ML20214L237
| ML20214L237 | |
| Person / Time | |
|---|---|
| Site: | Three Mile Island  |
| Issue date: | 08/29/1986 |
| From: | Warren R GENERAL PUBLIC UTILITIES CORP. |
| To: | |
| Shared Package | |
| ML20214L235 | List: |
| References | |
| 3527-006, 3527-006-R04, 3527-6, 3527-6-R4, NUDOCS 8609090574 | |
| Download: ML20214L237 (212) | |
Text
{{#Wiki_filter:' ENuclear TER 3s27-oos aEv 4 ISSUE DATE August 29, 1986 E ITs O wen O wits DIVISION TECHNICAL EVALUATION REPORT FOR Submerged Demineralizer System COG ENG dO M DATE B/'8 /% RTR PA > DATE K /2c/% I I DATE I cog ENG MGR. E E i 1 DOCUMENT PAGE 1 OF l
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No ENuclear reCanICAt entVA110n ace 0R1 35h-006 Title Page 2 of Submerged Demineralizer System (SDS) Rev.
SUMMARY
OF CHANGE Approval Date 0 Initial issue per GPUNC Letter 4400-82-L-0066 4/82 1 Reissue per GPUtlC Letter 4410-83-L-0122 6/83 2 Reissue per GPUNC Letter 4410-84-L-0109 7/84 Incorporates changes required by ECM's S-1151 (Revisions 0 through 3), S-1163 (Revisions 0 through 3) 1110 Revision 0, 1140 Revision 0, 1159 Revision 0, and 1141 Revision 0 3 Annual Update 8/85 Incorporates changes made by S-ECM 1110 Revisions 0 and 1, ECA's 072, 042, 047, 041, and 102. 4 Annual Update Incorporates changes made by S-ECM 1058 Revision 2, 8/86 ECA's 041, 072, 087, and 312 = b 7 5 Si 9 2 J
TER 3527-006 TECHNICAL EVALUATION REPORT SUBMERGED DEMINERALIZATION SYSTEM J l l 1 c k
$ + TER 3527-006 CONTENTS Chapter 1 Summary of Treatment Plan 1.1 Project Scope 1.2 Identification of RadlonucIldes and Radioactivity Levels 1.3 Alternatives Considered 1.4 Description of the Decontamination Process 1.4.1 General 1.4.2 SDS Operating Description Chapter 2 Summary of Health and Environmental Effects 2.1 Occupational Exposure During Routine Operation 2.1.1 Exposure Planning 2.2 Exposures to the Pubile Ouring Routine Operation of the SDS and EPICOR-!!
2.3 Evaluation of unexpected Occurrences 2.4 Industrial Health and Safety 2.4.1 Public Safety 2.4.2 Occupational Safety 2.5 Non-Radiological Environmental Effects 2.6 Ultimate Waste Olsposition i
TER 3527-006 - Chapter 3 Process Description 3.1 Introduction 3.2 Ion-Exchange Concepts 3.3 Ion-Exchange Materials 3.4 Resin Selection Criteria 3.5 Predicted Performance of Ion-Exchangers 3.6 Monitoring of Ion-Exchangers Chapter 4 Design Basis 4.1 Introduction 4.2 Components of the SDS Waste Processing System 4.3 Submerged Demineralization System Criteria 4.3.1 Design Basis 4.3.2 Process 4.3.3 Performance 4.3.4 Capacity 4.3.5 Performance and Design Requirements 4.3.6 Piping System 4.3.7 Vessels and Tanks 4.3.8 Shielding Design 4.3.9 Leakage 4.3.10 Building and Auxiliary Services Interfaces 4.3.11 Controls and Instrumentation 4.4 System Operational Concepts 11
TER 3527-006 Chapter 5 System Description and Arrangement 5.1 Demineralizer System 5.1.1 Influent Water Filtration 5.1.2 Ion Exchanger Units 5.1.3 Leakage Detection and Processing 5.1.4 EPICOR-II 5.1.5 Monitoring Tank System 5.1.6 Off-Gas and Liquid Separation System 5.2 Sampling and Process Radiation Monitoring System 5.2.1 Sampilng System 5.2.2 Process Radiation Monitoring System 5.3 Ion-Exchanger and Filter Vessel Transfer in the Spent Fuel Pool 5.4 Arrangement of the Water Treatment System in the Fuel Storage Pool 5.5 Liner Recombiner and Vacuum Outgassing System Chapter 6 Radiation Protection 6.1 Ensuring Occupational Radiation Exposures are ALARA 6.1.1 Policy Considerations 6.1.2 Design Considerations 6.1.3 Operational Considerations 6.2 Radiation Protection Design Features 6.2.1 Facility Design Features 6.2.2 Shielding 6.2.3 Ventilation 6.2.4 Area Radiation Monitoring Instrumentation ill
TER 3527-006 6.3 Dose Assessment 6.3.1 On-site Occupational Exposures 6.3.2 Off-site Radiological Exposures Chapter 7 Accident Analyses 7.1 Inadvertent Pumping of Containment Water into the Spent Fuel Pool 7.2 Pipe Rupture on Filter Inlet Line (above water level) 7.3 Inadvertent Lifting of Prefilter Above Pool Surface 7.4 Inadvertent Lifting of Ion Exchanger Above Pool Surface 7.5 Inadvertent Drop of SDS Shipping Cask Chapter 8 Conduct of Operations 8.1 System Development 8.2 System Preoperational Testing 8.3 System Operations 8.4 System Decommissioning References tv
