Text

Tests of Full Scale 1/48 Segment of Humboldt Bay Pressure Suppression Containment
	ML20207U023
Person / Time
Site:	Humboldt Bay
Issue date:	11/17/1960
From:	Imhoff D, Robbins C; GENERAL ELECTRIC CO.
To:	;
Shared Package
ML20207T986	List: ML20207T985; ML20207U023; ML20207U059;
References
	FOIA-87-40 GEAP-3596, NUDOCS 8703240520
	Download: ML20207U023 (122)
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{{#Wiki_filter:, ~- l i l r GEAP 3596 l I .p-MASTER .. c..- 9 TESTS OF A FULL SCILE,1/48 SEGME!E [' l g OF THE / ~ HUMBOLDT BAY PRESSURE SUPPRESSION CONI _ARRENr w s ( PREPARED FOR PACIFIC CAS AND ELECTRIC COMPANY liEQUISITION NO. 474-96252 i I November 17, 1960 l f Author ) C. H. Robbins countersigned 6 N D. H. IdhVff CENERAL ELECTRIC CCHPANY ' ATOMIC POWER EQUIPHENT DEPARTHENI San Jose, California St. q, \\1 32 O B70320 g7g 7,.. -- , - -......y, ;$..m,gg [u THOMAS 87-40 PDR

/ y.s-IMPGITANT N(7PICE REPARDING CONTENTG GP THIS REPollT PLEASE READ CAREFUILY The only undertakings of General Electric Company respecting infor-mntion in this doeurnent are contained in the contract between Pacific Gas & Electric and General Electric Company, Requisition No. h74-96252, and nothing contained in this document shall be construed as changing the contract. The use of this information by anyone other than i Pacific Cas & Electric, or for any purpose other than that for which it is intended, is not authorized; and with respect to any unauthorized use, General Electric Company makes no representation or warranty, and assumes no liability ac to the completeness, accuracy, or usefulness of the information contained in this doctament. i -} i I l i ., - ~ -.

= I R TABLE OF CONTENTS l Page No. ) i List of Figures Ssmanary i I. Introduction 3 i II. Objectives 4 III. Conclusions 5 IV. Description of Test Facility 6 V. Discussion of Results 10 A. Flow from Reactor Vessel to Dry Well 10 B. Dry Well 15 C. Vent System 20 D. Suppression Chsaber 24 Appendix I Tabulation of Test Data and Results I-1 Appendix II Average Flow Kates from Reactor Vessel 11-1 and into Vent from Dry Well Appendix III Pressure Traces III-1 i e t 9 $h I

A Jl l LIST OF FIGURES A Fage .(*,1 2 ~ ~ ~ ~ Numbers i Figure 1 Photograph of Test Facility 9-a l Figure 2 Schematic Diagram of Moss Landing 9-b I Pressure Suppression Test Facility 1, I Figure 3 Arrangement of Moss Landing Test Facility 9-c j Figure 4 ' Requirements for Pressure Vessel 9-d Figure 5 Piping and Mechanical Miscellaneous 9-e Sections and Details i Figure 6 Test Dry Well and Arrangement of 9-f Internals Figure 7 Details of Suppression Chamber 9-g Figure 8 Test Results of Flow from Fressure Vessel 13-a Through a Sharp Edge Orifice Figura 9 Sequential Photographs of Fool Action 24-a 9 i I F- ' o

SUMMARY

A full scale 1/48 segment of the Humboldt Bay pressure suppret.sion contain ~, ment was built and tested. The objectives were to demonstrate the ability of the system to handle *.he accident predicated for the Humboldt containment design, and to obtain information on the performance. i The test facility represented one of the 48 Humboldt Bay vent pipes, the portion of the suppression chamber and pool associated w.'.h it, and appro-priately sized vessels representing the reactor vessel and dry well. Transient tests were conducted by heating water in the reactor vessel to 1250 psig. A rupture disk arrangement was broken allowing water and stess from the pressure vessel to flow through ari orifice into the dry well. Flow l proceedeo from the dry well into the suppression chamber through a vent pipe which simulated the length and resistance of the Humboldt vents. Transient pressures were measured.and recorded continuously at various locations. e Temperatures were also measured at strategic points and recorded. Many parameters were investigated in the tests. The orifice diameters ranged from 0.14 to 3.28 inches as compared with the 1.64 inch diameter representing the maximum credible operating accident break postulated for Humboldt design. Two different size dry wells were used and internals in the dry well varied the amount of water carri:d with the steam through the dry well into the ve'nt. The effect of additional air was investigated by discharging air from an auxiliary tank into the dry well in the middle of The initial vent depth of submergence was changed by raising or a run. lowering the pact water level. Initial depth of submergence was varied between 12 feet 5-inches, and a level with the vent 3 feet above the water surface. The initial temper.atute of the water pool was raised to about 138' F in one ts.st to determine the ability of hot pool water t.o condense. Flow through the break from the reactor veseel was much lower than would be predicted using a cold water orifice coefficient and the assumption that fluid flowing through the orif* ice is saturated water at the existing reactor The data tends to indicate that the flow is affected by the pressure. flashed stems entrained in the flow toward the orifice. The maximum dry well pressure for tests representing the Humboldt design accident was in the range 25-36 psig, compared with the design pr' essure for the Humboldt dry well of 72 psig. The resistance of the vent rather than the depth of submergence determines the maximum dry well pressure for the Humboldt design. t Pressures in the vents can be calculated fairly accurately using a homogeneous flow model for the two-phase steam-water mixture. However, the homogeneous model is probably not satisfactory for predicting pressure [ $P \\, s 9 e

at the end of the vent. Tes~t. data was inconclusive whether a critical end pressure occurred in any of the tests. 7., ] Condensation in the water was rapid and complete for a wide range of test parameters including and exceeding the design conditions for the Humboldt l containment system. Essentially complete condensation was achieved with: 1. An orifice area 4 times that representing the Humboldt design conditions, 2. The vent initially 2 feet above the water pool as compared with the 6 foot submergence in Humboldt, and F as compared with 3. A water pool with a temperature of 138-1610 the Humboldt design conditions of 80-115' F. l The tests with added air show that air with the steam-water will not pre-vent the steam from being rapidly and essentially completely condensed in j the. pool. No severe equipment vibrations or water hammer were observed. l The testa show conclusively that the Humboldt Bay pressure suppression containment could safely hancle the assumed maximum credible operating i accident with a large safety margin. i i f i f c l l 2 F I l 4 I, _.,.. -.. _ ~.. _ - - - _ _ _ - - -. - - - - - -. - - - ~ ~ * * - * * ' ' - - - - " - - " ~ ' - * * " ~ ' " " ~

I. IN1110 DUCTION .q d,*- 5*** This report describes tests conducted in May and June of 1960 to verify the pressure suppression containment design proposed for Humboldt Bay Power Plant, Unit No. 3. Previous tests conducted in 1959 demonstrated the basic feasib!11ty of pressure suppression containment and provided data required for design. These results were then used in preparing the con-tainment design for Humboldt Bay and approval was sought from the United States Atomic Ener8y Commission for tFis containment. Upon receipt of the March 14, 1960 letter from the Advisory Consnittee on Reactor Safeguards, which expressed the view that the earlier tests had not fully demonstrated the safety of the proposed pressure suppression system, the full scale 1/48th segment tests described in the present report were nianned and performed to provide assurance that the specific design selected for Humboldt Bay would function properly. The test equipment was designed and built to represent a full scale 1/48th segment of the Humboldt Bay pressure suppression sys tem. Principal components were: a simulated reactor vessel, an orifice to produce the desired break area, a dry well, a 14-inch vent line, and a suppression chamber containing a water pool. The performance of this equipment was meabured over a range of simulated accidents. The f acilities for these tests were designed, built, and operated by the Pacific Gas and Electric Company. Consultation was provided and this report ~ was prepared by the Atomic Power Equipment Department of the General Electric Company. The work described here is an extension of the deveinpment program on pressure suppression conducted for Pacific Gas and Electric by General Electric. Planning of the facilities and of the tests was under the direction of C. C. Whelchel, Chief Mechanical Engineer of the Pacific Gas and Electric Company. Among the many other PG6E employees who contributed to this work, the names of the following should be mentioned: D. B. Barton, A. M. Kennedy, and N. Wheelock. l l l F 3 -~v---,-<-----

