIME PERIOD 11.25 TO 13.25 HR TIME PERIOD 13.7 TO 14.3 HR TIME PERIOD 14.56 TO 14 9 HR LOCATION FLOW TEMPERATURE LOCATION FLOW TEMPERATURE LOCATION FLOW TEMPERATURE RATE RATE RATE (Ib/sec) (*F) (Ib/sec) (*F) (Ib/sec) ('F) l l l \ 5 m11578w-3.non:lb-081898 4-187 Rev.l' s
FINA1.
~
u l TABLE 4.13-5 TEST 222.1, RUN RC061, DISTRIBUTION OF DRY STRIPS TEST CONDITION WET AVERAGE DRY WIDTH (9) (in) l m\3578w.3.n=:1b-osis9s 4 188 Rev.I
FINAL T l 4.14 Test 222.2 l The transient flow test reported herein were conducted by providing the maximum flow of steam j attainable to the test section for a 15 second period of time. The flow was then reduced to approximately 3 lbm/sec for 30 seconds and then reduced to 0.5 lbm/see for the remainder of the test until the vessel arrived at a constant pressure with the air cooling fan on and with water cooling to the vessel set at a predetermined level. De pressure is then increased to approximately 30 psig and the vessel is allowed to come to steady state. The extent of water coverage on the vessel was measured during the steady state periods and gas sampling was performed to determine the concentration of noncondensibles. The bottom of the vessel below the open and deadened companment areas remained uninsulated with the insulation left in place under the steam generator companment. l The initial transient flow to the test vessel with the steam diffuser raised to a level 5.8 ft. above the operating deck is displayed in Figure 4.14-1. The start of the transient is calculated from the data I contained in Appendix D to the data set taken at 9.9936 hours. The mass flow transient was calculated from the vonex meter output together with the steam temperature and pressure at the flow meter. The line pressure at the steam meter was estimated from the data available in the DAS output and the pressure history of similar transients. The steam temperature was estimated from a linear regression of the DAS monitored steam temperature. The nominal values of pressure and temperature are indicated on Figure 4.14-1. The results for the low (RC065A) and high (RC065B) steam flow rate, steady state periods of Test 222.2 are tabulated in Tables 4.141 and 4.14-2. The steady state data was taken from the time periods 12.06 through 13.04 hours and 15.32 through 16.32 hours, respectively. Tables 4.14-3 and 4.14-4 show a summary of the vessel average, minimum, and maximum temperatures on the inside and outside reactor walls at each set of test conditions. Also included are the maximum, minimum, and average differential temperatures across the wall. The data presented is representative of approximately one hour of test operation; plots of the vessel pressure and steam flow (vonex meter) are shown in Figure 4.14-2. The comparison of the condensate and vortex steam flow measurements are also illustrated in Figure 4.14-2. The steam flow as recorded by the vonex meter maintains a steady flow over both of the steady state periods. The condensate flow settles into a steady flow rate approximately 5 percent higher than the steam flow rate. Condensation collection during the steady state portion was switched to different collection tanks to detennine the distribution of condensate within the vessel. Table 4.14-5 documents the condensate flows during the steady state period. The initial two collection periods seem to indicate that condensate was held up for a time and later discharged during the second period and the early pan of the third. Review of the data indicates that approximately 61 percent of the condensate is generated on the vessel dome during the final collection j period. i l Re results of the non-condensible sampling are shown on Figure 4.14-3 at the four sampling locations [ [ (Dome-90*-63"-3", A-270 -6", E-90*-6"and F-0 -6"). The data shows that the air tends to concentrate no3578w.3.non:nwoais98 4-189 Rev.I
FmL below the steam injection point, since the air partial pressure at both the "P and "E" levels are close to the pressure of the vessel. The internal velocity meter located at A-90*-1.5" provided output that indicated that the velocity was down along the sidewall throughout the test. The majority of readings were on the order of the average value shown in Table 4.14-6 with the peak velocity occurring during the initial steam transient. The remainder of the internal velocity meters did not function throughout the test and are considered to have failed. Figure 4.14-4 shows the behavior of the internal velocity meters throughout one test. Water distribution around the circumference at the bottom of the baffle was taken after completion of the transient and after steady state was established. Table 4.14-7 summarizes the water distribution around the circumference of the vessel at each of the steady state conditions. Performance of the velocity meter (Channel 295) below the fan assembly is no longer providing reliable data. Use fan calibration data located in Section 2.2.7, equation 13 for an estimate of the outlet velocity based on the fan RPM. Figures 4.14-5 and 4.14-6 provide an indication of the average temperature distribution as a function of level for the inside vessel wall and the fluid temperature approximately 1 inch inside the vessel. mA3578w.3.non:ll>-081898 4 190
Fw"
' Ac .
l l l l l l \
- an og
' e ' s ad o s N N 5 H k k E l a M i I . m 4 i
- l Ee l sua Smut 4
4 E ! 5 i l l 1 m:U578w-3.non:tum209s 4-191 Rev.2 l' t
FINAL
- a,c m
at E as i n N Y b
!k k
E a 3 m 1a 2 i> N 4 9 e t E m:\3578w-3.non:lb-08209s 4-192 Rev.2
Fmrt r l ac l-m ! 8 i U j e a M N N b i I E
.e Wna E
U N l
- 8 E
e 1o U ko \ Z m 4 ,
)
9 v 8 s
.E f %
l L m:\3578w.3.non:Ib42098 4-193 Rev.2
'l1 F
I I Pa 5 6 0 C R n u R 2 2 2 2 t s e T , t s n e m e r u s ae M y t i c l o e V l a n r t e I n
. 4-4 1
4 e r u g i F I l I<. g e aG34dBi%n5
- Gu
FINAL a,c l I m b at a s a: ci e4 N N 5 H 2 8. H t I k I e m 4 4 2 E E i l mM578w-3.mulb-082098 4-195 Rev.2
FINAL a,c i m at E at et c4 N 1 P l 1w R. E H 3s E I 4 2 im E mus7sw 3.non:ims 4 196 Rev.2 I - - _ _ _
FINAL a,c i TABLE 4.141 TEST 222.2
SUMMARY
DATA RUN RC065A AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE OUTSIDE FLUID WALL AT INSIDE BAFFLE ('F) ('F) ('F) ('F) (*F) l l 1 I i l 1 l l I l nv\3578w.3.non:ltA81898 4 197
.j
FINAL a,c TABLE 4.14-1 (cont.) TEST 222.2
SUMMARY
DATA RUN RC065A AVERAGE TEST DATA m \3578w-3.non:lb-081808 4.} 9g
1 l FINAL ac TABLE 4.14 2 TEST 222.3
SUMMARY
DATA RUN RC065B AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE (*F) (*F) ('F) (*F) (*F) i i
.l 1
l m-A3578w 3.non:lb-081898 4 199
FINAL 3,C TABLE 4.14 2 (cont.) TEST 222.2 SU.MMARY DATA RUN RC065B AVERAGE TEST DATA ntuS7sw.3.non: b-081898 4-200 Rev.1
FINAL l a,c l TABLE 4.14-3 ! I VESSEL TEMPERATURE DISTRIBUTION FOR TEST 222.2, RC065 AVERAGE WALL MAXIMUM WALL MINIMUM WALL I TEMPERATURE TEMPERATURE TEMPERATURE ' INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) l l l ? l t : 1 I 1 1 ; l l 1 I i l 1 l 1 mA3578w 3 non:Ib-081898 4 201 Rev.I
FINAL 4.C TABLE 4.14-4 i VESSEL TEMPERATURE DISTRIBUTION FOR TEST 222.2, RC065B AVERAGE WALL MAXIMUM WALL TEMPERATURE TEMPERATURE MINIMUM WALL TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) i m:\3578w 3.non:Ib-081898 4-202 Rev.1
R l' T A) R RF H EC P 2 3 M L E I T O T
?