c TER 3527-006 Appendix No. 1 - RC Processing Plan with the RCS in a Partially Dralned Condition Appendix No. 2 - Internals Indexing Fluture Processing System (Deleted) l Appendix No. 3 - Fuel Transfer Canal Draining System Appendix No. 4 - Fuel Transfer Canal Shallow End Orainage System Appendix No. 5 - Early Defueling DHC Reactor Vessel Filtration System j V
TER 3527-006 Chapter 1 Summary of Treatment Plan 1.1 Project Scope To date the SDS system has processed almost 4 million gallons of l contaminated water, including: 650,000 gallons of Reactor Building sump water, 366,000 gallons from RB decon.and 870,000 gallons of RCS water. l The continued decontamination of THI-2 includes the repeated processing of the IIF/RCS using the Letdown / Makeup Method or the Reactor Vessel l Filtration System (DHCS). The activity level of this water is given in Table 1.1. In addition, Reactor Building Decon water or water from other sources may be processed through SOS as necessary. This report describes the Submerged Demineralizer System (505) and the work associated with the developrr,ent of the system for the expeditious clean-up and dispriitton of the contaminated water mentioned above. Specific design f eatures of the system include:
- 1. Placement of the operating system in the spent fuel pool to take advantage of shleiding provided by the water in the pool.
- 2. Radioactive gas collection and treatment prior to release.
- 3. Liquid leak-off collection and treatment.
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- 4. Underwater placement of lon-exchange vessels into a shipping cask without removal from the spent fuel pool.
- 5. Use of existing EPICOR-II equipment for polishing of SDS effluent, as required.
1.2 Identification of Radlonuclides and Radioactivity Levels Water samples were taken from the reactor coolant system and the containment sump, and were analyzed to identify specific radionuclides and concentrations. Typical results are listed in Table 1.1. The Recctor Coolant System (RCS) and containment sump specific radionuclides and concentrations are based upon actual sample data taken. The RCS activity decreases due to radioactive decay and leakage from the RCS. However, RCS activity may increase during processing shutdown due to leaching. 1.3 Alternatives Considered During the early phases of developing a system for the control, clean-up, and disposition of t'he contaminated water located in the containment building of THI-2, several methods or alternatives were evaluated. .These alternatives were grouped into two categories: 4 (1) those with no volume reduction, and (2) those with volume reduction. 0564X/LC
TER 3527-006 Presented below, are the alternatives considered with a discussion and conclusion about each. Alternative I: Leave Contaminated Hater in Containment Indefinitely (No Volume Reduction) j Discussion A. Containment Sump Hater
- 1. The sump water contains radionuclide concentrations as depicted in Table 1.1. The existence of this may cause some increase in radiological exposure problems during the recovery program, i.e., increased exposure to recovery program personnel, increased contamination levels, and increased possibility of airborne radioactivity.
- 2. The presence of the contaminated sump water would prevent decontamination of the lower levels of the containment building.
B. Reactor Coolant System Hata* The presence of the contaminated water in the reactor coolant system would inhibit disassembly of the reactor and impede defueling operations. 0564X/LC
TER 3527-006
Conclusion:
Alternative I is not deemed feasible for the following reasons:
- 1. The potential for increased personnel exposure exists. Therefort,
> compliance with the principles of ALARA is not possible.
- 2. Facility decontamination and defueling operations are seriously inhibited or perhaps prevented.