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l II. OBJECTIVES l i A. Desmonstrate the ability of the Humboldt Bay pressure suppression t.# I-containment system to handle the primary system break postulated as the uaximum credible operating accident. This is defined as the instantaneous rupture of a 12-inch line. Measure test performance and compare with Humboldt Bay design values for the following: 1. Maximum dry well pressure 2. Maximum suppression chamber pressure B. Obtain additional information on the performance of the Humboldt Bay pressure suppression containment system: 1. Determine energy and mass flow rates following a primary system ';f rupture as a function of break size and the amount of water in the sys tem. 2. Obtain data on dry well pressure transients which can be used to help improve and verify analytical work on Humboldt Bay design. 3. Measure flow resistance of the 14-inch vent pipe to obcain data on inlet losses, bend losses, and pressure, and total pressure i drop. Investigate the effect of water and air mixing with the steam leaving the dry well. 4. Observe action of the suppression pool water during transient operation. Measure temperatures at different locations. t 5. Investigate effect of vent pipe depth of submergence on dry well pressure, suppres,sion chamber pressure, and pool circulation and mixing. 6. Investigate effect of suppression pool temperature on performance j! i of pressure suppression systta. \\ 4 .i 9 I V

III. CONCLUSIONS A. The Humboldt Bay pressure suppression containment system could handle. the maximum credible operating accident with a considerable margin of safety. 1. The Humboldt dry well is designed for 72 psig, but in tests representing the M.C.O.A., dry well pressure was in the range 25-36 psig. l 2. The Humboldt suppression chamber is designed for 10 psig and will withstand. higher pressures because of other design considerations. The test chanber pressures did not exceed 9.3 psig in tests representing conditions much more severe than the M.C.O.A. B. The mass flow rate from the reactor vessel is substantially lower than would be predicted using an orifice equation with a cold water ' coefficient and asstaning a density of saturated liquid. C. The resistance of the vent rather than the initial depth of submer-gence determines the maximum dry well pressure for the Humboldt design. D. The homogeneous flow model for flow of steam-water mixtures predicts pressures in the vents fairly accurately except for the vent outlet pressure. A critical pressure did not appear to occur at the vent exit, but test data was not conclusive. E. Steam condenses very readily in the water pool. 1. Very high flow rates condense. 2. The vent can be above the initial water level and the ateam will still be condensed quickly and completely. 3. The water in the pool can be hot (140-160' F). 4. Air from the dry well does not prevent efficient condensation. F. Water in the pool is thrown high into the suppression chamber at the start of a test by the air leaving the vent. Mixing of the water in the pool was excellent in all tests covering a wide range of simulated break sizes.- i / G. No severe vibration or water hammer occurred. j 33 I t

I i "IV. DESCRIPTION OF TEST FACILITY .-? A. Basic Criteria and General Description, 7 ~ a The test facility at Hoss Landing was designed and built to reproduce as exactly as possible one of the 48 Humboldt Bay vent pipes, the l portion of the suppression chamber and pool associated with it, and an appropriately sized dry well and reactor vessel. A photograph of the l facility taken near the completion of construction is shown in Figure 1. 4 The schematic diagram of the equipment appears as Figure 2, and l Figure 3 presents the equipment arrangement. I i B. Reactor Vessel and Connections to Dev Well The vessel shown in Figure 4, which simulates the reactor vessel, was made from 20-inch schedule 80 pipe with a volume of 55 cubic feet. This is equal to 1/48th of the net volume of the Humboldt Bay reactor vessel. The test vessel was designed for 1250 psig. A steam line was attached to the bottom of the vessel for heating the water. Other small connections were provided for the safety valve, pressure and tempera-ture measurements, water level indication, and filling and draining. A 6-inch nozzle was connected to the vessel for discharge through an orifice to the dry well as shown in Figure 5,. Different sized sharp edged orifices were used: 0.14 inch diameter, representing a small break (very small) 0.30 inch diameter, representing a small break l 0.6 inch diameter, representing a small pipe break l 1.1 inch diameter, representing an 8-inch pipe break 1.64 inch diameter, representing a 12-inch pipe break (the I maximum credible operating accident) l 2.10 inch diameter, representing a break 647. Larger than the maximum credible operating accident. 2.32 inch diameter, twice the area of 1.64 inch 2.84 inch diameter, three times the area of 1.64 inch 3.28 inch diameter, four times the area of 1.64 inch i, l A double rupture disk assembly between the orifice and the dry well was used to initiate the tests. t l Figures 1-7, which describe the equipment, appear at the end of Section IV. f 1 ? l-l i j

j 1 C. Dry Well and Internals The dry well was simulated by a tank as shown in Figure 6. The inlet opening was 10-inches in diameter and the outlet was 14-inches in diameter. Other nozzles were provided for instrumentation, for a safety rupture disk, and for vcating and draining the tank. A { deflection plate, consisting of a 14-inch square curved plate was n:ounted 4-inches out from the discharge opening, simulating the deflector plate used in the Humboldt design. During the first 12 tests, the volume of the tank was 277 cubic feet.- 4 Heaters were provided to preheat the air in the tank and the outside of the tank was insulated. t During tests 13 and beyond, the volume of the tank was reduced to 199 cubic feet by shortening the height of the vessel. The insulation was not replaced af ter this change. Various internals were used in the dry well in order to vary the j amount of water carried into the vent pipe from the dry well and to change the relative timme during the transient when the air lef t the \\ dry well. The arrangessents tested are shown in Figure 6, and include the followi'ag: 1. A tee discharges horizontally near the dry well inlet with j a deflector plate guarding the vent inlet. 2. The deflector plate is removed. An extension piece ending 13-inches from the vent pipe inlet is arranged to discharge toward the vent inlet. 3. A short (10-inch) nozzle is aimed at the deflector plate covering the vent pipe inlet. 4. A tee discharges horizontally near the vent pipe inlet. The defl:ctor plate is installed. 5. A tee discharges vertically sear the vent pipe inlet. The deflector plate is installed. For three runs, an air tank with a volume of 38.1 cubic feet was connected to the dry well by a short line containing a quick opening valve. The tank was pressurized with air before a test. The quick opening valve was opened during the test to add a measurable amount of air to the dry well ana vent. . ~ \\ 1

k ~ ii D. Vent Pipinst The vent piping, shown in Figure 5, was designed to meet two criteria: 1. To make the total volume (and hence the transport time) the same in both the Moss Landing test and the Humboldt Bay design. I 5 2. To make the flow resistance for the Mosa Landing test the same as for the Humboldt Bay design. l A 14-inch pipe r nd fittings was used for the Noss Landing test. The s l arrangement using one long radius ell, one ahort radius ell, and a tee with one end capped was calculated to provide the same equivalent length as the Humboldt Bay sys tem. Details of the equivalent lengths are given in Section VC2. The volume of the test vent piping from the dry well to the normal suppression chamber water level was 49 cubic feet. g.. 7 l E. Suppression Chamber i Figure 7 shows the Moss Landing suppression chamber, which was designed to provide the same size and shape of water and air space as those associated with a single 14-inch Humboldt Bay vent pipe. The suppression chamber was approximately trapezoidal,12 feet acrose. 2.35 feet on one base, and 1.23 on the other base. The entire chamber was 49 feet high and the normal water depth was 18 feet. When filled to a depth of 18 feet. the free volume in the Moss Landing suppression chamber was 650 cubic feet, or 1/48th of the Humboldt Bay suppression j chamber air volume. l. The chanbar was contained in a cylindrical pressure vessel partially buried in the ground. Space between the walls of the cylindrieml ~ vessel and the walls of the trapezoidal pressure suppression chsaber I were filled with concrete. The walls of the suppression chamber were insulated to reduce condensation. Openings were provided in the Moss Landing suppression chamber for filling and draining connections, instrumentation, viewing ports, a' t manhole, vacuum breaker, safety valve and vent. F. Ins trumentati_o_n 1 n The instrumentation provided for the Moss Landing tests is shavn in Figure 2 1. Water Levels I Water level in the reactor vessel prior to testing was measured by a two foot sight glass which could be mounted at three different'y' elevations. -S-