t i l WEc t D OTne O LAeh I FR( t R E P W E M N O I T O L I T F A W A M R A E T E S R t' S f A) U R H RF-S E( P R 7 8 M E 1 1 E T V O T E e T lf. l WE)ce OT A a D L AW e S O FR O N I t t E E P D E N 5N M I O 4 O I T T A 1 C C O 4 F L EO L BN E AO R t' TIT T A ) RF U R I EC B I 8 P I 0 M R I I E T T O S I T 5 I D 7 0 WEel 1 OThe L A h 5 D 6 O I FRt( 0 R C E P R E N M O N I T I T U C A R O L 2 2 2 E 2 R t' T T A S R RH E I I E( P T 5 7 - M G E I T O T 4 8 1 W E )e D OT se LAW O I FRO _ R E P _ E M N I O I T T A C O L l iE BG'a 7s t= 5& == bbOw t I l'l
FINAL LC TABLE 4.14-6 TEST 222.2 RUN RC065, INTERNAL VELOCITY TEST DATA STANDARD AVERAGE MAXIMUM MINIMUM DEVIATION LOCATION (ft/sec) (ft/sec) (ft/sec) (ft/sec) NOTES i nt\3578w-3.nortib-081898 4 204 Rev.I
FINAL a,c 1 TABLE 4.14 7 TEST 222.2, RUN RC065, DISTRIBUTION OF DRY STRIPS T AVERAGE DRY WIDTH TEST CONDITION cf ) I
)
\
l i f m:\3578w-3.norrib-081898 4-205 Rev.I
FINAL 4.15 Test 222.3 He initial transient steam flow to the test vessel with the steam discharge directed horizontally at the 5.8 foot elevation through a 3 in. diameter nozzle is displayed in Figure 4.15-1. The start of the transient is calculated from the data contained in Appendix A to approximately 5 seconds after the data set taken at 10.1356 hours. The mass flow transient was calculated from the vonex meter output together with the steam temperature and pressure at the flow meter. The steam meter pressure was calculated from the data available in the DAS output and the pressure history of the transient. The steam temperature was estimated from a linear regression of the DAS monitored steam temperature. The nominal values of pressure and temperature are indicated on Figure 4.15-1. The results for the low (RC064A) and high (RC064B) steam flow rate, steady state periods of Test 222.3 are tabulated in Tables 4.15-1 through 4.15-4. The steady state data was taken from the time periods 13.01 through 14.00 hours and 16.50 through 17.52 hours, respectively. The data presented is representative of approximately one hour of test operation. Tables 4.15-3 and 4.15-4 present a comparison of the average, minimum and maximum temperatures on the inside and outside vessel walls at each cross section of the vessel for each of the air flow conditions. Plots of the vessel pressure and steam flow (vortex meter) are shown in Figure 4.15-2. He comparison of the condensate and vonex steam flow measurements are- also illustrated in Figure 4.15-2. He steam flow as recorded by the vonex meter is somewhat erratic over the first steady state period but is essentially constant over the final period. The total condensate flow settles into a steady flow rate approximately 13 percent higher than the steam flow rate during the first steady state period and approximately 2 percent higher during the second steady state period. I Condensation collection during the steady state portion was switched to different collection tanks to determine the distribution of condensate within the vessel. Table 4.15-5 documents the distributed condensate flows during the steady state period. Erratic flows during the first three periods generate an 18 to 26 percent difference between the condensate and the average steam flow measurements. The condensate backed up into the test vessel during the third period. Review of the data indicates that approximately 56 and 58 percent of the condensate is generated on the vessel side wall during the last two steady state periods. The results of the non-condensible sampling are shown on Figure 4.15-3 at the four sampling locations (Dome-90*-63"-3", A-270*-6", E-90*-6"and F-0*-6"). The data shows almost complete mixing throughout the test vessel for this configuration. Review of the pressures recorded during sampling 1 indicates that the dome values differed from the values recorded at the other three locations and the i vessel pressure by an average of -4.3 percent throughout the test which would tend to raise the calculated air concentrations in the dome of the samples taken after 15 hours by I to 1.4 psi. l The internal velocity meter located at A-90*-1.5" provided output that indicated that the velocity was down along the sidewall throughout the test. The majority of outputs were on the order of the average l value shown in Table 4.15-6 with the peak velocity occurring during the initial steam transient with l mA3578w-4 non:Ib.081898 4-206 Rev.I j l
FINAL the nozzle pointed toward the wall at A-270*. The remainder of the internal velocity meters did not function throughout the test and are considered to have failed. Figure 4.15-4 presents a plot of the behavior of the internal velocity meters. t Water distribution around the circumference at the bottom of the baffle was taken after completion of the transient and after steady state was established. Table 4.15 7 summarizes the water distribution around the circumference of the vessel at each of the steady state conditions. Performance of the velocity meter (Channel 295) below the fan assembly is no longer providing reliable data. Use fan calibration data located in Section 2.2.7, equation 13 for an estimate of the outlet velocity based on the fan RPM. 'Ihe velocity noted in Tables 4.15-1 and 4.15-2 reflect these value.s. Figure 4.15-5 and 4.lf-6 provide an indication of the average temperature distribution as a function of level for the inside vessel wall and the fluid temperature approximately 1 inch inside the vessel. mA1578w4rmIb-08I898 4 207 Rev.I
FmAL
~
a,C e M s 3 n 16 b k k E 3 5 3 x
.5 i
S 4 I s
.5 m
mA3578w4.mit42098 4-208 Rev.2
lllIllI 'l ll m2g I l E 4 _ 6 0 C R n u _ R - 3 2 2 2 _ t s e T y r - o i t s _ H . w _ o l _ F - m _ a t e S _ d n - a e r u s s e r P l e s s e V 2-5 1 4 e r u g i F l l R9e[t=l .b8 oq
- to
FINAL a,c j sc E AC N n I H E 4 5 ie U M 1 E i 7 5 4 2 E E nr\3578w4norrib-os209s 4-210 Rev.2
I I b3E$= b!! f u$-
FLNAL a,C l O N E u N N h t a b I. E 5 ii W l> w m N 4 2 a 5: m:\3578w 4.non:lb-082098 4-212 Rev.2 I,
---n-------,-,
FINAL a,c U M c s M n N s t ibe a e b 2m b T L' 4 b
=
DC I i m-us7sw-4.non:ib.os209s 4 213 Rev.2 l l
FINAL I _ a,c TABLE 4.151 TEST 222.3
SUMMARY
DATA RUN RC064A AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE- OUTSIDE FLUID WALL AT BAFFLE ('F) ('F) (*F) (*F) ('F) m:\3578w4non:lb4)81898 4-214 Rev.I
FINAL a.c TABLE 4.15-1 (cont.) TEST 222.3
SUMMARY
DATA RUN RC064A AVERAGE TEST DATA f 1 ? l l l t l l 1 l l 1 l nt\3578w4non:lb-081898 4 215 Rev.1 l L______._______.__._____._.______ __ J
FLNAL a,c TABLE 4.15-2 TEST 222.3
SUMMARY
DATA RUN RC064B AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE OUTSIDE FLUID WALL AT INSIDE BAFFLE (*F) ('F) (*F) (*F) (*F) mA357tw-4.non:lb-081898 4 216 Rev.1
FINAL _ a,c TABLE 4.15 2 (cont.) TEST 222.3
SUMMARY
DATA RUN RC064B AVERAGE TEST DATA r l l l l l l l r ms37sw-4.rmet tb-081898 42]7 Rev.I l 1
FINAL a.c TABLE 4.15-3 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 223.1, RC064A AVERAGE WALL MAXIMUM WALL MLNIMUM WALL TEMPERATURE TEMPERATURE TEMPERATURE INSIDE OUTSIDE DELTA LNSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) mA3578w4non:Ib-081898 4 218 Rev.I
FINAL l _ a,c l ! TABLE 4.15-4 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 223.1, RC064B AVERAGE WALL MAXIMUM WALL TEMPERATURE TEMPERATURE MINIMUM WALL TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCAT10N (*F) (*F) ('F) (*F) (*F) (*F) (*F) (*F) (*F) l l l l 1. m:\3578*-4.non lb-081898 4 219 Rev.I
l1lt l Iil l 9 $t-I l E P)F R t M* E(
'l _
T 2 5 7 5 O T OT 0 0 5 WE)h LA FRc 1 D O I R E N3 P M E T _ M A I C T O. W E O L F P. ) M R MT E( H T A 9 E 4 0 T I S O T W E )r S 9_ OTe L Ah t U 2 1 FRit S D R ) M E R E N V P E O I E M T A T I T C O A L S N E D R P. ) MF 5N H E *( 5 O T 8 9 1 C 2 1 4 F O T W E )e EO L 5 7 Tu s O. A ld t 2 FRa BN 1 AO D O TIT I R E N U O P I B E T A I M C R T I O T L S I D R P. H MF) 4 E *( 6 M T 0 1 C 3 O R T WE' , 2 OT L N 9 LA FR C U 8 1 R D O
, I 3 R N E O 2 P IT 2 E A 2 M I
C T T O. I S E T P) R MF _ H E *( 3 T 4 n a 0 WE' 7 OT 4 t LA" FR "- s _ D . O t _ R N E _ ) P M E T A MI 'M T t. E
' I n&aaE 8n. .
