ML20206R931
| ML20206R931 | |
| Person / Time | |
|---|---|
| Issue date: | 08/31/1998 |
| From: | Damon D NRC |
| To: | |
| Shared Package | |
| ML20206R845 | List: |
| References | |
| NUDOCS 9905210016 | |
| Download: ML20206R931 (65) | |
Text
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IAEA Internadonal Conference on Topical Issues in Nuclear, Radiation, tnd Radioactive Waste Safety j
Vienna, Austda -- August 31-September 4,1998 i
APPLICATION OF INTEGRATED SAFETY ANALYSIS TO NUCLEAR FUEL CYCLE FACILITIES Dennis R. Damon U. S. Nuclear Regulatory Commission T8D14 Washington,DC 20555
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United States of America Abstract In order to assure that a comprehensive and documented safety basis exists for fuel cycle facilities, the U. S. Nuclear Regulatory Commission staff has encouraged performance of systematic safety l
analyses. These analyses have the purpose ofidentifying all potential accident sequences, then evaluating and l
documenting te items relied on for safety in preventing or mitigating these sequences. One characteristic l
sought in the;c analyses is an integration of radiological, chemical, nuclear criticality, and other safety controls. Although the current regulations do not explicitly require it, several major U. S. fuel fabrication facilities are performing these htegrated safety analyses (ISA). The paper discusses the objectives of this regulatory initiative, how Integrated Safety Analysis is to achieve them, and aspects of the analysis that pose l
challenges in practical application. Among the more significant of these practical challenges have been: 1) producing descriptions of processes and their safety controls that effectively define why the controls make the process safe, and 2) developing efficient and consistent methods for evaluating the reliability of safety controls.
- 1. BACKGROUND AND INTRODUCTION l
l Regulations governing safety of U. S. nuclear fuel cycle facilities have not, unlike those for nuclear reactors, l
required a commitment by the facility to detailed hardware design criteria for each process. This is so, in part, because the process hardware at such facilities has greater diversity, and is subject to more change, than nuclear reactors. Design information is submitted during licensing of the facilities, but this information is not required to be kept current. As a result of serious incidents at U. S. nuclear facilities, the Nuclear Regulatory Commission (NRC) became aware of the need for more current information, and of the need to include an integrated assessment of nuclear criticality, chemical, radiological, fire, and other safety hazards in the overall review of fuel facility safety. One response to these incidents was the initiative to require Integrated Safety Analyses (ISA) by major fuel cycle licensees, including commercial fuel fabrication facilities. The component tasks that comprise an effective IS A will be described below. How the results of the ISA can be used to achieve a current and adequate safety basis will then be discussed.
- 2. INTEGRATED SAFETY ANALYSIS By ISA, the USNRC s,taff means an analysis identifying all accidents that might occur in a facility that could lead to consequences of concem to the agency, and which identifies the items relied on for safety for protection from these accidents. ISA also includes an evaluation of the adequacy of these items relied on for safety (also referred to as safety controls), and correction of vulnerabilities. The analysis is performed using proven systematic methods, and with integrated consideration of radiological, chemical, nuclear criticality, and fire hazards.
The component tasks in an ISA are, in order: documenting process safety information, hazard identification, process hazard analysis (accident sequence identification), evaluating accident consequences, documenting 1
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and evaluating formal safe.y controls, and evaluating acceptability of risk.
J Current and accurate process information is needed to permit safety analyses to be performed. Hazards are the specific items that are the sources of danger, such as toxic chemicals or sufficient fissile material to
- permit accidental nuclear criticality. Process hazard analysis (PHA) is application of an appropriate systematic method, by a team of analysts qualified in the relevant disciplines, to identify all sequences of events that could lead to consequences of concern. The types and magnitudes of consequences of concern are necessarily specified in advance. Usually an accident sequence leading to such consequences involves failure of designed safety controls. The next' step in ISA is to determine the types and magnitude of consequences of the identified accidents. Finally the adequacy of safety controls is evaluated based on acceptance criteria graded according to risk. The concept of risk-grading simply means that controls to address accidents of higher consequences are to be of correspondingly higher reliability. Although Probabilistic Safety Analysis (PSA) is one acceptable method of assessing accidents, other less quantitative methods are also acceptable.