The amount of water remaining in the dry well vessel following a test was measured by draining into a calibrated container. Water level in the suppression chamber was measured by using the drain valve at the normal water level or by a manometer. 2. Dew Point Suppression chamber dew point was measured with a dew point recorder prior to testing. The instrument was removed before a l test to keep water from splashing on it and damaging the element. 3. Pressure Bourdon tube pressure gages were used to measure pressure in r the reactor vessel, dry well, and suppression chamber. Strain gage transducers were used with a 10 channel Visicorder oscillograph to measure and record pressures during a test. Measuring points were the following: a. Near top of reactor vessel in steam space. b. In discharge flange just before orifice. c. In discharge pipe between rupture disks and dry well. d. In dry well. e. In 14-inch vent pipe adjacent to dry well. f. In 14-inch vent pipe downstream from T. g., At discharge end of 14-inch vent pipe. h. In vapor space of suppression chamber. i. In auxiliary dry well for runs 40, 41 and 42. 4. Temperature Fast response thern.ocouples with a recorder were used to measure and record temperatures at the following locations: I a. Near the top of the reactor vessel. b. Near the middle of the reactor vessel. c. Near the bottom of the reactor vessel. d. In the dischsrse from the reactor vessel. e. In the dry weu. f. At three elevations in the vapor space of the suppression chamber. g. At four locations in the suppression chamber pool. y, .-,,_,3,w ,,,,,y,- m_ww,--4 m,m,-m- _me-

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V. DISCUSSION OF RESULTS t A tabulation of test results is presented in Appendix I and reproductions of all the pressure traces are shown in Appendix III. The first four tests were conducted primarily to check out the equipment j under conditions of increasing severity. Subsequent tests investigated the effects of different parameters and are discussed in the following paragraphs. 1 A. Flou From Reactor Vessel to Dry Weil 1. .Conclus ions, Evaluation of the test data results in the following conclusions 6 concerning flow from the reactor vessel to the dry well. a. The resistance of the piping connecting the test reactor vessel with the dry well has a minor effect on the flow i rate from the vessel. Calculacions indicate that for the i 1.64 inch orifice, the discharge tube reduced the flow about 37. and for the 3.28 inch orifice the discharge tube reduced the flow about 8%. b. The mass flow rate is'substantially lower than would be l p.edicted using an orifice equation with a cold water coefficient and assuming a density of saturated liquid. The test data tend to support the hypothesis that the velocity of the fluid in the vessel in approaching the l orifice affects the amount of flashed steam drawn along g with the liquid. It is possible that flashing during flow through the orifice miy reduce mass flow and that critical flow may occur.' i 2. Discus'sion ,l l 8 a. Shape of Pressure Traces The shape of the pressure vs. time curves for the reactor vessel indicate that flow proceeds in the same manner as in the Transient Tests at San Jose in 1959. Pressure in the vessel decreases in three phases. I GEAP 3143

Test Report for the Pressure Suppression Development Program",

by Fiock, Janssen and Steamer, April 2,1959. - to - l l I

P}( Phase A occurs right af'ter the rupture and consists of a sharp drop in pressure followed quickly by a partial recovery. For example, in run 15 pressure measured at the top of the reactor vessel dropped from 1250 psis to 1175 psig in about 0.25 seconds and then rose to about 1190 psig by 0.75 seconds after the start. The usagnitude of the first sharp drop tends to increase with orifice size; the initial drop was 75 psi for run 13 with a 1.64 inch orifice while the drop was 165 psi for run 17 with a 2.84 inch orifice. The pressure af ter recovery at the end of Phase A appears to be affected by the initial water level; for example, run 21 and run 15 had initial water volumes of 49.8 and 39.2 cubic feet and pressures at the end of Phase A of 1215 and 1190 psig, respectively. It is also interesting to note that the total pressure drop during Phase A is about 60 psi for orifices 1.64 inches and bigger, but the drop de:reases as orifice size decreases below 1.64 inches. Comparison of the pressure traces for the 1960 Moss Landing tests with the 1959 San Jose tests show that the duration of Phase A is shorter for the small scale tests. Phase B, which follows Phase A, is a period of almost steady decreacc of re c. tor vessel pressure with time. The average -4 rate of press, a decrease in Phase B is much slower than N that in Phase A Phase C is a period when the pressure decay curve is concave upward as would occur with blowdown of a gas-filled pressure vessel. The transition from Phase B to Phase C is less abrupt as the orifice size relative to the vessel diameter increases. The pressure decay curves may be skplained in the followtas l ways: Flow during Phase A starts with the expulsion of subcooled liquid through the orifice and ends when the pressure in the vessel has dropped so the fluid flowing through the orifice is saturated. The partial recovery from the first sharp pressure drop may be the result of delay in flashing of steam. The initial steam volume expands, pushing liquid out through the orifice and lowering the liquid level in the vessel. As flashing occurs, the mass that was initially liquid swells and the pressure rises as the vesset contents return more nearly to equilibrium. Flow during Phase B consists of a mixture of steam and water. V.

i Phase C begins when all the liquid has been expelled from the vessel and only steam remains. Flow during Phase C consists of steam only. ) b. Ef fect of Discharme Section Between Orifice and Dry Well I The downstream pressure of the orifice is somewhat higher than the dry well because of the restriction of the piping connecting the reactor vessel with the dry. sell. Calculations have been made to help evaluate the effect of the discharge tube on flow through the orifice. An upstress pressure of 1190 psig and an enthalpy of 580 Btu /lb was l assumed in all cases. The pressure downstream from the orifice was taken as the maximum dry well pressure to evaluate flow without the discharge tube. For flow with the discharge tube, a pressure just downstream from the orifice i was cniculated by using a homogeneous flow model, assuming critical flow at the end of the 6-inch discharge tube and calculating the pressure drop in the 33-inch length of 6-inch pipe back to the orifice plate. The average measured l flow as given in Appendix II was used. Results are: PD F orifice Max. Dry calc isted Calculated teatricted Flow Diametsr Well Pressure Pressure Below c=1cul ae.d Umy Pylet ed Finu f inches esim. Orifice. Psia. N(1190-P,)/G19&P ) D 1.64 33 104 .969 2.32 64 167 .954 2.84 90 220 .938 3.28 128 295 .918 These calculations show that the discharge piping between the reactor vessel and the dry well could not restrict flow very saich. There is a distinct possibility that flow through the orifice was critical, and if this were so, the discharge tube would have no effect on the flow rate from the reactor vessel. A pressure tap (PT7) was located near the middle of the 6-inch pipe. Near the start of Phase B, this pressure was about 70-80 psig with an orifice of 1.64 inches. The calculated pressure, V ! l t

( assuming a homogeneous model, was 101 psig at this point. With orifices larger than 1.64 inches, the pressure trace for the discharge tube went off scale and was not recorded i for the initial portion of Phase B. Comparison of the homogeneous calculation with the measured pressure shows that the homogeneous method gives too high a i pressure for this case. As a result, the calculated restric-tion of the discharge tube for flow through the orifice is probably too great. c. Flow Rate From Vessel The average flow rate per unit area of orifice during Phase A l and B decreases, but may approach a limit as the orifice size increases. This behavior is indicated in Figure 8 where the ordinate is proportional to mass flow rate, corrected for average pressure across the orifice during Phase B. The abscissa is the ratio of orifice diameter divided by vessel diameter. The orifice equation has frequently been used to predict ble Vown of a pressure vessel filled with saturated water. j Generally a coefficient of about 0.61 has been useo end the density of the fluid flowing has been assumed to be that of ( saturated liquid at the transient pressure prevailing in the reactor vessel. The test data confirm the belief that this method of calcula-tion predicts flow rates smch higher than occur. For exseple, flow rate calculated by these assumptions is about 501,901, and 250L too large for the 1.10,1.64, and 2.84 inch orifices, respectively. Among the reasons why the orifice equation with these assumptions is inaccurate are the following: (l') Critical flow may occur in the orifice and the orifice equation may not be applicable. Whether or not a critical flow can occur with a two-phase mixture through a sharp edge orifice has not yet been established. However, in preliminary evaluation of the test data, the assumption of critical flow appears to have some merit. (2) The assumption that the fluid flowing through the orifice is saturated liquid is probably a poor one. First, some flashing will occur during flow through the orifice so that the density will be less than that of saturated water. Second, the possibility exists that steam formed by 5 flashing within the pressure vessel will be drawn through the orifice before it has time to separate from the water. - is - t