e 5' bU)O tb * . .. lli!I>ll lll ,
FINAL. _ a,c TABLE 4.15-6 TEST 222.3 RUN RC064, INTERNAL VELOCITY TEST DATA STANDARD AVERAGE MAXIMUM MINIMUM DEVIATION LOCATION (ft/sec) (ft/sec) (ft/sec) (ft/sec) NOTES l nt\3578w-4 non:I M 81898 4 221 Rev.I
FINAL _ 3,C TABLE 4.15-7 TEST 222.3, RUN RC064, DISTRIBUTION OF DRY STRIPS WET AVERAGE DRY WIDTH TEST CONDITION (%) (in) m:uS78w-4.non:Ib-os1898 4-222 Rev.1
FINAL. 4.16 Test 222.4 The initial transient steam flow to the test vessel with the discharge directed upward through a 3 in. diameter nozzle is displayed in Figure 4.16-1. The start of the transient is back calculated from the l data contained in Appendix D to 10.8975 hours or about I second before the first transient data set. The mass flow transient was calculated from the vortex meter output together with the steam i ! temperature and pressure at the flow meter. The steam line pressure at the flow meter was calculated from the data available in the DAS output and the pressure history of the transient. The steam temperature was estimated from a linear regression of the DAS monitored steam temperature. The nominal values of pressure and temperature are indicated on Figure 4.16-1. The results for the low (RC066A) and high (RC066B) steam flow rate, steady state periods of Test 222.4 are tabulated in Tables 4.16-1 through 4.16-4. The steady state data was taken from the time periods 12.25 through 13.25 hours and 15.75 through 16.77 hours, respectively. The data presented is representative of approximately one hour of test operation. Tables 4.16-3 and 4.16-4 present a comparison of the average, minimum and maximum temperatures on the inside and outside vessel walls at each cross section of the vessel for each of the air flow conditions. Plots of the vessel pressure and steam flow (vortex meter) are shown in Figure 4.16-2. The comparison of the condensate and vortex steam flow measurements are also illustrated in Figure 4.16-2. The total l condensate flow settles into a steady flow rate approximately 4 percent higher than the vortex steam flow rate during the first period anil approximately 3 percent higher during the second. Condensation collection during the steady state portion was switched to different collection tanks to l -determine the distribution of condensate within the vessel. Table 4.16-6 documents the distributed condensate flows during the steady state period. The condensate backed up into the test vessel during the third period and appears to have overflowed into the other condensate system as evidenced by the low condensate collection rate in the early portion of the third condensate collection period flowed by an increased collection period. Review of the distributed condensate data indicates an inconsistency in the condensate distribution. Although the total condensate collection agrees well with the steam flow, the specific distribution to the dome and side wall during the first two collection periods do not produce consistent results, i.e., total to 118 percent. It is recommend that this condensate distribution data be used with caution. The results of the non-condensible sampling are shown on Figure 4.16-3 at the four sampling locations (Dome-90*-63"-3", A-270*-6", E-90*-6"and F-0*-6"). The data shows that the dome tends to have a l smaller concentration of air than the remainder of the vessel. All the pressure transducers of the l sampling system were in agreement with the vessel and each other within 0.3 psi. The internal velocity meter located at A-90*-1.5" provided output that indicated that the velocity was down along the sidewall throughout the test. The majority of outputs were on the order of the average l value shown in Table 4.16-5 with the peak velocity occurring during the initial steam transient with the nozzle pointed directly upward. The remainder of the intemal velocity meters did not function 1 mA357sw-4.non:ib-osis9s 4-223 Rev.I
l 1 FINAL. throughout the test and are considered to have failed. Figure 4.16-4 presents a plot of the behavior of the intemal velocity meters. Water distribution around the circumference at the bottom of the baffle was taken after completion of the transient and after steady state was established. Table 4.16-7 summarizes the water distribution around the circumference of the vessel at each of the steady state conditions. Performance of the velocity meter (Channel 295) below the fan assembly is no longer providing reliable data. Use fan calibration data located in Section 2.2.7, equation 13 for an estimate of the outlet velocity based on the fan RPM. The velocity noted in Tables 4.16-1 and 4.16-2 reflect these values. Figures 4.16-5 and 4.16-6 provide an indication of the average temperature distribution as a function of level for the inside vessel wall and the fluid temperature approximately 1 inch inside the vessel. i m:\3578w-4.non:Ib.o81898 4 224
FINAL
~
a,c l 1-l l l i b U l 8 i e 4 3 x 4 e4 m : N I w 0 , b ! k k E a m
.a.
.11 m
a== see 4 4 8 3 P in 1 1 1 1 l 1 1 m:us78w-4.noitib os209s 4 225 Rev.2 l
FINAL a,c l N E N 4 d N D o 2 m k k E in 1a 2 i> N 4 a. b oc E m:uS7swa.non: b-os209s 4-226 Rev.2
,_-_-m.- --_--. _ _ - . _ . - - - - . - - - . . ---
FmAL
' - a,c l
l I at e s as 4-e4 N N l 5 H E
.2 E
lio
\
h U
.2 e
1 Ie Z m 4 4 2 l
& I E i i
i 1 l l 1 mme l l l- m:U578w-4.nortIb482098 4-227 Rev.2 I L _ _ _ _ _ _ _ - - - _ - _ _ _ _ _ _ _ _ _ _ ~
FINAL a,c M i a k N h ia Ie I
=.>
a E s I E m:us7 w 4.non: b os209s 4-228 Rev.2
i FINAL j- - i- - a,c 1 1 I 1
)
i i j M i
- a
' s M 4 ei l N 1 N 2 t a. 8 I. J f E 5
=
a l w
. en 4
4 2 5 E l l i. m:0578w-4.non:lb-082098 - Rev.2
~
4-229
FINAL a,c N s a 4 e4 N h i s a k i H 2 3 4 2 l m:us7sw-4.noiutb-os209s 4-230 Rev.2
FINAL i _ a,c TABLE 4.161 TEST 222.4
SUMMARY
DATA l RUN RC066A AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE (*F) ('F) (*F) ('F) ('F) l l l l l l m:\3578w-3.non:lM)81898 4-231
FINAL a,c TABLE 4.16-1 (cont.) TEST 222.4 SLLIMARY DATA RUN RC066A AVERAGE TEST DATA m:\3578w-3mn:Ib-081898 4 232
l FINAL _ a,c TABLE 4.16-2 TEST 222.4
SUMMARY
DATA RUN RC066B AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE ('F) (*F) ('F) ('F) ('F) l l l l m:\3578w-3.non:Ib-081898 4 233
l FINAL _ 8,C l TABLE 4.16 2 (cont.) TEST 222.4
SUMMARY
DATA RUN RC066B AVERAGE TEST DATA
- ntuS78w-4.non:ib-osis9s 4 234 Rev 1
i FINAL l l l _ 3,C t TABLE 4.16 3 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 222.4, RC066A AVERAGE WALL MAXIMUM WALL MINIMUM WALL TEMPERATURE TEMPERATURE TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION ('F) ('F) (*F) (*F) ('F) (*F) (*F) (* F) ('F) l l l l l l l l i m:\3578w 3.non:lb-081898 4-235
FINAL a,c TABLE 4.164 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 222.4, RC066B AVERAGE WALL MAXLMUM WALL MINIMUM WALL TEMPERATURE TEMPERATURE TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION ('F) (*F) (*F) ('F) (*F) (*F) (*D (*F) ('F) mA3578w.3.non:Ib-08I898 4 236
l FINAL _ ac TABLE 4.16-5 TEST 222.4 RUN RC066, INTERNAL VELOCITY TEST DATA STANDARD AVERAGE MAXIMUM MINIMUM DEVIATION LOCATION (ft/sec) (ft/sec) (ft/sec) (ft/sec) NOTES l l l l. I i I 1 l l l i l mM578w-4.non:Ib-081898 4 237 Rev.1 L______.-______.__.__---___. _ _ _ _ _ - - - - . _ - _ . . -- --- .-
l i I i1 1Ill1! - l 1!, ! i2>r I I eo P R M) E T H T( 8 7 1 0 7 8 WE' 5 4 OT LA' I D FR-O I R E N P E O I M T I A T C O L W O L P F R M)T E H T( M 0 A 5 1 E O T T WEcte S 5 7 OTe LAW S 4 I FR( I U D O S I R R E N E P O I V E M T A E I C - T O T L A S N P. E R H MT) E( D 5 T 6N 5 t 6 O 1 O 1 C T WE" OT 4 F 7 9 LA". ^ EO L 1 1 D F'R-BN O I AO I R E N 3 TT P E H T U M A C B I T O I L R T S I P MFD D R H E* T( 5 6 2 6 1 3 0 C O T WEcte OTe R 2 4 LAW _ FR( I N 2 1 U D O R I R N _
, E O _
4 P I . E T 2 A 2 M I C 2 T O _ L T _ S E . T R P MF ) H E* 2 T( 4 L I O WE" T OT - 5 LA J 2 1 FRT: 1 D O I R N E O P I T E A M I C T O L I I nc$IbI= a& U= ._
FINat. _ a,c TABLE 4.16-7 TEST 222.4, RUN RC066, DISTRIBUTION OF DRY STRIPS WET AVERAGE DRY WIDTH TEST CONDITION (%) (in) l l l l l l l l [ mA3578w 3.non:lt>081898 4 239 l e-________-_.
1 i i FINAL. l l l 1 1 4.17 Test 223.1 The constant flow test reported herein was conducted by initially providing a low steam flow of approximately 0.25 lb/see to the test vessel under maximum attainable vacuum condition. The steam flow rate was then increased to approximately 1.5 lb/sec for the remainder of the test until the vessel arrived at a constant pressure with the air cooling fan on and with water cooling to the vessel set at a predetermined level. The extent of water coverage on the vessel was measured during the steady state periods and gas sampling was performed to determine the concentration of noncondensibles. For the test 223.1 the insulation was removed from the bottom of the vessel below the open and deadend compartment areas; insulation was left in place under the steam generator compartment. The results for the steady state period of Test 223.1 (RC069) are tabulated in Table 4.17-1 and 4.17-2 and are representative of approximately one hour of test operation. Table 4.17-2 provides a I comparison of the average, maximum and minimum temperatures on the inside and outside vessel l walls. Also included are the maximum, minimum and average differential temperatures for the same locations.The steady state data was taken from the time periods 12.06 through 13.04 hours. Plots of the vessel pressure and steam flow (Gilflo and condensate) are shown in Figure 4.17-1. Review of the vortex meter data indicates that its outputs are beyond the linear range of the associated amplifier, i.e.