There are several primary results from an ISA. One is the documented Process Safety Information, which provides a description of the processes and system interfaces suitable for assessing safety. Another is a list specifying the items relied on for safety (controls), their safety limits, characteristics essential to reliability, and support measures to assure that they are available and effective when needed, such as maintenance, configuration management, and monitoring. A summary of the process hazard analysis, formatted so as to show that completeness has been achieved in identifying all accidents is also an essential result. Calculations supporting accident consequences, and information supporting the reliability of safety controls are also products of the analysis.
- 3. WHAT INTEGRATED SAFETY ANALYSIS ACCOMPLISHES When the component steps in the ISA are executed adequately, the results of an ISA form a logically
. complete demonstration of the adequacy of a facility's designated safety controls. For this reason, these results constitute an acceptable and documented safety basis. Maintenance of this safety basis in a current state thus provides continuing assurance to facility management and the regulatory agency, that public safety is being protected. The integrated assessment of chemical, radiological, and nuclear criticality hazards and controls assures integrated consideration of the adequacy of safety controls, accounts for potential interactions between hazards and controls, and recognizes potential tradeoffs involved in controls When changes are made to safety controls, an ISA of the change would be conducted and the descriptions of these controls kept on file at the regulatory agency would be promptly updated. This would provide the regulatory agency the opportunity to confirm, by review or inspection, that the change did not degrade safety. Thus the objective would be achieved of avoiding long periods of time in which operations were conducted with inadequate safety controls in place.
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- 4. CHALLENGES IN APPLYING ISA Since a number of facilities are in the process of performing Integrated Safety Analyses, lessons are being learned about each of the steps in the analysis. Discussion of some of these lessons follows. Although Process Hazards Analysis (PHA) is a central and time consuming task in an ISA, most applications have not j
encountered difliculties here. This is true because the techniques used in PHA have been used intensively
]
throughout the U. S. chemical industry. Thus effective methods, guidance, and training exist for these techniques. For other steps, there is less relevant experience, hence challenges exist.
4.1 Documenting Processes and Safety Controls In order to establish and maintain safe processes, complete process safety information must be kept current
m... e at the facility. A summary of this information needs to be submitted as part of the ISA results sent to the NRC. The descriptions of both the licensed process and its safety controls need to have sumcient detail to demonstrate to the NRC license reviewer that the safety controls are adequately reliable. Normally these descriptions would include identifying the controlled process parameter, safety limits and margins for that parameter, and the reliability characteristics of the hardware or procedure relied on for safety. In practice, it is dimcult to strike a balance between too much and too little detail in these descriptions. The purpos,e is to explain the safety basis, not provide a design or operating manual. Because this task is dimcult, training in technical writing and consideration of where to strike the balance would appear to be appropriate preparatory measures for ISA.
4.2 Evaluating Adequacy of Safety Controls Once the ISA has established the items relied on for safety in a process, and the consequences should these items fail, it remains to determine whether these items have sumcient reliability to prevent or mitigate the consequences. The challenge in this step is the need for efficient and adequate methods for evaluating the reliability of safety controls. Traditional quantitative reliability evaluations require detailed modeling plus application of data from experience. Because there are typically hundreds of safety controls at fuel cycle facilities, quantitative evaluation of all of them would require substantial effort. On the other hand, holistic engineering judgment is subjective, hence inconsistent, and may be wrong. What is currently being sought in this area are methods that, while emeient, make use of some of the objective information considered in reliability analysis. For instance, such information includes facility experience with failures in similar equipment, and established functional surveillance time intervals. Pooling international experience in this area may offer valuable insights.
- 5.
SUMMARY
Integrated Safety Analysis, by systematically identifying all potential accidents, has the potential for establishing a systematic documented safety basis for nuclear fuel cycle facilities. This would place the safety of this industry on a firm foundation similar to what has been done for nuclear reactors and major chemical facilities. Based on experience with analyses in progress, ISA appears to be both practical and effective. Some practical challenges remain, but are being addressed by adapting existing methods to this new application.
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ITEM REVIEW CHECKLIST ALL ITEMS Poor Marainal Good 1.
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ADDITIONAL GUIDANCE MJLTIPLE-CHOICE ITEMS Poor Marginal Goo 17.