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( (3) The orifice coefficient may be different than 0.61. Diameter, viscosity, and density all have some effect on the orifice coefficients determined for single phase flow of gases or liquids. " Fluid Meters", ASME,1959 presents a discussion of these factors along with tables of orifice coefficients as a function of Reynolds number and orifice dianater relative to pipe diameter. The variation of the orifice coefficient is about 1-2% in the i range of test conditions, as determined by these tables, based on single phase flow of gas or 1.Wid. / The relationship between flow and orifice d s n.or can be 1, accounted for at least in part by the amou of flashed steam h that is drawn through the orifice. If the orifice is small relative to the vessel disaneter, the velocity of the liquid l* flowing toward the orifice will be small compared with the velocity of the flashed steam bubbles rising by buoyancy. If the liquid velocity downward is small, most of the flashed steam can escape, and the fluid entering the orifice will be r-early that of saturated liquid. On the other hand, if the crifice is large, the downward velocity will be high and will swaep the flashed stem with it through the orifice. The density of the fluid entering the orifice will be r.uch lower than that of saturated liquid in this case. If the liquid velocity is high enough, essentially all of the flashed stean is drawn with the liquid; an ir.ressa in velocity will not further decrease the density of the fluid entering the orifice. The test data plotted in Figure 8 tend to support this hypothesis. The ordinate correspoads to mass flow corrected for differences in pressure drop across the orifice. The t abscissa, orifice diameter to vessel diameter, is a measure of the downward velocity of the liquid in the vessel. The mass velocity appears to be near a limit for values of orifice to vessel diameter greater than about 0.13, at which point the average downward velocity of the liquid, meglecting volme occupied by the steam, is about 2 foot per second. L Test data for both the 1959 Transient Tests and the 1960 Mose ( Landing tests have been plotted on Figure 8. The 1959 tests ( used a 10-inch diameter pressure vessel with a volume of 3 ft3 and an initial pressure of 1000 psig for most tests. This compares with the 1960 tests using a 20-inch dismater vessel with a volume of 55 f t and an initial pressure of 1250 pois in most runs. The agreeseent between the two sets of data is surprisingly good. I i I I .)

( (3) The orifice coefficient may be different than 0.61. Diameter, viscosity, and density all have some effect on the orifice coefficients determined for single phase flow of gases or liquids. " Fluid Me ters", ASME,1959 presents a discussion of these factors along with tables of orifice coefficients as a function of Reynolds number and orifice dianater relative to pipe diameter. The variation of the orifice coefficient is about 1-27. in the ran;c of test conditions, as determined by these tables, based on single phase flow of gas or liquid. The relationship between flow and orifice diameter can be accounted for at least in part by the amount of flashed steam that is drawn through the orifice. If the orifice is small relative to the vessel diameter, the velocity of the liquid flowing toward the orifice will be small compared with the velocity of the flashed steam bubbles rising by buoyancy. If the liquid velocity downward is small, most of the flashed steam can escape, and the fluid entering the orifice will be nearly that of saturated liquid. On the other hand, if the orifice is large, the downward velocity will be high and will swasp the flashed steses with it through the orifice. The density of the fluid entering the orifice will be ir.uch lower than that of ,s saturated liquid in this case. If the liquid velocity is high enough, essentially all of the flashed steam is drawn with the liquid; an ir.ressa in velocity will not further decrease the density of the fluid entering the orifice. The test data plotted in Figure 8 tend to support this hypothesis. The ordinate correspoads to mass flow corrected for differences in pressure drop across the orifice. The abscissa, orifice diameter to vessel disseeter, is a measure of the downward velocity of ttne liquid in the vessel. The mass velocity appears to be near a limit for values of orifice to vessel diameter greater than about 0.13, at which point the average downward velocity of the liquid, neglecting volume occupied by the steam, is about 2 feet per second. Test data for both the 1959 Transient Tests and the 1960 Mosa Landing tests have been plotted on Figura 8. The 1959 tests used a 10-inch diameter preasure vessel with a vo16ses of 3 ft3 and an initial pressure of 1000 pais for most tests. This compares with the 1960 testa using a 20-inch diameter vessel with a volume of 55 f t3 and an initial pressura of 1250 pois in most runs. The agroereent between the two sets of data is surprisingly good. s - \\

B. Dry Well

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1.

== Conclusions:== a. The maximum dry well pressure for tests repres:nting the l Humboldt design accident was in the range 25-36 psig. compared with the design pressura for the Humboldt dry I well of 72 psig. b. The resistance of the vent rather than the vent depth of submergence determines the maximum dry well pressure for j the Humboldt design. The maxim = dry well pressure is essentially a kinear c. function of the orifice area for orifice diameters in the range of 1.64 to 3.28 inches. \\ 2. Shape of Dry Well Pressure Traces i Pressure rises rapidly in the dry vs11 immediately af ter the ruptura disks break and reaches a pressure of about 2/3 the naaximuss in about 0.25 seconds. The pressure curve at the smaximum is generally flat or well rounded. Following the sneximum, the pressure declines gradually until the water has i been expelled fross the reactor vessel (and of Phase 3). The dry well prassure then decreaacs more rapidly during Phase C while the steen leaves the reactor vessel. a. The time the aneximum dry well pressure is reached, relative to pressure changes in the vent line outlet and suppression chamber, depends on the particular test conditions. For the Eumboldt design conditions (1.64 inch orifice and 6 feet submergence), the maximum dry well pressure occurs shortly after the vent outlet pressure starta to rise. This is a tiime in the order of 0.25 seconds af ter the start of the test. Increasing the orifice size delays the time of the maximum dry well pressure. For orifices 2.32 inches and 3.23 inches, the pressure rose rapidly for about the first second. Reducing the vest submergence also delays the time of the maximum dry welt pressure. 3. Maximus Pressure for Numboldt Desien Conditions i The snaximum dry well pressure for testa representing Rumboldt design conditions is in the range of 25-36 pais. The design pressure for the Numboldt dry well is 72 psig. The design ~# conditions are represented by testa 13, 16, 15, 24, 25, 26, 24 36, and 44 where the orifice is 1.64 inches, the initial volums i ! i, ) s

( 3 of vator is about 38 f t, vent submergence is - feet, the dry well rad vent volume is 248 ft, and the suppression chamber is 3 closed. The spread in pressures for these testa is largely the result of changes in the dry well internals. These affected the amount of water carryover in the vents, the relative time air left the dry well, and the entrance loss for flow from the dry well to the vent. 6. Effect of Varf us Parameters on Peak Dry Well Pressure a. Orifice Sise t The martmuss dry well pressure varies approximately linearly with orifice area. The 11asar reistionship betw.:ca orifice area and dry well pressure results from a combination of: I (1) flow into the vessel vs. orifice area. and (2) pressure drop between dry well and suppression chamber as a function of flow. Both relat' ions (1) and (2) are fairly linear over a wide range and the dnartures frors linearity tend to counteract each other. Consequently, muimum dry well pressure varies au arly linearly with orifice area la the range tested, b. j!oi,*,ure Carrvover from Dry Well to Vent Conclustoms drawn from the test results on the effect of i moisture carryover are limited because average carryover throughout a run was deters'uod rather than the amount of moisture carryover at the time of the maximum dry well pressure. In additime, the effect of air and water carryover are inseparably mixed la most tests. Some idea of the effect of moisture carryover om dry well pressure can be obtained by can. paring run 13 with run 36. Test, conditions are very similar and the pressure traces show that air left the dry well in much the same fashion la both. However, run 13 had 281 of the maximum possible water la the dry well at the end of the test as compared with 771 for rum 36. This resulted in the average mass flow rate in the weats being 201 hiaber for run 36 than for run 13. The maximum dry well pressure, which occurred very soon after the test started was 32 psis for run 13 and 33 psis for rum 36. At the and of Phase B when the last of the water was leaving the pressure vessel, the dry well F pressure was 19 peig for run 13 and 27 peig for rue 36. These numbers suggest: _,_-_n_-- w ' ' ' ' ~ * " " * * ~ ~