) 630 mv, and therefore are not plotted and should not be considered as valid test data. The l
l condensate flow settles into a steady flow rate approximately 6 percent higher than the average Gilflo steam flow rate. f The initial pressure of the vessel was measured at 0.00 psia by the pressure transducer mounted on the sampling apparatus at A-270*. The indicated vessel pressures were determined to be an average of 1.9 psi higher than the manual data recorded during extraction of the noncondensible samples at approximately 23 psia. The results of the non-condensible sampling are shown on Figure 4.17-2 at the four sampling locations (Dome-90*-63"-3", A-270*-6", E-90*-6"and F-0*-6"). The data shows that the air tends to concentrate l below the steam injection point in the heel of the vessel. l No internal velocity meters were active during this test. The annulus velocity meter appears to be l functioning again with reasonable values but performance during the previously reported test (RC066) indicate erratic performance. It is recommended that the fan calibration located in Section 2.2.7 (equation 13) be used for an estimate of the outlet velocity based on the fan PfM. The velocity noted in Table 4.17-1 reflects this value. Water distribution around the circumference at the bottom of the baffle was taken after completion of the transient and after steady state was established. Table 4.17-3 summarizes the water distribution around the circumference of the vessel at each of the steady state conditions. Figure 4.17-3 and 4.17-4 provide an indication of the average temperature distribution as a function of level for the inside vessel wall and the fluid temperature approximately 1 inch inside the vessel. m \3578w.3.non:Ib-081898 4 240
FINAL a,C . l l-l e
.as s
a as 4 N N l I F 8 3
- n k
k E a 3 m 1a E I a. i r- i m i 4 1 2 m os iZ ! 1 l muS7sw-4.mnib-osis9s 4-241 Rev.1
FINAL a,C e 8 u N s 3 M a N N e E
.2 li A',
a V i
.2
.C 4s C
k e Z U \ C 4 0 3
.5
""~ ~ l m:\3578w4.non:Ib-081898 4-242
l
)
FINAL a,c e M E 3 K
~
4 N . N \ b h a K E F
=a N
1 w 9 t-m A 3 BC E l m'0578w-4mn:lb42098 4-243 Rev.2
FINAL a,c ch M c 3 M E N N i H a 8. E e b 2s E Y t-m 4 N
=
E j la. l l I l l l
)
m \3578w.4.non:1b-082098 4-244 Rev.2
FINAL _ 3,C TABLE 4.171 TEST 223.1
SUMMARY
DATA RUN RC069 AVERAGE TEST DATA j. WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE ) (*F) ('F) (*F) ('F) (*F) i l l l 1 l _ m:uS78w-4.non:lb 081898 4 245 Rev.1
FINAL _ a,c TABLE 4.171 (cont.) TEST 223.1
SUMMARY
DATA RUN RCM9 AVERAGE TEST DATA m:u578w-4.non:1ba1898 4 246 Rev.1 i
FINAL l
- - a,c TABLE 4.17 2 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 223.1, RUN RC069 l AVERAGE WALL MAXLMUM WALL MINDIUM WALL TEMPERATURE TEMPERATURE TEMPERATURE INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA INSIDE OUTSIDE DELTA LOCATION (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F) (*F)
I i l l mA3578w.4.non.ib-osis98 4-247 Rev.1 l
FINAL _ a,c TABLE 4.17-3 TEST 223.1, RUN RC069, DISTRIBUTION OF DRY STRIPS WET AVERAGE DRY WIDT.H TEST CONDITION (%) (in) m\3578w-4.non:lb-081898 4-248
\ , FINAL 4.18 Test Results 224.1 The flow tests reponed herein were conducted by providing a constant flow of steam to a vessel initially pressurized with 2 atmospheres of air. Test 224.1 was conducted with a steam flow of approximately 0.25 lb/sec until the vessel arrived at a constant pressure with the air cooling fan on and with water cooling to the vessel set at a predetermined level. The extent of water coverage on the vessel was measured during the steady state periods and gas sampling was performed to determine the concentration of noncondensibles. The bottom of the test of the vessel below the open and deadend compartment areas remained uninsulated; insulation under the steam generator compartment was left in place. The results for the steady state period of Test 224.1 (RC067) are tabulated in Table 4.18-1. The steady state data was taken from the time periods 14.17 through 15.17 hours. Table 4.18-2 provides a comparison of the average, maximum and minimum temperatures on the inside and outside vessel j walls. Also included are the maximum, minimum -d average differential temperatures for the same locations. The data presented are representative of approximately one hour of test operation; plots of the vessel pressure and steam flow (Vonex, Gilflo and condensate) are shown in Figure 4.18-1. The condensate flow to condensate tank I appears to be somewhat erratic with relatively high values occasionally indicating some holdup. The vonex meter is providing indicated flows within 4.5 percent of the condensate flows. The results of the non-condensible sampling are shown on Figure 4.18-2 at the four sampling locations (Dome-90*-63"-3", A-270*-6", E-90*-6"and F-0*-6"). The data shows that the air tends to concentrate below the steam injection point in the heel of the vessel. The sampling apparatus thermocouple measuring the sample fluid temperature at E-90* failed during the test and the fluid temperature of an average of the fluid thermocouple at the E cross section at the equivalent times were substituted for calculation of the air concentration. No internal velocity meters were active during this test. The annulus velocity meter is considered to have failed. The velocity reponed in Table 4.18-1 relfects this value. Water distribution around the circumference at the bottom of the baffle was maintained at a 100 percent coverage level throughout the test. Figure 4.18-3 and 4.18-4 provide an indication of the average temperature distribution as a function of level for the inside vessel wall and the fluid temperature approximately 1 inch inside the vessel. i I ( mus78w-4.non:ib-osis9s 4-249
FINAL
- l a,C I
b M c s K N N ' b b t'O 5 x k k E E le E I e 4 E fe E
~~ _
f
. nt\3578* 3.non:IbO81898 4-250
- l. FmA1, l
l _ a,C l l I l i l I l l e-3 V M i s a M J N N I
.2 li 3
a o O , 2 !
.c \
"E G
3o I o Z 7 oc w A E
= ,
E i m:\3578w-3.non:1b-082098 4 251
FINAL _ a,c l tw aC a s at J b N I H h a li. n E E e H
==
a 3 1 e m ob i E o
.E m
l J mA3578w-3mIb-082098 4-252 _ _. __ =. - _ .a
FINAL
-a,c f
l 1 1
-l t
i i l 1 I l 8 u 3 m 3 M l i v N N w I su 3 A 6 se b 3s E 7 ee i v b M
.E b
I mA3578w-3.non:1b-082@8 4 253 o____..___..__ __
FINAL a,C TABLE 4.181 TEST 224.1
SUMMARY
DATA RUN RC067 AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL WALL INSIDE INSIDE OUTSIDE FLUID AT BAFFLE ('F) (*F) ('F) (*F) ('F) mM578w 3.non:Ib-081898 4 254
FINAL
- a,c TABLE 4.181 (cont)
TEST 224.1
SUMMARY
DATA RUN RC067 AVERAGE TEST DATA i l l I 1 1 i muS78w 3.non:Ib-osts9s 4 255
FINAL
*4 a,c TABLE 4.18 2 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 224.1, RUN RC067 AVERAGE WALL MAXIMUM WALL MINIMUM WALL TEMPERATURE TEMPERATURE TEMPERATURE INSIDE OL7s DE DELTA INSIDE OLTSIDE DELTA INSIDE OUT$tDE DELTA LOCATION en en en en en en en en en e
i 1 m:\3578w 3.non:lb-081898 4-256
FINAL l l 1 4.19 Test Results 224.2 The flow tests reported herein were conducted by providing a constant flow of steam to a vessel I initially pressurized with 2 atmospheres of air. Test 224.2 was conducted with a steam flow of 0.5 lb/sec until the vessel arrived at a constant pressure with the air cooling fan on and with water cooling to the vessel set at a predetermined level. The extent of water coverage on the vessel was measured during the steady state periods and gas sampling was performed to determine the concentration of noncondensibles. The insulation was removed from the bottom of the vessel below the open and deadend compartment areas; insulation was left in place under the steam generator compartment. The results for the steady state period of Test 224.2 (RC068) are tabulated in Table 4.19-l. The steady state data was taken from the time periods 13.39 through 14.39 hours. Table 4.19-2 provides a comparison of the average, maximum and minimum temperatures on the inside and outside vessel walls. Also included are the maximum, minimum and average differential temperatures for the same locations. The data presented is representative of approximately one hour of test operation; plots of l the vessel pressure and steam flow (vortex, Gilflo and condensate) are shown in Figure 4.19-1. I Review of the vortex meter data indicates that its outputs are approximately 0.1 percent higher than the average condensate flow. The average condensate flow is approximately 16 percent higher than l the average Gilflo steam flow rate over the majority of the test. I The indicated vessel pressures were determined to be an average of 0.4 psi higher than the manual data recorded during extraction of the noncondensible samples at approximately 56 psia; no pressure corrections were performed on the conversion of the vessel pressure. The results of the non-condensible sampling are shown on Figure 4.19-2 at the four sampling locations (Dome-90*-63"-3", A-270*-6", E-90 -6"and F-0*-6"). The data shows that the air tends to concentrate below the steam injection point in the heel of the vessel. No internal velocity meters were active during this test. The annulus velocity meter is considered to have failed. The fan calibration correlation located in Section 2.2.2 (equation 13) should be used to estimate of the outlet velocity based on the fan RPM. The velocity reported in Table 4.19-1 reflects this value. Water distribution around the circumference at the bottom of the baffle was maintained at close to 100 percent coverage level throughout the test (Table 4.19-3). After 265 minutes two strips approximately 1.5 in. wide and approximately 6 ft. long were observed on the test vessel around the 210' location. l Figure 4.19-3 and 4.19-4 provide an indication of the average temperature distribution as a function of level for the inside vessel wall and the fluid temperature approximately 1 inch inside the vessel. m:us78.-4.non:ib-081898 4-257 Rev.I
i FINAL _a,C l O at E a: i 3N h e
!k f
a a re 1 k 1 7' S 4
'I is:
I
- nt\3578w-4.non:ltmo98 - 4-258 Rev.2 1
FINAL - a,c I U at a s as 6 2 N E
.2 li he a
O
.1t
.o 1
1 Z 4 2 4 2 s
.P Ene i
l l l 1 g i i nt\3578w-4.non:lbM2098 4 259 Rev.2 u________---__ __. _-.