- 3. Continued storage of the contaminated water in the containment sump for increased periods of time increases the probability that leakage from the building may occur. Leakage of contaminated water from the reactor building sump may threaten the public health and safety.
- 4. Continued storage of the water in the containment building for an extended period of time is undesirable. The primary isotopes of concern (Cs-137 and Sr-90) exhibit decay half-lives of approximately 30 year. Storage in the containment sump for approximately 300 years would be required for 10 half-life decay.
Maintenance of containment integrity for this interval of time cannot be assured. Alternative II: Transfer Water to On-site Storage Facility (No Volume Reduction) 0564X/LC
r TER 3527-006 Discussion:
- 1. To safely contain the contaminated water, the construction of an on-site liquid radwaste storage facility would be required.
- 2. Additional radiation areas on the plant site would be created if a 11guld radwaste storage facility were built.
- 3. Estimates indicate the construction of a liquid radwaste storage facility would require two to three years, at a minimum.
- 4. A 11 auld radioactive waste transfer system for the transfer of the contaminated water from the various locations to the waste storage complex would be required.
- 5. Handling and pumping operations may involve leakage and the spread
! of contamination.
- 6. Disposal of the water prior to natural decay is required because of the long radioactive decay half-lives. This alternative is not representative of an acceptable long-term solution.
l l l
Conclusion:
Based on the above discussion, Alternative II is not a feasible method. Alternative III: Solidification and Disposal (No Volume Reduction) i 0564X/LC
n -- TER 3527-006 Olscussion:
- 1. The construction of an on-site solidification facility would be required.
- 2. Based on 1,000,000 gallons of contaminated water originally to be processed, a 30-gallon availability of water vclume in a 55-gallon drum, 70% availability, 24-hour / day operation, and a 45 minute cycle time, the prccessing time may exceed four years.
- 3. Based on 1,000,000 gallons of contaminated water originally to be processed and a 30-gallon availability of water volume in a 55-gallon drum. The number of drums of solidified waste that would be generated would exceed 33,000. Handling, transportation and disposal of this extremely large quantity of solidified waste would be prohibitively expensive and violate basic principles of minimizing radioactive waste volumes.
- 4. The handling evolution required to solidify the contaminated water may involve substantial radiation exposure to personnel.
- 5. The potential for leakage and contamination problems may c'e substantial in operating a solidification facility for processing this contaminated water in this manner.
Conclusion:
Based on the above considerations, Alternative III is not
. considered to be feasible.
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TER 3527-006 Alternative IV: Submerged Demineralizer System (SDS) in the "B" Spent Fuel Pool and EPICOR-II System (Volume Reduction) Discussion:
- 1. The system would be capable of concentrating fission products on a medium to effectively remove those products from the water.
- 2. Processing contaminated water cJ1d result in concentrated waste requiring additional shielding.
- 3. The systert. (ncorporates remote operability features.
- 4. Design, construction and operation would allow for relatively short lead times.
- 5. The system would require minimal maintenance.
- 6. The SDS is amenable to location within the Spent Fuel Pool which would utilize the shielding capability of the pool water.
- 7. Containers of highly loaded lon exchange media arising from operation of the SDS would not be acceptable at shallow land disposal sites. The SDS design and selection of lon exchange media l
allows volumes of such highly loaded media to be minimized to permit interim storage and probable ultimate disposal in a geological repository. It is believed that the EPICOR-II liners, generated as a result of polishing the SDS effluent, will be suitable for shallow land disposal because of their low curie ! content. l 0564X/LC l
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- 8. The EPICOR-II system, used in conjunction with SDS, will provide the capability to_ remove trace quantities of radionuclides from the SDS effluent.
Conclusion:
Based on the above considerations Alternative IV is an acceptable method for decontamination. Alternative V: Evaporation (Volume Reduction) Discussion:
- 1. Evaporation would require the design and construction of a new facility.
- 2. Due to the nature of the contaminated water to be processed the design of the facility would be complex to allow for maintenance of the processing system and personnel radiological protection. The construction of the facility may require at least four years.