- - - ~ ~, n I (1) Variation in moisture carryover has only a saia11 effect on the maximum dry well pressure. (2) Moisture carryover is not uniform during any one 5,- This would account for the greater difference test. F-in dry well pressures at the and of Phase 5. l c. Air Flow l The time air leaves the dry well probably does not have a Air does large effect on the maximum dry well pressure. have some effect on the flow loss in the vent, and this subject will be discussed in a subsequent section of the report. f The effect of delay in air leaving the dry well is shown, in part, by tests 6, 7, and 27. In these tests, the reactor ) vessel discharge pipe was extended so that the discharge was near and directed at the dry well outlet. The delay l in air leaving the dry well is indicated by the rise in suppression chamber pressure which is slow compared with other runs such as 15 or 25. The effect of air delay is difficult if not impossible to separate from other effects. J Runs 6, 7, and 27 have lower dry well pressures than other runs such as 15. However, this difference could be caused Runs 6, 7, and 27 were arranged by the flow conditions. so that the jet entering the dry well discharged right at and near the vent inlet. In run 15, the flow entering the dry well would slow down in the dry well. Consequently,. dry well pressure in run 15 would be higher than in run 27 by the velocity head of the fluid passing through the dry well. d. Vent Depth of Submeraence The initial depth of submergence has a small effect on the l maxismze dry well pressure for the proportions tested. Reducing the initial depth of submergence from 6 feet has no appreciable effect for an orifice size of 1.64 inches; ) this is shown by runs la and 20 which have submergences of ) 6 feet and -0.5 feet and maximum dry well pressures of 33 and 34 psis, respectively. Runs 16 and 32 with an orifice size of 2.32 inches resulted in dry well pressures of 64 and 59 psig for initial subsergences of 6 feet and -2 feet j respectively. '.Y I f { I t g

~. l ' ( Increasing the submergence tends to increase the maximum dry well pressure as is shown by comparing runs 8 and 12. Run 8 with a submcrgence of 6 feet had a maxf:num dry well pressure of 28 psig, but run 12 with a submergence of 12 feet 5-inches had a maximum dry well pressure of 38 psig, e. Dry Well Volume A change in dry well volume had little effect on maximum dry well pressure for the conditions tested. This conclusion is consistent with other indications that vent flow resistance controlled the peak dry well pressure. The effect of dry well volume is indicated by comparing some of the first twelve runs with similar tests made later. Between tests 12 and 13, the dry well volume including vents was reduced from 326 3 to 248 f t. The following t?ble lists pertinent information on this matter, for orifice diameter of 1.64 inches and initial submergence of 6 feet. Dry Well Internal Max. Dry Well Dry Well and Run Arrannement Pressure osia. Vent Volume 8 C 28 326 ft3 25 C 33 248 26 C 34 248 .I 5 A 40 (first max. 326 is 32) 15 A 33 248 24 A 32 248 36 A 35 248 6 3 23 326 7 B 26 326 27 5 25 248 l 28 3 25 248 l f. Effect of Dry Well Internals The dry well internals used affected the ar.ount of moisture carryover, the time air left the dry well, and the entrance loss for flow from the dry well into the vents. Figure 6 shows the arrangements used. In addition, arrangement A was tested (run 37) without the deflector plate to measure its effect on maximum dry well pressure. The effects of air and moisture carryover have been discussed l, previously. s 18 - l I

-l ~ The deflection' plate at the vent entrance increased the maximum dry well pressure from 33 pois (run 37) to 35 psig (run 36). 3 Effect of condensation on Dry Well Valls and of Internal Dry Well Tea rsture Maximum dry well pressure is not significantly affected by f condensation on the dry well walla for orifice sises of 1.64 inches or bigger. Condensation may not be significant for smaller trifices either, but test dats is not available f on this question. g Comparison of pressure traces for tests with different initial dry well temperatures is the best indication of the effect en dry well pressure. Runs 27 and 28 are identical la initial conditions except that the starting l dry well toeperature was 54' F ta one case and 89' F in the other; the dry well pressure traces are identical. Runs 38 and 39 have the same initial conditions except for dry well temperatures of 74 and 113' F; the same maximum pressure of 33 psig was reached in the same. length of time. Rens 4 and 12 can be compared for the first 0.25 I seconds, but not much later beer.use of the different i i initial depth of vont submergence. The initial dry well temperature was 103' F for run 8 and 193 for run 12. At the end of 0.23 seconds, the dry well pressure was 22 peig for both. i i e a + 1 k I\\ ~, 19 i L i h! Ii A

C. Vent System 1. Conclustons Pressure at the end of the went was probably not critical. a. Calculated critical pressures using either homogeneous or L slip models were substantially different from measured values. Measured values of vent and pressures were questionable, however. ( b. The homogeneous flow model for steam-water mixtures l predicted measured pressures in the vent very well except at vent discharge. i 2. Vent Flow Resistance The follouing table presents flow resistance of the vents, between the dry well and the water pool to terms of equivalent length of 14-inch pipe. ' Numbers represent the best estimate, using available Laformaties on single phase flow. The equivalent length of 14-inch pipe was obtained from the K factor by using a friction factor of 0.01. Straight length of 14-inch pipe 51 feet Retrance from dry well including 93 guard plate Tee 64 Long Redius, ett 22 Rapaastoa joint 7 i short radius all J i 272 feet 3. Flow Conditions at Test Init The asasured pressure at the end of the vent pipe probably did not repruent the true static pressure at this point. In all test ruas, the measured pressure at the vent exit was fairly constant durtag the time water was being expelled from the reacter vessel (Phase B), but the measured static pressure rose af ter steam esty was flowleg from the reactor vessel (Phase C). This behavior could be expiataed by the water pool around the vsat in most cases, but the sans behavior was noted when the 20 - 1 O

I l l + vent pipe was initially uncovered as in tests 30 and 32. The I most probable explanation is that the pressure tap in the vent S exit was installed in auch a manner that it was affected by t the velocity and demsity of the flowing fluid. l } Further doubt is thrown on the accuracy of the pressure 1 1 measurement at the vent exit by lack of agreement with the 1 ) suppression chamber pressure at the end of some runs. For i example, at the and of run 30 the suppression chamber pressure reads 10.5 psig while the vent exit reads 5.7 psig. The change in pool water level during a test with the vent initially submerged would cause a difference of about 0.5 pais but the y direction of this change is different from the observation. i The discrepancy anay be caused by a change during a test in l density of the fluid in the 6 foot line from the vent exit to the pressure transducer. Flow from the vents was apparently not critical on the basis l of test data and calculated critical pressurss. The following table illustrates this point for a few test runs including run 33 with the highest flow rate. Flow from the vent was the average calculated as described in Appendix II. The measured vent outist pressure was corrected for a water leg of 6 feet. critical pressures were calculated by both a homogeneous model and a slip model,k Comoorison of Measured Vent Exit Pressures With l Calculated Critical End Pressures'

l (Enthalpy Equals 580 Etu/lb for calculations)

I Run 15 16 17 30 32, 33 35 2 Mass Velocity,1bs/sec. f t 92 150 204 92 139, 275 46 Maast$ red Vent End Pressure, 23.6 21.3 22.3 17.4 16.7 23.3 21.3 ' i Psia. Calculated Vent End Pressure 16.8 27.0 35.8 14.8 25.0 47.5 18.5 (homogeneous) Psia. Calculated Vent End Pressure 11.2 18.0 23.9 11.2 16.7 31.7. 12.3 (slip) Faia. l Iai 65739, " Steam-Water Critical Flow Using the Separate Flow Model", l by W. A. Massena, June 10, 1960. Ii 1 1 ,\\

. - ~ - - - 4. Preticure Drop BeYween Dry hell and Vent Exf t Prelimirary evaluation, but not detailed analyscs. of pressure measurements in the vents has been made. Detailed evaluation of the pressure drop data is beyond the scope of this report bec,tuse of the quantity of data and the many ways in which it can be interpreted. The following table illustrates the cifect of flow rate into the vents and the relative pressure drop in each part of the test system. Average flow was calculated by taking the initial reactor veJsel muss minus the amount of water remaining fu the dry well :sud dividing this difference by the time rect,rdes for expulsion of water from the reacto: vessel. Average pressures were obtained from the traces by choosing the timo as the ridpoint between the start of the test and the time water was expelled 1 from the reactor vessel. Average Vent Pressures and Flow Rates I Run 13 15 16 17 2,2 33 Flow,1bs /sec. 51.1 87.5 144.4 191 47.2 263 ~ Dry Well, pais. 23 27 52 80 16 120 ) hP, Dry tell to Vent Inlet 6 4.5 '.7,,.. 10e 2 18 \\ ] Vent Inlet, psig. 17 22.5 45 70 14 102 l & Vent Inlet to T 2 '2.5 9 24 1 ) Af ter T psig. 15 20 36 56 13 i i AF T to Vent Outlet to 14.8 31.6 51 6.6 Yent outlet, peig. 3 6.2 4.4 5 6.4 7.5 4 F h u 2.) = .g e e l l I - r, #we w.