FINAL a,c U M e s i 2 N I H Y 3 lL E 5 ii k 1 e 1_. 7 2 4 2 E I l rix\3578w-4.non:Ib 082098 4 260 Rev.2 i
FmAL
- a,e l
l i
- l 3
U u a m x
-A {
N so C H I u 5 h 2s E 7 e 9 n E m u E l t i 1 I l 1 1
- j. m-\357s*-4.non: b-os209s 4- M 2 i.
L-__ -_--_ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ . _ _ _ _ _ _ _ _ . _ _ _ _ _ _ _ _ _ _
FINAL a.c TABLE 4.19-1 TEST 224.2
SUMMARY
DATA RUN RC06J AVERAGE TEST DATA WALL TEMPERATURES TEMPERATURES INTERNAL INSIDE INSIDE OUTSIDE FLUID WALL AT BAFFLE (*F) (*F) (*F) ('F) (*F) m:\3578w.4.non:lb-081898 4 262
l FLNAL l l l i TABLE 4.191 (cont.) TEST 224.2
SUMMARY
DATA RUN RC068 AVERAGE TEST DATA I l l l m11578w-4.non:Ib-081898 4-263
FINAL ( _ _ ac TABLE 4.19 2 VESSEL TEMPERATURE DISTRIBUTION FOR TEST 224.2, RUN RC068 AVERAGE WALL MAXIMUM WALL MINIMUM WALL TEMPERATURE TEMPERATURE TEMPERATURE INSIDE oL7s DE DELTA INSIDE OLTSIDE DELTA INSIDE OLT51DE DELTA LOCATION rn en en en en en en en en e m\3578w4non:lb-081898 4-2 M
FINAL I l
- _ a,C TABLE 4.19 3 TEST 224.2, RUN RC068, DISTRIBUTION OF DRY STRIPS WET AVEF AGE DRY WIDTH TEST CONDITION (%) (in) l 1
1 l m:0578w 8.r.on:lb-081898 4 265 l
FINAL
5.0 CONCLUSION
S The tests reported herein were considered acceptable since the test objectives and the criteria of Section 3.3.1 were met. Assessment of the heat balances of the tests shown in Figure 3.3-1 indicate that the tests performed in a consistent fashion and that the overall behavior is repeatable, j Velocities within the test vessel were measured at five different locations. The sensor outputs support a consistent downward velocity along the vertical wall of the test vessel which was apparent in almost all of the tests. Sensors located in the dome were not as consistent but in general showed that the l velocities were upward along the surface of the vessel dome. The maximum sustained internal l velocities were approximately 5 ft/sec. i L Distribution of noncondensibles within the test vessel showed that an air-rich mixture collected below the operating deck and below the height of the steam inlet with relatively low velocity steam injection. Increasing the inlet velocity caused the noncondensible concentration to become even throughout.
- . He injection of light noncondensibles showed an initial concentrating effect in the top of the vessel during helium injection followed by a rapid (3 to 4 hours) redistribution to uniform concentration throughout the vessel. _ De light noncondensible testing was all conducted at relatively low steam
, injection velocities but the effect of higher velocity steam injections can be assumed to speed the redistribution of helium, i j m:\3578-5w.non:lt481898 5-1 (
FINA1.
6.0 REFERENCES
6.1 " Quick Look Report for Large Scale PCCS Tests 202.3 and 203.3," AP600 Doc. PCS-T2R-014, Rev. O, September 1993. 6.2 " Quick Look Report for Large Scale PCCS Tests 212.1 and 213.1," AP600 Doc. PCS-T2R-015, Rev.1, October 1993. 6.3 " Quick Look Repon for Large Scale PCCS Tests 214.1 and 215.1," AP600 Doc. PCS-T2R-l 017, Rev. O, October 1993. ' 6.4 " Quick Look Report for Large Scale PCCS Test 216.1," AP600 Doc. PCS-T2R-021, Rev. O, January 1994. 6.5 " Quick Look Report for Large Scale PCCS Tests 217.1 and 218.1," AP600 Doc. PCS-T2R-018, Rev. O, November 1993. 6.6 " Quick Look Repon for Large Scale PCCS Test 219.1," AP600 Doc. PCS T2R-022, Rev. O, January 1994. 6.7 " Quick Look Report for PCCS Large Scale Phase 2 Tests - Blind Test 220.1," AP600 Doc. PCS-T2R-020, Rev. O, December 1993. 6.8 " Quick Look Repon for Large Scale PCCS Test 221.1," AP600 Doc. PCS-T2R-023, Rev. O, February 1994. 6.9 " Quick Look Report for Large Scale PCCS Test 221.1," AP600 Doc. PCS T2R-024, Rev. O, March 1994. 6.10 " Quick Look Report for Large Scale PCCS Tests 222.2,222.3 & 222.4," AP600 Doc. PCS-T2R-026, Rev. O, April 1994. 6.11 " Quick Look Report for Large Scale PCCS Test 223.1," AP600 Doc. PCS-T2R-028, Rev. O, May 1994. 6.12 Quick Look Report for Large Scale PCCS Tests 224.1 & 224.2," AP600 Doc. PCS-T2R-029, Rev,0, May 1994. i 6.13 "AP6001/8th Large Scale Passive Containment Cooling System Heat Transfer Test Baseline Data Report," AP600 Doc. #PCS-T2R-003 Rev.1, WCAP-13566, October 1992. I rnA3578-5w.non:lt481898 6-1
FINAL 6.14 " Tests of Heat Transfer and Water Film Evaporation on a Heated Plate Simulating Cooling of the AP600 Reactor Containment," WCAP-12665 Rev. 01,4/24/92. 6.15 "PCS Water Distribution Test Film *Ihickness/ Percent Coverage," AP600 Doc. PCS-T2C-002, Rev. O, 4/6/92. 6.16 " Integral Containment Cooling Test Extension - Test Specification, Rev. 0," WCAP-13315, Rev. O, AP600 Doc. PCS-TIP-003, Rev. O. i 6.17 " Test Specification: Large Scale Passive Containment Cooling Test," AP600 Doc.
#PCS-TIP-002 Rev.1, WCAP-13107, December 1991.
6.18 " Passive Containment Cooling System Wind Tunnel Test Specification, Rev. 0," WCAP-13294, Rev. O, AP600 Doc. PCS-TlP-004, Rev. O. 4 1 6.19 " Tests of Air Flow for Cooling the AP600 Reactor Containment, Rev. 0," WCAP-13328, AP600 Doc. PCS-T2R-010, Rev. O. 1 aL\3578 5w.non:lb-081898 62
~
FINAL l i r l l-t i l l l l l l I I I APPENDIX A FACILITY DRAWINGS l m:us7sw.non:ib.osis9s A-1
FLNAL l
- ~, Q \
Appendix A contains facility drawings of the PCS Test Pressure Vessel "As Built" Condition (Drawing # 202 E3 Rev. 2, Sheets 1-12 of 12). m \3578w.non:1b-082098 A-2
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- FLNAL i
l APPENDIX B L
- SAMPLING APPARATUS I
i l l mA3578w.non:ll>osts9s g,3
FINAL I -1.0 PURPOSE ne original air in the containment mixes with steam released from the primary system and inhibits condensation on the cooled containment dome and walls. Diffusion of steam through air at the wall controls heat transfer by condensation. The larger the partial pressure of air in any region, the lower will be the condensation rate. But, if air, the denser component, concentrates near the bottom of the containment vessel by the continuous rectification processes, upper regions will have higher heat transfer rates. Den the cooled portion of the containment may have a higher overall thermal conductance and a lower pressure for a given steaming or heat release rate. Measuring the partial pressure of air at various locations in the model will show the distributions that result and this enables validation of condensation correlations, air redistribution and overall heat transfer analysis in containment computer codes. Hydrogen released during a late period in a postulated severe reactor accident will accompany steam released from the primary system into the containment. That too will mix with air to form a possibly combustible mixture. Helium, a gas whose difference in density from that of air is nearly the same as for hydrogen, is injected with steam to model the transient conditions in the containment. To find the- - likelihood and type of combustion, the helium-air mixture partial pressure and fraction of helium are measured at various locations in the containment model. mA3578w b.noo:lb-o81898 B-2
FINAL l l l 2.0 PRINCIPLES OF MEASUREMENT i , Samples of air-steam mixtures may be withdrawn into a sample cylinder taking care not to allow l steam to condense as it is withdrawn nor before closing the sample volume with a valve. Next the j steam in the sample cylinder may be condensed which assures that what remains as vapor is saturated. l A pressure gauge connected to the sample cylinder is used to measure the pressure of the hot sample before closing the volume, p3, and after cooling the volume and condensing steam, p2. The pressure, pg, after flow into the sample volume has stopped is the same as the containment pressure, po. A thermocouple in the sample volume is used to measure the temperature of the hot sample before closing the valve and after equilibrium has been established with the sample cylinder by heat transfer, and at equilibrium after the sample is cooled and steam is condensed. When steam is condensed to liquid, the volume of vapor int he sample cylinder is reduced slightly from V to V 2 by the volume of liquid condensed. If all the steam is condensed, the pressure in the sample cylinder would decrease to the partial pressure of air in the containment vessel times the ratio of absolute temperature (T 2 /II ), and of the vapor volumes, VN ). 2 But with a residual steam vapor pressure, the measured pressure p2 *ill be increased by the steam saturation pressure at T .2 Psat. steam (T 2 ). That is: p2 = (T /f2 )(VN i ) Pair,o 2 + Psat. steam (T2 ) (1) I The partial pressure of air in the containment, which is the same in the sampling cylinder at first, from equation (1) is: pair.o = (T 1 /I )(V 2 N)(P2 2 - Psat. steam (T2 )) (2) The ratio V 2N is very nearly equal to one because the specific volume of liquid is so low compared with that of the vapor. For example, if steam vapor pressure in the sample is 20 psia and temperature is 300*F (T i) and T 2is 70*F, the ratio V N2 is 0.9993, a 0.07% reduction from unity. Pressures can be measured to 1 psi,1% or more. Therefore the uncertainty of pressure is greater than an error by assuming V2 N is unity. 'Ihis is always true for any containment test conditions. If the sample in the vessel contains wet steam and the sampling system superheats it, the steam vapor fraction of the mixture will be increased somewhat, lowering the measured partial pressure of air below the value in the containment. Whether the steam is saturated or not can be determined by measuring the temperature, To, in the containment. After measuring the air partial pressure, p,;,,o, if the steam partial pressure that is inferred, po - p,ir,o is less than or equal to the saturation pressure corresponding to To, the steam is dry. If it is more, then steam is wet and a correction may be necessary. But there is sufficient measured information to make the correction and find the wet steam quality because it depends on how far above the saturation pressure, the inferred vapor pressure is. The actual partial pressure of steam is in fact simply found, the partial pressure of vapor is the j~ saturation pressure and the air partial pressure is yo - psat. steam (T o ). The usefulness of sampling then is to determine that P o- p,;,,o from sampling measurements is less than psat. steam (To ) so that the steam l must have been wet. i mA357sw-b.non:ib-osis98 B-3