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'e Reprinted from Nuclear Engineer ng and Design Nuclear Engineering and Design 187 (1999) 229-239 Analysis of hydrogen depletion using a scaled passive autocatalytic recombiner b
Thomas K. Blanchat ^ *, Asimios Malliakos
- Reactor Safety Experiments, Sandia National Laboratories. Albuquerque, NM 87185-1139, USA
- U.S. Nuclear Regulatory Commission Il'ashington DC, 20SSS-000), USA Received 24 August 1998; accepted 3 September 1998
?
Nuclear t
F.
Engineering C
andDesign ELSEVIER Nuclear I:ngineenng and I)esign 1x7 ilv9m 229 2w Analysis of hydrogen depletion using a scaled passive autocatalytic recombiner Thomas K. Blanchat " *, Asimios Malliakos b
- Reactor Safety Dyerunents. Sandia National Laborarancs. Albuquerque. NM 87183-l139. USA
U.S. Nuclear Regulatory Conunmion n'ashmgton DC l0SSS-OtXH. USA Recened 24 August 1998; ucepted 3 September 1998 Abstract flydrogen depletion tests of a scaled passhe autocatalytic tecombiner (PAR) were performed in the Surtse) test vessel Germany) at Sandia National Laboratories (SNL). The experiments were used to determine the hydrogen depletion rate of a PAR in the presence of steam and also to evaluate the effect of scale (number of cartridge >) on the PAR performance at both low and high hydrogen concentrations. O 1999 Elsevier Science S.A. All rights reser ed.
- 1. Introduction natural convective flow currents promote mixing I
of combustible gases in the containment. The Passive autocatalytic recombiner (PARS) are recombination rate of the PAR system needs to be being considered by the nuclear power industry as
_ great enough to keep the concentration of hydro-a combustible gas control system in operating gen below acceptable levels.
plants and advanced light water reactor (ALWR)
There are several catalytic recombiner concepts containments for design basis events. PARS do under development worldwide. SNL is evaluating not require a source of power; instead, they use a a PAR which has been developed by the NIS catalyst to recombine hydrogen and oxygen gases Company, in Hanau, Germany. Detailed tests and j
into water vapor upon contact with the catalyst.
analyses were made in cooperation with the Bat-At low hydrogen concentrations, energy from the telle Institute, Frankfurt, and the Technical Uni-recombination of hydrogen with oxygen is re-versity, Munich. Its development has been leased at a relatively slow (but continuous) rate sponsored by the German utility, RWE Energie.
into the containment. The heat produced creates The NIS!RWE PAR device contains flat rectan-strong buoyancy effects which increases the influx gular cartridges filled with porous spherical ce-of the surrounding gases to the recombiner. These ramic pellets, which are coated with palladium.
The large surface area of the palladium layer of
- corresponding author Tel; + i-505-845-3048; rax: +1 the pellets acts on diffused gas molecules to re.
505-845 3117; e-mail: tkblane@sandia gov.
combine hydrogen with oxygen. Between the car-0029-5493 9) 5 - see front matter C 1999 Elsesier Science S.A All rights resersed.
Pil: S0029 5493(98)00283 0
N 2.\\n
[L K ll! ant hat..i tir:Hiak m
.\\ ut leur f.ngineertne anal l%sen 18' (lWh 2:'l
.H tridges, the PAR desice has open tion channels to the prototype PAR that was deselop. d and fahn-allow heavier particles or aerosols m the atmo-cated by Nis mgenieurgesellschaft Mlill iltanau, sphere to flow through with little plugging of the Germany) (EPRI ALWR Program. IW1 The pellet surface.
prototype PAR contained two rows oi standard Sandia National Laboratories (SNL). under the catalytic cartridges (44 cartridges pei ion) and sponsorship and direction of the USNRC, has had dimensions of 1 m by 1 m. The PAR test conducted an experimental program to evaluate module (also manufactured by NIM iontained the performance of PARS. A PAR was tested at only one row of standard catalytic c.uindges and the Surtsey experimental test facility at SNL. The could be assembled as either a 1/2 sca 144 car-
)
following describes the configuration of the PAR, tridges),1/4 scale (22 cartridges), or 1 scale (11
)
the test facility, the instrumentation, the control cartridges) PAR by removing cartridges and using and data acquisition system, the test conditions,
,maller (length) front and back panels. Note that and the test results and analyses.
the !!2 scale PAR test module configuration has dimensions of = 0.5 m by = 1.0 m.