l Cood correlation between test at.d calculated dry well pressures has been obtained for the six test runs in the preceding table. The method of calculation used a homoger:ous model, constant l enthalpy expansion at 580 Btu /lb (equal to saturated water at 1250 psig.) and a vent end line pressure of 20 psia. The !i following table shous the agreement for three runs of different l flows. Pressures for the other runs of the previous table have been estimated on the basis of the calculations for rune 15, i i 17 and 33. Agreement is best at high flow rates. ll Run 15 17 33 Flow Ibs/sec. 87.5 191 263 I! 's Dry Well, psig Test 27 80 120 Calculated 28 79 120 i Vent inlet, psig Test 22.5 70 102 Calculsted 20 64 100 After T, psig Test 20 56 Not Nessured Calculated 16 58 92 5. Effect of Air on Vent Flow Runs 40, 41, and 42 were conducted to determine the effect of adding air to the dry well shortly af ter the test began. The primary purpose was to help demonstrate that air from a pressure suppression dry well could not significantly interfr,re with steam condensation. In these three tests the auxiliary sk receiver was connected to the dry well. Before a test the auxiliary air receiver was pressurized with air. About five, seconds af ter a test rupture began, a quick opening valve was opened allowing the air from the air receiver to flow into the dry well. The initial masses of air in the dry well and air receiver were approximately the same in runs 41 and 42, and in run 40, the = air receiver had somewhat less air because of a lower initial pressura. 9 The test traces show that the sudden addition of the air to the dry well had little effect on:the flow resistance in the vent and consequently little effect on the dry well pressure. The mass flow rate of air into the dry well in the first second was about 101 of the mass flow of steast-water into the vents. t The effect on dry well pressure was to increase it by about 10-15%. _., Further analysis of the test results of flow of air-steam-water is probably desirable, but is beyond the scope of this report. l c 1-S

j D. Suppression Chenher 1. C<me tusiona a. m tests show that the Humboldt suppression chamber design r would perform satisfactorily with a large margin of safety. b. Steam was rapidly and essentially completely condensed even though: (1) the vent was initially uncovered, (2) the pool water was hot (140-160" F), (3) buge quantities of air flowed with the steam-water into the pool. c. Water hanner was not appreciable in any tests, d. Mixing of the pool water was excellent. t 2. Suopression Chamber Pressure vs. Time Suppression chamber pressure started to rise rapidly very soon af ter the dry well pressure started to rise. In most testa pressure rose rapidly reaching an initial peak in about half a second; pressure then declined rapidly for perhaps another half-second and finally rose more slowly to the maximum. N tine the maximass was reached depended upon the time air left the dry well, but it usually took many seconds. Following the maximus, the pressure remained nearly constant, balancing the vepor pressure of hot water remaining ta the bottasi of the dry well. The early pressure peak in most tests is readily explained by considering the action of the air and water. N air above the water is compressed like gas in a cylinder by water in the pool acting as a pistan. '1he piston of water is driven by the air and water below it coming from the vent. Air leaving the vent expania rapidly in the pool throwing the mass of water abwe it upwards. The air initially above the pool is compressed and acts as a spring. As the air from the vent slips throagh the water, the water or piston falls back and the suppression char.ber pressure falls of f. N explanation is substantiated by two obs trvations, first, the initial peak did not occur in any tests whara the vent was initially y l uncovered. Secend, the height of the initial pressure blip is greater for large.r orifices. An analysis to predict the height of the blip has not yet been developed, but would be very useful u. I i e \\

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in support of design of preer.ure suppression systems. 3. Pool Aerion The action of the water pool is shown by the sequence of pictures shown in Figure 9. Movies were taken through an open manhole at the top of the suppression chamber during l runs 38 ar.d 39. The s.ovies were taken at 128 frames per second. Figure 9 was prepared from the movies by taking every fifth frame and mounting the still photographs to read sequentially as in a book. The surface of the water can be seen with the 14-inch vent pipe at the bottom of the pictures and the walls of the suppression chamber extending on both sides. The water surf ace begins to be disturbed by the fif th picture. Subsequent pictures shou the water being thrown up and then falling back down. A large amount of water appears to be thrown as high as 15 feet above the initial surface of the water. In other tests with the suppression chamber closed, the pool could be observed through a glass port at the top of the supprussion chamber. Water was thrown about two-thirds as high with the closed chamber. The tesiperature of the water in the pool was fairly uniform before, durias and af ter tests. (' 4. Condensation of Steam in Uster condensation of steam in the water was rapid and complete. This conclusion is based on the data in Table V (page 26 and 27) ubich compares the maximum measured suppression chamber pressure with a maximum calculated value using test conditions and the meaumption that all steam was condensed. If a significant amomet of uncondensed stems were present, the measured pressure would have been higher than the calculated pressure. The calculated pressure of Table Y was determined with the following condition and methods.

s. All air in the dry us11 and wants was transferred to the

] suppression chamber above the water pool. i

b. The taitial dry well air temperature is as shown in Table 1 of the Appendix.

c." The averages of the initial and final temperatures in the suppression chamber are the true =*==. 25

i TABLE V Maximum Suppression Chausber Pressures Calculated From h liessurgd Data 5 7.0 9.4 7 8.0 8.8 8 8.5 8.6 9 7.5 8.3 10 6.5 8.8 12 8.0 9.8 i 13 8.1 7.'2 i 14 7.5 7.4 15 8.8 8.7 16 8.0 8.4 17 8.5 7.9 18 4.0 6.4 i '.5 6.6' 20 6 21 8.8 9.7 22 7.5 8.9 e 24 9.3 9.4 25 9.3 9.1 26 8.5, 9.0 27 8.0 8.0 28 7.8 8.0 29 7.0 6.9 8-y e e

e P,

g 6 e l i

) i G TABLN V (Continued) calculated From Run Measured Data 30 14.5 10.2 31 5.0 7.6 32 7.2 6.9 ) 33 8.5 7.9 34 6.5 7.5 l 35 8.0 . 7,.9 36 8.2 8.5 37 8.0 8.3 40 11.5 11.2 41 12.5 12.9 i 42 13;6 14.0 43 6.5 6.4 44 7.5 7.2 45 7.8 7.6 r s i l I

~ I I s d. The suppression chamber is leak tight. .3 e. Air in the suppreaston chamber is saturated with water vapor before and af ter a test. j f. The suppression chamber vapor space decreases by the j amount of water transferred from the reactor vessel. i Comparison of the measured with the calculated values shows i good agreement in all but a few cases which will be j discussed later. { Probably a small cause for differences was in the temperatures 's assw.ed for the calculations. The average of measured temperatures may not have been the mean, and the time of the temperatures could have been different from the time of the asair.um measured pressure. j 4 1 Some air may have stayed in the dry well which would cause the measured values to be lower than the calculated. It is ^ of interest to note that for runs 5-12 with a larse dry well, the measured presrure was always lower than the calculated. j After the dry well was reduced in stae (runs 13 and on), t t there was no Landancy for the calculated pressure to be either E l higher or levar thus the measured pressure. Air leakage was negligible. In a special test, to det-i== J the ichk tightness of the suppreesian chaber, the chasher 0 was filled with air to e pressure of 18-inches of mercury. } After 20 minutes the pressure had dropped to 17.9 inches of ( f mercury. 1 Condensattee of steam em the walls of the suppression chsaber, 4 could not have been a sesjor source of error. Tests were made 1* in which measured amounts of steam were bleum into the vapor 4 gl epace of the suppressica chamber and the chamber temperatures measured. If the experisestally datav=imad condensettaa rate were to have occurred la run 15, it would have reduced the t mart=== suppression chamber pressure S. g 5. Effect of various Parameters on condeaaatisp a. Flow Esta The rate of flow from the vest did not affect the d===attaa within the large range tested. Flow rate from the vent ramsed from 0.23 lbe/sec. Crum 31) to 263 the/sec. (rum 33). j n===inariam of Table V does not show any consistaat variation j with flew rata between the measured and calculated==-t-N A "* ih.,, - , j.,.- l J l,.: ~ : l / - l s a 6

suppression chamber pressure. b. J.oot Temperature Steam was condensed rapidly and completely even though the water in the pool was much hotter than the Humboldt design conditions. The Humboldt pool has an initial design temperature of 80' F with a final design temperature of 115' F. Test 26 i was run with conditions simulating the Humboldt maximum credible operating accident except for an initist pool temperaJ ture of about 138 F. The average temperature of the pool af ter the test was 1618 F. Cowarison of the observed and calculated maximum suppression chamber pressures shows that the steam was efficiently condensed in the hot pool water. c. y p,te r C a i r m e r h amount of water carried over with the steam from the dry well did tot affect condensation. A wide rance of carryover was obtained in the tests. For example, t in 24 had 84% of the maximum possible carryover while run 25 had 11%. The variation in suppression chamber pressures with uoisture carryover is not signifie sne. d. Air With Steam Large e.nounts of air with the steam-water did not pre. cat rapid and comriste condensation. This conclusion is based partly on ruas 7, 27, and 28 ubers the air left the dry well relatively late, and largely on runs 40, 41 and 42 with special equipment. In runs 40, 41 and 42 an air receiver with a volume of 38.1 embic feet was connected to the dry well by a short length of pipe containing a quick openiss yalve, h air receiver was pressurised before a test. Seconds af ter the rupture disk blew, starting a test, the valve was opened allowing the extra air to enter the dry well and join the steam-water entering the vent. N initial mass of air in the receiver for runs f.!L and 42 was about the same as the initial mass of air in the dry well. The initial temperature and pressors of the air receiver are as follous: Ron 40 41 42 Initial Fressure, peig. 65 91 91 Initial Temperature.