)
. .I
FINA1. When the sample contains steam, air and helium, the sum of the partial pressures of the non-condensables, air and helium, is found in the same way as has been described for air alone. Samples of those can then be analyzed by mass spectrometers to find the partial pressure ratio of helium to air. m:\3578w b.non:lb-081898 B-4
I FINA1. l 3.0 SAMPLING AND MEASUREMENT SYSTEM DESIGN REQUIREMENTS i ne first requirement for measuring air partial pressure is that steam must not condense in the sampline lines. If it did then the sampling cylinder would be filled with more air than normal. For example, if all the steam condense before reaching the sampling cylinder, the partial pressure of air would appear to be the containment pressure. He second requirement is that steam not condense in the sampling cylinder before the filled pressure is read and the volume closed by a valve. That can only be assured by heating the sampling line and cylinder walls above the saturation temperature, l which is 324 F for 95 psia (80 psig) steam in the containment and no air. Volumes that cannot be heated, such as in the pressure gauge must be kept negligibly small and isolated so as not to affect the sampling cylinder contents or else one must be able to measure the temperature in such volumes and calculate the effect of condensation in the isolated volume. A third requirement is that the sample be fresh, that is, the sample lines and cylidner must bepurged of gas' and vapor that was taken from another place or at another time. i After the non-condensable gases' pressure is measured, separate samples to find the component partial pressure ratios, can be drawn without concern for condensing. It is even advantageous to have a high pressure of non-condensable samples because the sample cylinders will be at containment pressure, above atmospheric pressure; and sample gas can only leak out while stored for analysis, preserving the ratios in the sample. l i m:uS78. Anon:1b-os1898 B-5
FINAL i 4.0 SYSTEM DESIGN An assembly view of the system is titled "Large Scale PCCS Test, Partial P of Air and He in Air Probe, Sampling and Measurement System." The probe and sampling system may be moved to any one of six penetrations on the containment model upper head, twenty on the side wall or two on the lower head. Each one used has a heavy wall carrier tube fastened to a fitting on the vessel, a ball valve outside the air baffle wall and a fitting that seals the probe. The probe slides into the seal, then after the ball valve is opened, through the carrier tube into the containment vessel. Its position can be at the wall or anywhere else, up to four feet inside. An extension may be added that extends the probe to the center of the vessel, seven and one-half feet inside. At 80 psig vessel pressure, the maximum force on the probe, which may only be held by the seal friction, is 12 pounds. The probe sample tube (0.25 OD) is thermally insulated from the probe shield tube (0.3675 ID) by an air gap,0.059 inch wide. The conductance through air is 0.34 Btu /h*F per foot and by radiation is 0.07 Btu /h*F per foot of probe. This is intended to be the primary insulation. The conductance of the ; shielded sample tube to ambient is estaimated to be 0.25 Btu /h*F per foot through the carrier tube and 0.30 Btu /h F per foot outside in free air. A sheathed electrical heater inside the sample tube heats it continuously and heats sample gases and vapors when they flow. To maintain a temperature near 400*F, the 675 W heater (at 240 volts) is energized only at 120 volts (one quarter full power). The 400 F temperature is when the probe is outside the carrier tube; inside it may be 65 F warmer. These temperature provide a substantial superheating for steam so that it will not become saturated in contact with less directly heated portions in the sampling system path. The probe tube length inside the containment vessel is also heated. 'Ihere the temperature may be as much as 300*F above the air and steam temperature or approximately 600*F. The heater occupies approximately 50% of the cross - sectional area inside the probe tube. This flow area has been satisfactory in prior designs but the hydraulic diameter,0.055 ine'a, is less than that of the prior designs,0.125 inch. The increased flow resistance does not adversely affect operation. The heater may rest on the probe tube. Thermocouple, sheathed chromel-alumel (type K), 0.030 inch diameter are led through the 0.059 inch air gap between the probe tube and shield tube. TCl is led thorugh the seal plug at the end of the probe, and is brazed in place one-eighth of an inch beyond the probe tube inlet to measure the sample vapor and air temperature. To. TC2 is held against the sample tube uder a centering wrap of teflon tape,30 inches from the inlet end and TC3 is similarly fastened 60 inches from the inlet. These thermocouple verify that the probe tube is above the saturation temperature for steam, especially at
' the outer end where thermal conductance to a cool ambient is largest. They may also aid in making adjustments to the heater energizing voltage to change the probe tube temperature.
The probe and shield tube assembly can withstand a maximum bending moment of 165 inch-pounds. The sampling system may weigh as much as fifteen pounds so the cantilevered length cannot be longer than eleven inches. A support for the probe is needed. A 1-1/4 x l-1/4 x 1/8,6061-T6 aluminum angle with the corner down can support a 1544 inch-pound bending moment, more than adequate for supporting the probe and sampling system when the probe is completely withdrawn. It may be fastened below the ball valve and clamped with 5/8 inch wide "U" bolts to the 5/8 inch m:\3578w-b.nonM81898 B-6
I FINAL, I-diameter carrier tube at each end of the valve. The carrier tube can withstand only 625 inch-pounds of bending moment. This is marginal for supporting a withdrawn probe and deflection is excessive so additional support is needed for the aluminum angle " tray". He sampling system has a cross with toggle valves to interconnect the probe tube through valve Vi , l the purge cylinder and helium and air sampling cylinders through valve V2, a vacuum line through l ~ valve V3 and the main sampling cylinder through valve V 4 . With Valve V iclosed all sampling l dylinders are evacuated after draining and while heating 'the main sampling cylinder to evaporate any liquid in it. After the sampling cylinder has reached 400'F, V3 and V4are closed and Vi is opened to purge the sample tube contents into the purge cylinder. Next V2 is closed and V4 is opened to draw a sample of vapor and air and helium into the sample cylinder. When pressure in the cylinder becomes steady at containment pressure (under a second) V4 is closed and the cylinder is cooled again to under 100*F by compressed air expanding and flowing over the cylinder. With cooling removed the gauge is used to find the steady pressure of air and residual saturated vapor. If helium in air samples are to be obtained V2is opened, then the top valve on one 1800 psi sampling cylinder is opened momentarily and then closed. The steps may be repeated to take another sample at the same location but a later time or at a different location using another He-air sampling cylinder. He sampling system is assembled using brass pipe fittings so that lines are as short as possible to minimize volumes and heat transfer areas that might condense vapor and to keep the assembly as compact as possible. The valves are toggle action globe valves with Viton rubber seats and 0-rings useful from - 20*F to 300*F and to 200 psig. Vacuum is provided by a small bore plastic hose connected to a mechanical vacuum pump located in the laboratory. The sampling line up to the main sampling cylinder is trace heated by a 1/16 inch diameter,36 inch long,120 volts,400 W cable heater energized at a lower voltage to heat the path over 300*F. Those parts, including the line from the probe tube, valves V iand V and 4 the cross are insulated by closed cell silicone sponge rubber strip which is useful from - 100*F to 500*F. The sampling cylinder is designed to have a lower mass for heating and cooling than standard high pressure cylinders. At 100 psig cylinder stress is 1200 psi and plate stress is the same, much less than i 5400 psi allowed in high pressure cylinders. It weighs 0.51 pounds, and has a volume of 88 ml compared with 0.88 pounds and 75 mi for standard 1800 psi cylinders. Using a metal air baffle over the cylinder and up to the inlet tee, a temperature controlled 1680 W, 9 cfm heat gun set to 700*F can heat the cylinder and tee from 50*F to 400 F uniformly in 3.6 minutes. He heating time is govemed by air to metal forced convection heat transfer, not energy content of the air stream. Only
- 20,600 Ws heat is required for the sample cylinder but the heat gun has supplied up to 366,000 Ws.