Fig. I and Fig. 2 show that the PAR test
- 2. Par and test facility description module housing holds the catalyst cartridges in a sertical plane and guides the air flow. A sertical The PAR test module was a scaled version of flow channel of about i em spacing is formed betw een the cartridges. These flow channels (along with the PAR body or housing) define the C
flow area for convection of the heat generated by k
the heat of reaction. The PAR exit has a chimney with a free cross-sectional area equal to the cross-sectional area through the cartridges.
The catalyst material is inserted into rectangu-lar eartridges (0.45 m length, 0.01 m wide, and
)
0.20 m tall). The cartridges are filled with the o
Z catalyst pellets. The steel sides of the cartridges "E
are perforated with many slotted-like openings that allow hydrogen to enter into the cartridge.
The catalyst is a palladium-coated (0.5 w/o) alu-minum oxide pellet with a diameter of = 4-6 mm and a bulk density of = 0.5 g cc-' The porous j
)
oxide pellet provides a large inside surface area
( = 100 m g - ') of palladium that allows a high 1
l' j
y' conversion. A hydrophobic coating is placed on l
J each pellet to minimize startup delavs due to
,, soe 7
water on the catalyst surface, either from steam 4
condensation or from containment sprays.
Fig. 3 shows the location of the PAR test
-3,.
module in the Surtsey vessel. Th,e PAR was lo-cated at the vessel centerline, = 1 m above the s
midline elevation in the Surtsey vessel, llorizontal
^ ' hM and vertical 1-beams exist in the lower half of the Surtsey vessel but there are no 1-beams located directly below the PAR. The Surtsey vessel is an Fig. l. Bottom view of the PAR housing and chimney with ASME-approved steel pressure vessel with a cur-one cartridge.
rent working internal volume of 99 m'. It has a
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I'ig. 2. Cartridges held m a serucal contiguration ly the PAR housing.
i cylindrical shape with removable, dished heads tions, and valve positions for steam. hydrogen, attached to both ends, and is 3.6 m in diameter by and oxygen additions. In addition, the DAQ sys-10.3 m high. The Surtsey vessel has a maximum tem controlled the hydrogen target concentration allowable working pressure of I MPa at 533 K. A and gas addition interval. This allowed changing total of twenty 30.5 cm (12 inch) and 61 cm (24 the test conditions (during the course of a test) inch) instrument penetration ports exist at six based on real-time test results.
different levels around the perimeter of the sessel.
Four pressure transducers were used to measure j
The vessel walls and heads are 5 8 inch thick and the pressure in the Surtsey vessel. The gas temper-covered with at least four inches of fiberglass ature in the Surtsey vessel was measured with insulation, or equivalent material.
twenty thermocouples installed in two rakes. The
-l two thermocouple rakes were installed vertically in the vessel; one rake at the vessel centerline
- 3. Instrumentation, control, and data acquisition (array A) and one rake (array B) located about 0.32 m from the vessel wall. Ten equally-spaced The most significant variables measured in the type-K thermocouples (1.0 m spacing) were 10-PAR experiments were; (1) the pressure and tem-cated on each rake. Six type-K thermocouples j
perature in the Surtsey sessel; (2) the gas con-were installed in the Surtsey vessel steel wallo. In stituents and steam concentrations; (3) the PAR addition, thermocouples measured the injected pellet and channel gap temperatures; (4) the flow oxygen, hydrogen, and steam temperatures, both velocity through the PAR: and (5) the amounts of at the respective manifolds and also at each hydrogen and oxygen injected into the vessel. A steamigas diffuser. In ordet to minimize steam personal computer (PC) based data acquisition condensation, steam was mixed with the oxygen system was designed to control and monitor the and'or hydrogen during each gas injection.