F 63 69 71

+ Transient pressure in the air receiver is shown as the pressure f traces in the appendix. E==f antion of the data shows that the added air did not interfere with the caad==ation of the steam. l

i 1 { ? [ ; e. Vent Submercance Vent submercence before a run was varied frca 12 ft. 5 inches (run 12) to minus 3 feet (run 30). The Humboldt design i ; submergence is 6 feet. Run 32 is the most extreme condition testod with complete condensation. Here the vent was initially 2 feet above water and the orifice was twice the area corres-ponding to the Humboldt maximum credible operating accident. I Incompleto condensation was observed only in run 30 with the j vent initially 3 feet above the water and the orifice corres-ponding to the Humboldt M.C.O..A. The observed mawimum pressure was 4.5 poi higher than the value calculated assuming complete condensation. The suppression chamber pressure rose above the j-calculated value after the water had been expelled from the reactor vessel. Apparently steam-water jetting into the pool will condense, but steam waf ting from the vent may escape uncondensed if the vent is several feet above the water. 5. Vibration in suppression chetsg No serious vibrations wars observed in any of the tests, as contrasted with some previous tests with the Condensing Test Facility.1 An observer at the top of the suppression chamber could definitely feel the structure shake beneath him, but with-out having a sense of danger. A slight water hammmer oss noted about about 10 minutes after the start of the test in run 31 with an 0.14 inch orifice. Rather strong water hammer was noticed throughout run 34 with an 0.6 inch orifice. gince both these runs had small orifices and small fivw rates, the water ha-r was probably caused by the intermittent action of condensation inthe vent pipe followed by expulsion of the hot saturated water in the vest. 6. Bumboldt Sueore. ston Chasber Desian ( The Rumboldt suppression chamber has 1sege margins of safety as iv.dicated by the tests. h design pressure for the Eumboldt suppression chamber is 10 pois, but it will withstand considerably higher pressures because of other design considerations. N maximas test pressure observed with conditions sianalating the l i maxismas credible operating accident was 9.3 peig. Many tests were run with conditions far more severe than the Humboldt design. 1 GEAP 3143 " Test Report for Pressure Suppression Development Prograsf'., by Fiock, Janssen, and Steamer, April 2,1959. q 30 - Sem ,,m.__

) APPENDIX I Tabulation of Test Data and Results The following table summarises by run the conditions of the teste, measured data, and some calculated results. Where blanks occur, no data was obtained. j l 1. Orifice diameter located between the reactor vessel and the- ) dry well. l 2. Initial water voluna in reactor vessel calculated free observed water level and "as constructed" drawing of the vessel. 3. Initial pressure in reactor vessel as measured by a Heise sage just before the test basan. 4. Temperature at top of reactor vessel (*F) as measured by thermocouples and recorded. During most of the tests the recorder tended to drifc very slowly a few degrees'during heating up. 5. Temperature meascred near middle of reactor vessel. 6. Temperature msg red near bottom of raactor vessel. 7. Temperature meas. red at the bottom of the reactor vessel near the 6-inch discharge opentag. l 8. Dry well internals indicated by letters are described by Figure 6. 9. Volume of dry well and the vent up tb the initial suppression pool level (or the end of the vent when the vent was uncovered to begig with).

10. Initial dry well tes.perature measure.1 near the top of the dry well before the test started.

l

11. Final dry well temperature measured when the reactor vessel-and dry well pressures were equal.

12. Maximum dry well pressure as determined from the pressure traces.

13. The water remaining in the dry well af ter a test was measurede by draining it into a calibrated container.

I-1 i i ev ,.------,n

] 1 t 1 A 1 M 1.1 2 D M 1. 1.64 1.64 2'.10 2.32 l'.64 1.64 1.64 1.64 ' 2. 39.25 39.15 39.1 38.47 38.7 38.7 38.25 39.6 3. 1250 1250 1250 1250 1250 1250 1250 1250 4. 570 572 574 574 574 574 574 569 5. 363 567 570 .570 570 568 571 565 6. 553 570 563 563 565 564 566 560 7. 541 561 554 549 556 547 547 543 8. B C C C C C D E 9. 326 326 326 326 3'6 326 2 2'8 4 ~ 48 2 10. 159 103 184 204 131 195 64 78 11. 204 236 23 6 237 235 237 236 228 it. 26 28 45 57 38 32 32 13. 44 115.5 106 100 88 78 14. 65 8 15 19 28 38 15. C C C C C C C C 16. 56/82 84/95 89/113 99/118 86/97 89/109 78/86 75 17. 56/78 84/100 90/110 99/113 84/106 88/103 75/90 74, 18. 58/97 84/92 88/98 96/109 87/96 110/105 76/82 74/90 19. 68/89 85/103 94/105 103/116 42/90 88/96 79/99 86/108 20. 55/91 77/102 80/109 87/120 99/117 69/100 80/102 89/112 21. 54/90 78/105 79/109 87/121 98/117 68/100 79/101 88/112 22. 44/74 72/88 74/108 89/117 79/110 66/101 78/98 86/111 23. 8.0 8.5 7.5 6.5 8.0 8.1 7.5 24. 32 25 88 79 87 25 76 25. 18 18 18 18 15 24'5" 18 18 36 6 6 6 6 3 12'5" 6 6 27. 650 650 650 650 715 - 508 650 650 28. 30.14 30.13 3 0.13 30.13 30.27 30.27, 30.15 30,15 1-4 ^

J.1 ,1_6 17 18 19 20 g y 6 1. 1.64 2.32 2.84 1.64 1.64 1.64 1.64 1.10 2. 39.25 39.37 39.37 38.7 39.15 38.7 49.81 49.37 3. 1250 1250 1250 1250 1250 1250 1250 1250 4. 574 574 574 574 572 574 574 574 5. 570 573 569 570 567 570 569 570 6. 547 567 569 565 567 569 569 7. 549 544 550 557 537 555 548 558 8. (A) (A) (A) (A) (A) (A) (A) (A) l 9. 248 248 348 254 248 254 248 248 i 10. 53 110 1M 57 98 102', 56 125 11. 233 233 229 214 219 227 240 248 12. 33 64 90 32 34 34 33 20 13. 31 23.5 18 29 27 31.5 48 14. 75 82 87 77 77 81 70 15. C C C 0 0 C C C 16. 73/86 84/109 90/104 78/87 84/101 86/107 75/109 92/125' 17. 73/94 84/107 89/105 75/89 75/92 84/104 73/104 98/116 18. 73/124 87/125 90/117 79/87 81/99 88/102 75/120 101/138 19. 94/116 107/116 109/108 75/82 74/93 80/90 83/108 116/121 l 20. 97/121 111/122 78/113 78/118 62/94 70/112 87/115 89/133 21. 96/120 104/121 77/113 82/118 62/95 70/114 86/114 87/130 22. 98/121 66/122 69/113 80/111 59/94 70/114 67/116 79/129 23. 8.8 8.0 8.5 ' 4.0 6.5 8.8 7.5 24. 70 87 86 60 81 78 70 84 15. 18 18 18 11.5 18 11.5 18 18 26. 6 6 6 -0.5 6 -0.3 '6 6 27. 650 650 450 792 650 792 650 650 28. 30.12 30.12 30.12 30.12 30.12 30.12 30.15 3 0.15 i L d .... ~,- _ -.-- - -. ---

l I h n M E D D E E 'I 1. 1.64 1.64

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196, 14.