For that reason, the baffle cylinder heating does not slow the sampling cylinder heating. A compressed air supply from an 80 psig laboratory compressed air line, led through a 3/16 inch diameter nozzle results in an underexpanded air jet of 34.4 scfm at a temperature that is theoretically l more than 160 F cooler. If it is actually only 80*F cooler than supply air at 80*F, the time to cool the sample cylinder and tee from 400*F to 100*F is 3.4 minutes. The flow baffle should establish an upward jet that does not expose the valve operating handle to excessive temperatures. mA3578w-b.non:Ib-o81898 B-7
FINAt. i Pressure in the main sampling cylinder and tee volumes is measured using a compound pressure gauge for 30 in Hg to 100 psig pressure. It utilizes a phosphor bronze bourdon tube filled with silicone oil and is connected to a diaphragm seal with a stainless steel lower housing. De gauge is ANSI Grade A,1% accuracy with I psi markings. The diaphragm seal permits displacing a potentially significant size condensing volume in the gauge with incompressible oil. The seal unit is massive (5 pounds) and although it can be used between - 40*F and 600*F, will not heat and cool appreciably during sample cylinder heating and cooling. It also shields the gauge from any hot, unmixed air jet flow. l The purge cylinder and the helium and air sample cylinders are standard stainless steel,1800 psig heavy wall, 75 ml cylinders with 1/4 inch needle valves for filling at the top and draining liquid at the bottom end. They are removable for laboratory analysis of the helium to air ratios after testing. These cylinders condense steam as samples are drawn and they reach containment pressure with nearly all air and helium in the volume. Temperatures at TCl (To), TC2, TC3 and TC4 (T gand T ) 2are read and recorded using a switchable digital thermometer registering in tenths of a Fahrenheit degree. The design is intended to improve upon a previous design in several ways.' he probe tube is better insulated by being centered in a shield tube. - The previous design relied on external insulation which is less effective at the larger radius and could become useless if wetted. The probe is directly heated over its full length by an internal heater rather than by trace heating under external insulation. The trace heating is not effective over certain portions of the path. Parts of the sampling system that are not directly heated but are trace heated under insulation are kept shorter than for the previous design. The sampling cylinder weight is reduced to shorten heating and cooling times compared with the previous design. Au electrical heat gun and air baffle are used instead of a gas torch. This should be more convenient and provide uniform heating of the cylinder. ___ _ l t
r FINA1. 5.0 PROCEDURES The following are the steps, in sequence, to be taken in order to measure the partial pressere of non-condensables (air or air and helium) in the large scale PCCS test and the fraction of helium in air. 5.1 Installation Fasten the aluminum angle in place to support the probe. Slide the probe through the reducing union up to the ball valve and snug up the ferrule or "O" ring on the probe shield tube. Open the ball valve. Slide the probe into the vessel to the desired location. Tighten the ferrule or "O" ring seal somewhat more. Fasten the sampling system to the probe at the probe tee. Connect the cable heaters to two auto-transformers (5A) and adjust voltage to predetermined values. Connect thermocouple to a switchable digital thermometer. Connect a vacuum line to the sampling system. l 5.2 Prepare for Sampling 1 Record test number, date, and alocation and insertion distance from vessel inner wall (e.g., A-180* - 40 inch) on test data sheet. Record atmospheric pressure (uncorrected to sea level). Heat sampling cylinder to over 200*F using electric heat gun set to 700*F. With valve VI closed, valves V2 and V4 open, open valve V3 and evacuate sampling system including He-air sample cylinders. Close valve V3 and note that the pressure gague indicates steady vacuum. Check that thermocouple TC2 and TC3 register 400*F or greater. Close valves on He-air sample cylinders, and V2 and V4. Heat sample cylinder more until TC4 indicates 400*F. 5.3 Sampling 5.3.1 Purge by opening valve V2 then valve VI. Close valve VI. Close valve V2. 5.3.2 Open valve V4 to admit sample. Monitor TC4 and pressure gauge. When steady (within seconds) record temperatures at TCl (T o ), TC4 (Ti ) and pressure (po). Close valve V4. Record time. 5.3.3 Close valve VI and open valves V2 and V3 to evacuate purge cylinder. Close valve V3. Open valve on one He-air sample cylinder with V2 open and open valve VI to admit sample to He-air sample cylinder. Close valves VI, V2 and on He-air sarnple cylinder. Record sample cylinder identification number. 5.3.4 Cool sampling cylinder using compressed air until TC4 registers less than 100*F. Stop cooling and monitor TC4 and pressure gauge. When steady record TC4 reading (T 2) and pressure (p2)- m:\3578w-b.non:lb-081898 B-9
FINAL The step 5.3.3 may be omitted if helium is not being injected during the test and the installation (5.1) may omit sample cylinders and replace the connecting pipe nipple with a plug. l I
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FINAL 6.0 DATA ANALYSIS The partial pressure of air or helium and air is found using the measured values of temperature and the measured values of pressure, in units of psig, added to the atmospheric pressure p., calculated from inches of mercury by: p, (psia) = 0.4912 x p, (in Hg) (3) Gauge pressures in i rhes of mercury vacuum are converted to absolute pressures in psia by: P (Psia) = 0.4912 (p, (in Hg) - p (in Hg vac.)) (4) Equation (2), with (V /V) 2 assumed to equal one, is used to calculate poir,o. P2ir.o = (T /T 3 )2(P2 - Psat. steam (T2 )) (5) Temperatures are in Rankine degrees which are obtained from Fahrenheit degrees by adding 459.7'F to T( F). The saturation pressure of steam is found between 40*F and 105'F by the following l expression which is within 0.05 psi of the actual value (32*F to 115'F for 0.1 psi accuracy): , p,,, (psia) = 0.51789 - 0.017112 T,, (*F) + 0.0002124 T,,, i i i mA3570w-b.non:!b.481898 B 11 L
L FINAL, l 1 l l l 1 a l l
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{ i 1 l l APPENDIX C l I DATA HANDLING i I I i I I I i l i 1 mus7sw. mon;nbeis" C-1 Rev.1 l
l APPENDIX C C.1 INTRODUCTION The LPCCS Fortran code is written to transform the hand input data and data recorded by the Fluke data l acquisition equipment of the test facility into a Foxpro hta base and/or Lotus spreadsheet format. Figure 3.2- ! I shows a simplified flow chart of the operations perfo.aied. , The code extracts data from a raw data file by using the first (and second, if necessary) character of data to l distinguish between data stomd internally on the Fluke DAS versus that stored by the computer-controlled data j acquisition. Table C.1-1 provides a list and definitions of hand input data variables. The " Flag" for non-l required input data refers to a character that identifies the data to the code. Data that is not recognized by the l code is identified to the user as possible faulty data in an error file ('RC0xx'E. err). Faulty data is dermed as failed or missing sensors and any Flukt, output that can not be identified. Failed data channels are zeroed to j avoid misinterpretation of the data. A list of failed channels can be found in Table 3.3-7. The code performs calculations to convert raw data values into engineering unit values. The code also performs calculations to extract pertinent data on the performance of the test section from each time step, != which provides an indication of the overall test performance. Upon completion of the calculations, the test identification and prerequisites, raw data, and calculated values are written to six ASG output files for import into their respective Foxpro data bases. The first three ASG files contain the test identification, prerequisites, and a portion of the Fluke data. The fourth ASCII file contains the remammg Fluke data. Note that in these { first four ASG files, several of the raw Fluke data channel values are replaced with their respective engineering unit values. Table C.1-2 lists the channels and their respective units. All other channels are thermocouple that are evpressed in Degrees Fahrenheit. The remaining two ASCII files contain the returned calculated values. A description of the calculated values can be found in Table C.1-3. The Foxpro program converts the six Fortran-generated ASG files into three easily manipulated and user l friendly data bases. These data bases are created from existing template data bases. The templates contain no ' , records, but are used to copy the desired field structure to the final output data bases. They are briefly J des:ribed in the following paragraph. The six ASG files (four containing Fluke data and two containmg calculated-value data) are converted into , three data bases, providing an easy method of ==n=ging the data and an easily retrievable test data record. l L Two temporary Fiuke data bases are used in creatmg the two Fluke fmal data bases ('RC0xx'Fl.dbf and
'RC0xx'F2.dbf). These data base files contaip all the DAS-acquired data transformed into engineering units.
The calculated-value final data base ('RC0xx'FO.dbf) is also created from its own temporary calculation data base. 'Ihe Foxpro program also creates three Lotus-123 spreadsheets ('RC0xx'FO.wkl. 'RC0xx'Fl.wkl, and
'RC0xx'F2.wk!) for user analysis.
TABLE C.1 DEFINITION OF HAND INPUT DATA INPUT VARIABLE DEFINITION REQUIRED TEST ID AND PREREQUISITES RUNID Test run identification number. MATXN Test run matrix number (alphanumeric). TDATE Date the test was performed. ISTH, ISTM, ISTS Test start time; in integer hours, minutes, and seconds. IETH, IETM, IETS Test end time; in integer hours, rninutes, and seconds. STMPRES Target steam pressure (psia) of the containment test vessel. Negative values indicate a flow control target value in Ib/sec. TPCOV Target % film water coverage of the test ver ,el dome. TCOVT Target film water coverage type for the test vessel dome. Coverage types may be " flooded", " striped", " quadrants", etc.. TAV Target test vessel anrulus airflow velocity (ft/sec). NON. REQUIRED INPUT DATA INPUT VARIABLE FLAG DEFINITION IDC,IHR,IMN,ISC Z Time the hand input data was taken; in the format " day count: hours: minutes: seconds". A'iMPRES P Atmospheric pressure (psia) recorded at the test site. AVIT X Average vessel inlet temperature (Deg. F). PCOV Percent film water coverage of the test vessel dome. For tests with multiple target conditions only the first are identified in the data files. g . COVT Film water coverage type for the test vessel dome. Coverage types may be " flooded", " striped", " quadrants", etc.. . RELHUM H Relative humidity (%) recorded at the test site. AV A Velocity (ft/ min) of the airflow entering the test vessel annulus. Not used in Phases 2 and 3. LOCVA, REFTEMP Indicated location of the velocity measurement; I for bottom,2 for top. Temperature (Deg. F) at which the velocity measurement is taken. Not used in Phases 2 and 3. BADCHN( ) D Bad data channel array. RPM , U Airflow fan speed (rpm). EWW, EWS W Excess film water information (Ibm; time in seconds to drain). Not used in Phases 2 and 3.