course of the test in real-time. The PC based data A real-time gas mass spectroscopy (GMS) sys-acquisition (DAQ) system gase instantaneous tem was used to determine the concentrations of readouts of the temperatures of the cartridge pel-nitrogen, oxygen, and hydrogen in the vessel at lets and corresponding cartridge air gaps, Surtsey four sample points. The four sample points were vessel pressure, temperatures, and gas concentra-at the PAR inlet, the PAR outlet, high in the
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vessel near the dome, and low in the sessel near A high resolution 12 inch charge-coupled the door. To ensure representative samples and to desice (CCD) color camera was mounted on a minimize the delay time due to purging sample lesel 5 port. and viewed the PAR through a lines, each line was purged for = 1 min prior to tempered glass window, in addiuon to the dignal sampling. This necessitated a continuous purge or camera. an infrared (IR) camera also siewed the gas out of the sessel. The sample lines and puree PAR thmugh a different lesel 5 port. The camera rate 3 were sized to allow no more than a 10 ~
siew could see the PAR exit (top of the chimney )
loss (by solume) of gas out of the sessel oser the and prmide usual esidence in the esent of a course of a 12 h test. Since the PAR inlet was the dedagration event. Other instrumentation in-sample point of greatest interest, this point was duded a hygrometer to measure relatise humidity selected for every other sample (i e., PAR inlet, and pitot-tube differential pressure transducers PAR outlet, PAR inlet, dome, PAR inlet, Surtsey and a hot-wire anemometer to measure the veloc-Door, PAR inlet. PAR outlet....).
ity of the gas at the PAR inlet and outlet.
Ten to twenty (depending on test conditions)
Tw,elve thermocouples monitored the catalyst temperature at three cartridge locations: PAR pre-evacuated 500 cm' gas grab sample bottles were used to collect samples from the sessel. Most middle (and a PAR middle backup), PAR cdge, of the gas grab samples were taken at the PAR and PAR corner. Three sertical positions for tem-perature measurement were monitored at each inlet; however, any of the four gas sample points location (2 cm from the bottom. middle. and top).
could have been selected. These gas grab samples These thermocouples were inserted into the car-were used as an independent verification of the tridges and surrounded by the catalyst pellets gas composition.
Twehe thermocouples monitored the temperature of the gas in the gap between the cartridges and were located opposite of the catalyst thermocou-ples. Four thermocouples monitored the PAR c
inlet temperature. Two thermocouples were 10-cated at the centerline middle and two were 10-
.g.
cated at the centerline edge (within 2 cm of the
.p PAR bottom). Four thermocouples monitored the
,~
h li PAR outlet temperature. Two thermocouples P
Y were located at the centerline middle and two i?
were located at the centerline edge (within 2 cm of 6
'[
the chimney exit).
" gl -
i The hydrogen and oxygen gas was supplied to the vessel from separate manifolds. Standard 441
,p compressed gas cylinders were installed on the l. l [,'q 'y manifolds. In the tests that involve a prototypic j
air steam atmosphere, the cold gas entering the j
t j
4 sessel was mixed with an appropriate amount of
]
steam (capable of heating the cold gas to near the e
a
,{ g-desired test temperature) using a diffuser mixer
~
pipe that was located near the floor of the vessel.
This was necessary to prevent condensation of the steam. Mass How controllers were used to proside precise metering of the hydrogen and oxygen into the sessel. Two mixing fans were installed in the sessel. They were located on opposite sides of the fig i PAR locanon in the Surtse) sessd PAR at the openings of the I-beam lattice: one l
l c
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T. K Blanchat, A..tlaihakos.\\tulcar Lngmeermg ami Desien 187 IItM 2 9 -2.N 1U 420 p ' ' ' " l" A~h" p
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Fig. 4. Centerline gas temperatures with I li scale PAR.
pointed upward and one pointed downward.
steam fraction must be known. A hygrometer The fans were usually operated when hydrogen was used to determine the relative humidity was injected and prior to taking gas grab sam-(Ril). The steam concentration was then calcu-ples.
lated from the ratio of saturation pressure to j
total pressure times the Ril fraction. The satu-ration pressure of steam was determined from
- 4. Gas composition measurements and analyses saturated steam tables using the vessel average gas temperature. The thermocouples on array 11 The GMS system cannot measure steam con-were used to determine the vessel average centrations; a dry sample must be presented. In temperature.
order to achieve this, a condenser and conden-The nitrogen-ratio method was used to deter-sate trap (and heated gas inlet lines) were in-mine wet-basis gas concentrations as a second stalled on each gas measurement line. This independent method (Illanchat et al.,1994). The yielded dry-basis gas concentrations; however, to nitrogen-ratio method does not require an esti-determine wet-basis gas concentrations, the mate of the pretest noncondensible fraction. It i
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3 T. K. Blanchat. A. Malliakos, % clear Engmeermg and Dc.nen 187 (l9991229-2.19 234
- 5. Test matrix does, however, require the pretest noncondensible fraction. For the various posttest times, the num-Six depletion rate tests using a scaled PAR were ber of mol of nitrogen is assumed to be un.