84 11 58 60 ' 78 74 0 i l U. C C C C C C C C l l 16. 78/11) 89/124 300/134 70/90 78/105 69/94 75/128 88/116 17. 79/108 88/124 99/132 70/87 77/100 69/92 72/126 85/113 18. 82/125 94/124 103/140 73/97 41/103 73/94 75/123 86/105 19. 92/114 124/147 137/157 75/104 92/106 66/87 70/123 87/115 20. 97/118 127/144 141/170 80/106 68/107 74/130 69/144 89/107- ~ l 11. 96/118 127/15 1 141/162 78/102 66/103 74/132 69/149 90/108 l 22. 81/118 125/148 135/155 81/107 64/111 73/131 66/118 90/107 23. 9.3 8.5 8.5 8.0 7.8 7 14.5 5 34. 68 45 90 64 79 70 79 82 25. 14 18 18 18 18

10.5 9

18 26. 6 6 6 6 6 -1.5 -3 6 27. 650 650 650 650 650 - 813 846 650 28. 30.24 30.24 30.24 30.05 30.05 30.29 30.29 3 0.29 M s I

22 21 2.4 35 36 21 28 y I 1. 2.32 3.28 0.6 1.1 1.64 1.64 1.64 1.64 2. 39.2 38.7 38.7 39.2 39.2 39.2 39.2 39.2 ( 3. 1250 1250 1250 1000 1250 1250 1250 1250 4. 573 574 574 551 574 575 574 575 S. 571 569 570 549 572 572 572 573 6. 566 564 566 544 567 568 567 567 7. 554 549 564 540 547 553 550 550 A (Without Same Same Deflector) As As 8. A A A A A 261 37 37 9. 254 248 248 248 248 248 248 248 I 10 62 115 114 62 70 88 74 - 113 I 11. 239 229 235 245 235 233 100 224 12, 59 128 10 18 35 33 32 32 13. 23 14 67 29 36 26 14. 78 89 48 77 72

80 s

l i 15. C C C C C C 0 (Hovies) 0 (Movies) l k i 16. 82/104 89/99 94/110 85/102 79/100 79/102 17. 82/103 89/100 94/107 85/100 77/97 79/101 74/100 83/102 18. 82/103 91/132 98/114 85/103 78/116 81/116 77/121 87/117 19. 80/99 113/123 104/106 94/111 84/106 94/105 92/111 as,ist 20. 84/131 116/129 78/107 89/112 85/112 81/112 91/117 79/111 i l i 21. 83/130 115/129 77/107 87/113 84/112 79/112 88/115 77/112 l' i 22. 81/130 74/129 74/94 83/108 84/108 69/109 78/114 76/112 l 23. 7.2 8.5 6.5 8.0 8.2 8.0 24. 72 85 90 72 80 25. 10 18 18 18 18 18 18 18 26. -2 6 6 6 6 6 6 6 l 27. 824 650 650 650 650 650 650 650 1 28. 30.22 3 0.22 30.22 30.20 30.06 30.06 30.11 30.11 k 1 1 1 1~ J f. s

Lee

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) Auxiliary dry well connected with quick opening valve.. 1-8 t M s 'i' - ..-.,,,,------~~.w -wm-wv-~-'* ~ ^ ^ " " ' ' - '

i APPENDIX II Average Flow Rates freer Reactor Vessel and Into Vent From Dry Well .l L The following table summarizes, calculated values of average flow l rates during the tests. The average flow from the reactor vessel was determined by dividing the uneasured initial amount of water in the reactor vessel by the time required for all water to be expelled (end of Phase B). This time is indicat'ed by an abrupt change in slope of the pressure trace shoering reactor vessel pressure vs. time. The average total mixture flow into the vent from the dry well was determined by dividing the initial reactor vessel water minus the smount collected in the dry well (item 13, Appendix I) by the time required for all water to be expelled from the reactor vessel (end i of Phase B). _I l < 1 No consideration was taken of the change in mass ci steam in the f! reactor vessel during Phase B; this factor would decrease the calculated j flow rates in the order of 31. h 1 ~ t 2 1 i 1 1 l s 3 I. L IIh1 4 l

l l.. il el d CALCULATED AVERAGE FLOW RATE FROM REACTOR AND INTO VENT [ t Flows from Flow into Reactor Vessel Vent Run 1bs /sec. . ibs /sec. 1 2 59.9 52.4 3 104.5 102.9 4 96.8 96.6 5 100.5 97.8 6 101 77.7 7 101 80.6 8 102.9 48.2 9 141.7 72.5 10 158.5 84.2 11 12 107.4 13 106.2 55.* 14 15 102 87.5 16 161.9 ' 144.4 17 208. ~. 191. 18-102.3 88.5 i l 19 101.1 20 - 100.5 87.9 . f _ e'- 21 100.5 89.1 22 56.9 .47.0 ' ~i ' j.,.? F :,. j ;;..: '._,, ' 'l " * -}~ 'W: ~..- II-2'....: O g e g ( i ~- -- -* ... ~. -~ -- - 3.~ _. -.... - 1 ~ 1 [_ e--.-----w--qwc-m- * - ' ' =

I ( ~ Flow From Flow into I Reactor Vessel Vent Run 1bs /sec. Ibs/sec. 23 24 100.2 90.9 25 102.3 48.5 26 102.6 27 100.5 75.7 28 101.1 77.1 29 102.4 92 l 30 99.6 87.9 31 1.02 .2E3 32 152.7 133. 0 i 33 281.7 263.3 34 21.1 35 55.8 44.0' 36 102.4 66.1 100.6 67.3 37 38 106.1 93.4 39 102 40 102.9 ~ 87.3 86.8 41 101.7 42 101.1 ~ 43 4.7 44 104.3 89.1 { 45 162.8 143.4 ~. II-3

N F. t l 8, APPENDIX III . / - l ( Pressure Traces i, l b This appendix contains half size reproductions of the pressure traces obtained with a Visicorder and graphs of three runs that } were too long to photograph conveniently. The run number and l time scale (for the origi: al rather than the reproduction) are shown { on each sheet. The iderury. tad pressure scale for the individual g runs are described belev. Lot.stion is distance from the bottom of J I ; the original. Scale r'f err, tc the original. The traces are inter-rupted periodically in sequene.3 by the recorder so that traces that g are close to each other, or.hich cross, can be identified. I i Location of Traces Runs 1-12 . ( Interruption [ Item Location Scale Order i Suppression Chamber 0.5" 10 psi / inch 7 Dry Welt 1.0" 50 psi / inch 2 I[ Vent Line Outlet 1.5" 12.5 psi / inch 8 Vent Line Entrance 2.0" 50 psi / inch 1 Vent Line Af ter T 2.5" 20 psi / inch 5 a 1 nl . Discharge Tube 3" 50 psi / inch 6 ~ g,l d;l Reactor Vessel Flange 4.5" 500 psi / inch 4 I Reactor Veseel Loop 5" 300 psi / inch 3 h ,1 } l ![ j 'l ? fg ii i 111-1 , I;iJ t 4l-U' r f f l

Location of Traces - Runs 13 to 45 Except 24, 25, 31, 34, 43, 40, 41, 42 l i l t Interrupter Item Location _Sc ale Order Suppression Chamber 0.5" 10 psi / inch 7 Dry Well 2.0" 50 psi / inch 2 Vent Line Outlet 1.5" 12.5 psi / inch 8 Vent Line Entrance 3.5"

50. psi / inch -

1 Vent Line After T 1.0" 20 psi / inch 5 Discharge Tube 3" 50 psi / inch 6 Reactor Vessel Flange 5.0" 500 ps1/ inch 4 Reactor Vessel Loop 5.5" 300 psi / inch 3 ) i For runs 24 and 25, there is no trace for the vent line after the ' T; the vent line entrance has a location of 1.5 inches with a scale of 20 psi / inch and an interrupter order of 5. In runs 40, 41 and 42, the discharge tube was not measured. The transducer was used instecid to meassa the pressure in the auxiliary air receiver connected to the dry well. The auxiliary dry well for runs 40, 41 and 42 then has an initial location of 3-inches and a scale of 50 psi / inch. The traces for runs 31, 34, and 43 have been replotted because the length of traces made photographing rather awkward. No pressure traces were obtained for runs 11,14 'and 23. i l 1 ux-2 4p p me , -M., - #,..... :l. : ) - ~ ~~ 1 ~~ - ~ ~~~.~' = 'w ~ ' ' " ' =

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