VELMTR (6) V Array containing 6 airflow velocity (ft/mm) meter readings around the circumference of the test vessel. Not used in Phases 2 and 3. LOCV, REFTEMP Indicated location of the velocity measurement; 1 for bonom,2 for top. Temperature (Deg. F) at which the velocity measurement is taken. Not used in Phases 2 and 3. TABLE C.1 DESCRIPTION OF ENGINEERING UNIT VALUES CHANNEL NUMBER DESCRIPTION OUTPUT ENGINEERING UNITS 238 Test vessel steam pressure. PSIA 240 Wind speed. MPH 241 Wind direction. DEGREES 242 Cooling water flow to the top of the LBdSEC test vessel. 243 Cooling water flow excess to the LBdSEC gutter. 244 Steam flow rate in the steam line just LBdSEC prior to the test vessel. 293 Test vessel steam inlet pressure. PSIA 294 Test vesselinside-outside annulus PSIA pressure differential below the fan. j 295 Cooling air velocity below the fan FT/SEC ! assembly. ) 2% E-level test vessel internal gas flow FT/SEC velocity, j 297 D-level test vessel internal gas flow FT/SEC velocity. 298 Dome-level test vessel internal gas FT/SEC . flow velocity. !
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299 A-level test vessel internal gas flow FT/SEC 0 velocity. _. i 300 Dome-level test vessel internal gas FT/SEC flow velocity. 333 Upstream steam flow rate; Gilflo. LBdSEC 335 Steam flow rate in the steam line just LBdSEC prior to the test vessel.
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TABLE C.13 - DEFINITION OF OUTPUT VARIABLES OUTPUT VARIABLE DEFINITION RUNID Test run identification number. MATRIX _NO Test run matrix number (alphanumeric). TEST _DATE Date the test was performed. START _ TIME Test start time; in integer hours, minutes, seconds. END_ TIME Test end time; in integer hours, minutes, seconds. TAR _STMPRS Target steam pressure (psia) of the containment test vessel. TAR _PERCOV Target 'A film water coverage of the test vessel dome. TAR _COVTYP Target film water coverage type for the test vessel dome. Coverage types may be " flooded", " striped", " quadrants", etc.. TAR _AIRVEL Target test vessel annulus airflow velocity (ft/sec). TIME Time that upcoming Fluke data was recorded; in decimal hours. DELTA _ TIME Time difference between individual time steps (sec). ATMOS _ PRES Atmospheric pressure (psia) recorded at the test site. REL_ HUMID Relative humidity (%) recorded at the test site. AIRIN_ TEMP Average temperature (Deg. F) of the airflow entering the test vessel annulus. AIR _IN_ VEL Velocity (ft/ min) of the airflow entering the test vessel annulus. AIROUTTEMP Average temperature (Deg. F) of the airflow exiting the test vessel annulus. AVE _EX_H2O Average film water drain flow rate (Ibm /hr). PERCENTNET Percentage wet coverage of the test vessel dome. AN_AIRVEL Air velocity (ft/sec) in the test vessel annulus, based on the fan rpm. AVG _AN_Ti Average annulus traverse airflow temperature (Deg. F) for test vessel levels i = A, B, and C. AVG _AN_ABC Average annulus traverse airflow temperature (Deg. F) of levels A, B, and C of the test vessel. AVG _IOABC Overall annulus traverse airflow temperatre (Deg. F) of the input, output, and levels A, B, and C of the test vessel. BFLTEMP_DO Average test vessel baffle temperature (Deg. F) at the Dome level. / BFLTEMP_i Average vessel baffle temperature (Deg. F) at test vessel levels i = A, B, C, D, and E.
TABLE C.1 DEFINITION OF OUTPUT VARIABLES OUTPUT VARIABLE DEFIhTTION AVFLDWT_DO Average test vessel wall fluid temperature (Deg. F) at the Dome level. AVFLDWT_i Average vessel wall fluid temperature (Deg. F) at test vessel levels i = A, B, C, D, and E. AVFLUDT_DO Average test vessel rake fluid temperature (Deg. F) at the Dome level. AVFLUIDT_i Average vessel rake fluid temperature (Deg. F) at test vessel levels i = A, B, C, and D. AVFLUDT_FH Average test vessel fluid temperature (Deg. F) below the operating deck, at the "high" level. AVFLUDT_FL Average v' nel fluid temperature (Deg.F) below the operating deck, at the %w" level. AVG _IN_i Average inside test vessel temperature (Deg. F) at the i = 21, 42,63, and 84-inch radial Dome locations. AVG _OUT_i Average outside vessel temperature (Deg. F) at the i = 21,42, 63, and 84-inch radial Dome locations. AVGDELT_i Average inside-outside vessel temperature difference (Deg. F) at the i = 21,42,63, and 84-inch radial Dome locations. AVG _IN_i Average inside test vessel wall temperature (Deg. F) at the i = A, B, C, D, E, and F locations. AVG _OUT_i Average outside vessel wall temperamre (Deg. F) at the i = A, B, C, D, E, and F locarons. I AVG _DELT_i Average inside-outside vessel temperature differene e (Deg. F) at i the i = A, B, C, D, E, and F locations. MAX _IN_i Maximum inside test vessel temperature (Deg. F) at the i = 21, 42,63, and 84-inch radial Dome locations. MAX _OUT_i Maximum outside vessel temperature (Deg. F) at the i = 21,42, 63, and 84-inch radial Dome locations. MAXDELT_i Maximum inside-outside vessel temperature difference (Deg. F) at the i = 21,42, 63, and 84-inch radial Dome locations. MAX _IN_i Maximum inside test vessel temperature (Deg. F) at the i = A, B, C, D, E, and F locations. l MAX _OUT_i Maximum outside vessel temperature (Deg. F) at the i = A B, l C, D, E, and F locations. l MAX _DELT_i Maximum inside-outside vessel temperature difference (Deg. F) at the i = A, B, C, D, E, and F locations. l
TABLE C.1 DEFINITION OF OUTPUT VARIABLES OUTPUT VARIABLE DEFINITION MIN _IN_I Minimum inside test vessel temperature (Deg. F) at the i = 21, 42,63, and 84-inch radial Dome locations. MIN _OUT_i Minimum outside vessel temperature (Deg. F) at the i = 21,42, 63, and 84-inch radial Dome locations. MINDELT_i Minimum inside-out.ide vessel temperature difference (Deg. F) at the i = 21,42,63, and 84-inch radial Dome locations. MIN _IN_i Minimum mside test vessel temperatw e (Deg. F) at the i = A, B, C, D, E, and F locations. MIN _OUT_i Minimum outside vessel temperature (Deg. F) at the i = A, B, C, D, E, and F locations. MIN _DELT_i Minimum inside-outside vessel temperature difference (Deg. F) at the i = A, B, C, D, E, and F locations. HS_ TEMP _i Average test vessel beat sink temperature (Deg. F) at each unit; i = A, B, C, and D. AV_ GRATE _T Average test vessel grating temperature (Deg. F). AV_IWALL_H Average test vessel inside wall temperature (Deg. F), at the "high" level. AV_IWALL_L Average vessel inside wall temperature (Deg. F), at the " low" level. TIMESTEP Test data set counter. 4
FINAL i l 1 i 1 l l i I, APPENDIX D OFFICIAL TEST DATA FILES
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i i l ' mus7sanon: b-ostees D-1 ;
FINAL
= 4,b Appendix D consists of an electronic data file which contains proprietary information.
ms57sw.non:S os209s D-2
FINAL l 4 APPENDIX E-BASELINE TEST DATA i l f m:\3578w.aom:Ib48209s E-1 w________-________________-________-___ _ _ _ - _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ - _ _ _ _ _ _ _ _ _ _ _ . _ _ _ _ _ _ - ._ _ _ _ _ _ _ _ _ _ _ _ _ _ .
1. Few.. Appendix E contains tabulated test data for the following tests. a.c j Baseline Tests No Internals: B.1 Test 201.1 Run 9L B.2 Test 202.1 Run 10L B.3 Test 203.1 Run 8L B.4 Test 207.1 Run 1IL B.5 Test 207.2 Run 12L Baseline Tests with Internals: C.1 Test 201.2 Run 17AL i C.2 Test 202.2 Run 34L ) C.3 Test 203.2 Run 27L C.4 - Test 204.1 Run 24L l J 1 C.5 Test 205.1 Run 23L C.6 Test 206.1 Run 26L C.7 Test 207.3 Run 21L I C.8 Test 207.4 Run 22L l C.9 Test 208.1 Run 20L C.10 Test 210.1 Run 28AL C.ll Test 211.1 Run 28L
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