conducted. PAR performance at low hydrogen changed, and the number of mol of another gas is concentrations was determined at l '2, 1 4, and simply the number of mol of nitrogen gas times 1,8 scale. NIS states that the hydrophobic coating the ratio of the other gas specie mole fraction to is probably destroyed when the PAR catalyst the nitrogen mole fraction. The nitrogen-ratio exceeds temperatures of about 473 K. The PAR method calculates the total number of noncon-catalyst would reach these temperatures at about densible moi. Total mol in the vessel is calculated 2"411, cold dry air and about l'S II, in the hot 2m using ideal gas law relationships. Therefore, the air / steam environment. These tests were per-number of steam mol is simply the difference formed at hydrogen concentrations that would between the total vessel mot and the total noncon-not destroy the hydrophobic coating.
densible mol. The steam fraction is found from Three repeat tests (at 1/2,1/4, and 18 scale) the ratio of steam moi to total vessel mol.
were performed at relatively high hydrogen con-500 & -^
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Fig. 6. Catalyst cartride temperatures with I'8 scale PAR.
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Fig 7. Inlet and outlet temperatures with I 8 scale PAR i
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'u-55 steam heat source (227 kg hr) into Surtsey.
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L N ',,; @.~. A with steam. The vessel bulk gas and wall heat up jin i
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H m.j 8
Note that the air pressure increased from 0.083 to i
o-n i
1 2
3 4
5 6
0.107 MPa because of the increase in air tempera-Time (hr) ture from 293 to 375 K.
Steam fractions, as determined from the ratio Fig. 8. Gas concentrations twet-basis) with I'8 wale PAR.
of saturation steam pressure to total pressure in the Surtsey vessel, and also from the nitrogen centrations which yielded the scaled counterpart ratio method, were very similar during the course performance data and completed the scaled deple.
of the majority of the tests. A few deviations were tion rate test series, seen in some tests and the steam fraction deter-mined by the method of pressure ratio is suspect; these deviations were attributed to nonsaturated
- 6. Experimental results conditions in the Surtsey vessel that occurred after hydrogen burns or after operating the PAR at The scaled depletion rate tests started with a high hydrogen concentrations for long periods of mixture of 0.107 MPa of air and 0.107 MPa of time.
steam, for a total pressure of about 0.21 MPa. To Two observations can be made regarding most achieve these conditions, the vessel was sealed of the PAR tests. The PAR started within 10 min with about 0.083 MPa of cold air inside (one in hot, steamy atmospheres when exposed to hy-Albuquerque atmosphere at = 293 K). The Surt.
drogen concentrations in the range of 1-6 mol%.
sey vessel was then heated internally with steam to The second observation was that at steady-state obtain a gas temperature of = 375 K. A portable 200 1.0 -
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gen ncentration (mole N Hydrogen Concentration (moki %)
Fig.10. flydrogen depletion rates at low concentrations.
Fig.12. Normahzed hydrogen depletion rates at low hydrogen concentrations.
operation the PAR appeared to generate a con-vective flow loop in the Surtsey vessel from the that in the upper half of the Surtsey vessel. Also, PAR outlet to the dome, down the Surtsey wall the convective loop appeared to be driven further (until reaching the height of the PAR inlet), and downward into the lower half of the Surtsey then returning to the PAR inlet; as indicated by sessel in those tests with the higher hydrogen both the hydrogen concentration and the vessel concentrations.
gas temperature measurements. Since the convec-A test with the PAR configured at 1/8 scale was tion flow pattern did not extend to the lower half used to measure the hydrogen depletion rate at of Surtsey vessel, the vessel was not completely low hydrogen concentration. The Surtsey vessel well-mixed by the PAR during steady-state opera-was sealed and pressurized with steam to about tion. The hydrogen concentration from the sam-0.21 MPa. The initial gas temperature was = 374 ple point located near the floor always showed a K. The PAR started recombining after the first higher concentration when measurements were hydrogen addition to about 1.0 mol%. There was taken after the last addition, as compared to the
= 10 min delay (from the time of first hydrogen other sample points. This indicated that the deple-injection) in PAR startup. The startup is shown tion below the PAR near the floor was lower than by the increase in the vessel gas temperature (Fig.
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Fig.11. flydrogen depletion rates at high hydiogen concentra.
Fig.13. Normalized hydrogen depletion rates at high hydro-tions.
pen concentrations.
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T K Blimchat. A. Atalliakos.vuclear Engincermg and Design 187 (1999) L'9. D9 237 4 and Fig. 5), the increase in the catalyst temper-equal value over the course of a test. This was ature (Fig. 6), and the increase in the gas tem-because the mixing fans were not turned on perature at the PAR outlet (Fig. 7). Fig. 5 also while depletion rate data were taken and the shows the times when the mixing fans were oper-PAR dow was not sufficient to maintain a mixed ating while Fig. 7 shows the hydrogen additions condition in the vessel. The methodology used to using the mass flow controller. Fig. 8 gives the determine the depletion rate assumed that the wet-basis gas concentrations. The steam concen-vessel was well-mixed; this introduced some error tration ranged from = 50 mol% at the beginning since the average hydrogen concentration was of the test to = 40 mol% at the end. The oxygen not actually measured and cannot be calculated concentration remained relatively constant at since the local steam concentrations were not about 10 mol%. Fig. 9 focuses on the hydrogen known. The measured depletion rates may concentrations at the vessel Door, PAR inlet, slightly overpredict hydrogen consumption at the PAR outlet, and vessel dome locations. This stated hydrogen level since the hydrogen concen-figure also shows the integrated hydrogen addi-tration at the PAR inlet sample point, just be-tion. The hydrogen concentration from the sam-fore the fans were turned on, was lower than the ple point located near the floor showed smaller average value. The depletion rate was then deter-decreases as time progressed after the last addi-mined by calculating the difference in hydrogen tion, compared to the other sample points. This mol at each successive time interval, using the indicated that a reduced depletion occurred in data from the steady-state depletion interval, af-the lower half of the Surtsey vessel, below the ter the hydrogen additions were stopped. The PAR elevation.
calculated depletion rate was then plotted against the measured hydrogen concentration.
PAR performance and the effects of scale were
- 7. Passive autocatalytic recombiner performance determined with tests at both low and high hy-analyses drogen concentrations. Note that the initial con-ditions for all tests started with a vessel pressure Hydrogen depletion rates are used to measure of about 0.2 MPa, with = 50/50 mixtures of air the performance of a PAR. The hydrogen deple-and steam.
tion rate is usually determined as a function of Fig.10 shows the PAR performance with low the hydrogen concentration in the vessel. Deple-hydrogen concentrations ( < 0.7 mol%) at 1/2, tion rate analyses can also be used to show the 1/4, and 1/8 scale. A regression fit of the number effect of various factors, such as PAR location.
of hydrogen mot in the vessel during the steady-oxygen concentration, catalyst poison, etc. on state depletion was used to calculate the fitted PAR performance.The following procedure was depletion rates (along with the 95% confidence used to determine the depletion rate. First, the intervals). Note that the 1/2 scale depletion rate time-dependent amount of hydrogen in the Surt-is 2 4 times the 1/8 scale depletion rate, Fig.11 sey vessel (in mol) was determined by multiply-shows the PAR performance with high hydrogen ing the average hydrogen concentration by the concentrations (1-6 mol%) and at 1/2,1/4, and total number of mol in the Surtsey vessel. The 1j8 scale. Simple scaling does not appear to ap-average hydrogen concentration was assumed to ply to depletion rates <at high hydrogen be that measured by the gas mass spectrometer concentrations.
at the PAR inlet sample point. The total number A better comparison of the scaled depletion of mol in the vessel was calculated using the rate data can be made by normalizing the data, aserage gas temperature (determined from the Depletion rate models predict that depletion rate array B thermocouples) and the ideal gas law.
is directly proportional to scale and depletion As shown earlier in the results section, the rate is independent of volume (Fischer, 1995; hydrogen concentrations measured at the four Sher et al.,1995). Therefore, a simple scale fac-sample locations diverged from some initially tor can be used to normalize the data. These I
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.s
238 T. K. Blanchat. A Malhakosi Mclear Enginecimg and Design 187 (1999) 229-239 models assume that the vessel is well-mixed.
dia National Laboratories. The experiments de-llowever, if the PAR only consumes hydrogen in termined the hydrogen depletion rate of a PAR a small portion of the total vessel volume, the in the presence of steam and also evaluated the depletion rate calculation can overpredict con-effect of scale (number of cartridges) on the sumption if the vessel is not well-mixed at all PAR performance at both low and high hydro-times. The depletion rate measurements then be-gen concentrations, come scale-dependent since tests with larger scale The following conclusions can be made. The and/or higher concentrations appear to deplete PAR started within 10 min in hot, steamy atmo-larger pockets of hydrogen within the total vessel spheres when exposed to hydrogen concentra-volume.
tions in the range of 1-6 mol%. The PAR Fig.12 and 13 show the scaled depletion rate appeared to generate a convective flow loop in data normalized to full-scale by applying the the Surtsey vessel from the PAR outlet to the scale factor ( x 2 for 1/2 scale, x 4 for 1/4 scale, dome, down the Surtsey wall until reaching a and x 8 for 1/8 scale). Fig.12 shows that the height near the PAR inlet, and then returned to depletion rates for these tests of low hydrogen the PAR inlet. liydrogen concentration was concentrations are indeed directly proportional stratified in the lower part of the Surtsey vessel.
to scale. However, Fig.13 shows that tests with This was proven by the hydrogen concentrations high hydrogen concentrations yield lower deple-from the sample point located near the floor tion rates for larger scale, probably because sSowing smaller decreases in time, as compared larger volumes are being depleted.
to the other sample points. The loop appeared Fig.12 and Fig.13 also give comparisons with to drive further downward below the PAR with published depletion rate data at pressures of 0.2 higher hydrogen concentrations and also with MPa and 0.1 MPa. Data at 0.1 MPa is only larger scale PARS.
presented to highlight the physics; depletion of Assuming a well-mixed condition in the vessel, hydrogen by the PAR is a mass diffusion pro-the hydrogen depletion rate is most likely pro-cess driven by density gradients. The data corre-portional to scale. The Battelle and the Fischer lates reasonably well with both the Fischer correlations agree reasonably well within the model and the Battelle correlation at 0.2 MPa range of the Surtsey PAR test depletion rate pressure when hydrogen concentrations were be-data. Parameters affecting scale proportionality low 4-5 mol%. However, the data shows deple-include the well-mixed assumption in the tion rates below that predicted by the 0.2 MPa methodology used to determine the depletion linear fit of the Battelle data for data extrapo-rate. If the PAR only consumes hydrogen in a lated to 10 mol%.I The steady-state pressure small portion of the total vessel volume, the de-conditions with the 1/4 and 1/2 scale PAR were pletion rate calculation can overpredict con-
= 0.3 MPa. This means that the test data should sumption if the vessel is not well-mixed at all really be compared to higher pressure theoretical times. The depletion rate measurements then be-depletion rate curves. Also, different PAR de-come scale-dependent since tests with larger scale signs probably have different performance and/or higher concentrations appear to deplete curves. Note that the Fischer model and the Bat-larger pockets of hydrogen within the total vessel telle data are applicable to the NIS prototype volume.
PAR design which did not use the 0.5 m tall additional chimney used in the SNL PAR tests.
Acknowledgements
- 8. Summary Sandia is a multiprogram laboratory operated by Sandia Corporation, a Lockheed Martin Hydrogen depletion rates using a scaled PAR Company, for the United States Department of were measured in the Surtsey test sessel at San-Energy under Contract DE-AC04-94AL85000.
r 1
t T. K. Blam-hat. 4, Malliakos, Nuclear I:ngimcrmg and IMign IS7 (1999) 229-2.19 139 RefereKM Niitigation, Nuclear Technology, Vol.112. October.1995.
EPRI ALWR Program, Qualitication of Passise Av*ocatalytic Recombiners for Combustion Gas Control m ALWR Con-liianchat, T. K., Allen. M D. Ni Pilch, R.T. Nichols, b. peri-taintnents. April 8,1993.
ments to lnvestigate Direct Containment ileating Phenom-Sher, R., J. Li, D. E. I.eaver, Niodels for Esahutmg the ena with Scaled Models of the Surry Nuclear Power Plant, Performance of Passise Autocatalytte Recembmers NUREG CR 6152 SAND 93 2519, Sandia National Labo-(PARsi.1995 National lleat Transfer Conference, ANS ratories, Albuquerque, NM, June,1994 Proceedings li'lC, Vol. H, Portland, OR, August 5-9 l'ischer, K., Quahtication of a Passne Catalytie for il>drogen i993.
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