- 3. Evaporation provides the ability to process a wide range of chemical contaminants.
j
Conclusion:
Evaporation is an acceptable alternative for processing the contaminated waste waters. Based on the long construction time of the facility and inherent potential for higher occupational exposure due to increased maintenance requirements, this alternative is less desirable than Alternative IV, Submerged Demineralizer System (505) coupled with the EPICOR II system. 0564X/LC
TER 3527-006 1.4 Description of the Decontamination Process 1.4.1 General _ Analysis of the alternatives previously presented has resulted in the determination that, of the two alternative categories considered, volume reduction is appropriate for the disposition of contaminated water. This conclusion was reached based on the considerations that volume reduction:
- 1. fixes the contaminants
- 2. concentrates the activity
- 3. minimizes storage and disposal space Of the volume reduction. category, the Submerged Demineralizer system (SDS) in conjunction with EPICOR II for final polishing, or Alternative IV, was chosen as the most appropriate process for the following reasons:
- 1. Basic design simplicity.
- 2. High performance for decontaminating liquids, i.e.,
decontamination factors up to 107 , or higher.
- 3. Amenable to placement under water to take advantage of shielding properties of the water 0564X/LC
-n--,. -- , - - - , ,-e- m
1 TER 3527-006
- 4. Ability to implement water processing in a timely fashion for support of the overall objective of fuel removal.
- 5. Ability to use existing proven plant structures, equipment and technology for containment of the processed water and final process polishing (EPICOR-II)
The SDS with EPICOR II is an lon-exchange process expected to 7 provide decontamination factors of up to 10 for cesium and 105 for strontium (see Table 3.1), thus removing the majority of the activity from the water prior to placement in the Processed Water Storage Tanks, or usage for continued decontamination or makeup to the RCS. 1.4.2 SDS Operatina Description Figure 1.1 shows a block diagram of the process flow of the Submerged Demineralizer System (SDS) with the EPICOR II System. Radioactive water enters the SDS via the RCS manifold. This source of water can pass through two cartridge or sand type filters for removal of particulate matter. Sample connections are provided on the influent and effluent of the filters, and influent to the ion-exchange system to determine radionuclide content and concentrations of the water to be processed. 0564X/LC 1
TER 3527-006 The first part of the SDS lon-exchange system consists of up to six underwater vessels (24 1/2 in. x 54 1/2 in.). Each vessc! contains approximately 8 cubic feet of homogeneously mixed IE-96 and LINDE-A zeolite ton exchange media. Zeolite media volumes and mixtures may be changed to reflect different processing scenarios (The resin mix is specified by Radiochemical Engineering on the form included in OP 4215-OPS-3527.16). Inlet, outlet, and vent connections are made with remotely operated couplings. The vessels are arranged in two parallel trains with three columns in each train. Flow may be directed through one train of three vessels or through both trains in parallel. Loading of the vessels will be controlled by feed batch size, residence time, influent and effluent sample analysis, and continuous monitoring. The second part of the SDS ion exchange system consists of two parallel sand filter vessels located underwater and immediately downstream of the zeolite beds. These sand filters will contain a mixture of sand and are intended to remove system effluent particulates, primarily zeolite fints. The columns are intended to be operated singly. Present SDS operations are envisioned to provide for radionuclide loading of the zeolite media to a maximum of 134 137 Cs at the time of shipping. 60,000 C1 of Cs and .. 0564X/LC p -- v -- - - - - - - - - - . - , _ - - - -- w+
TER 3527-006 This loading level is based on restrictions imposed based on the shielding provided by the Chem-Nuclear 1-13C II shipping cask. From the point of view of minimizing waste volume generation it is desirable to load the zeolites to these higher levels. When the desired bed loading is achieved on the first bed of the train, the feed flow to the train will be stopped, the bed will be flushed with clean water, and the first bed will be disconnected and moved to the storage rack in the spent fuel pool using the pool area crane. The second and third beds will be disconnected, moved to the first and second positions, respectively. A new lon exchanger vessel is then installed in the third position. Following installation of the new lon-exchanger, the treatment of the contaminated water will recommence. This operational concept, which is the currently intended mode of operation, has eliminated the potential for valving errors and also minimizes the possibility of an unexpected radionuclide " breakthrough" which could recontaminate the water already processed. This mode of operation may change if the processing scenario changes. Additionally some processing operations will require fewer ( than three (3) ion exchange units per train to achieve desired decontamination factors, in these cases jumpers will be installed to bypass the unused positions.
~
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TER 3527-006 When the SDS is processing contaminated sump water, the effluent from the " cation" sand filters can be sent to EPICOR-II for polishing. When processing reactor coolant the effluent may be routed to installed tankage for injection back into the Reactor Coolant System as a source of makeup or to EPICOR for polishing. The spent lon-exchangers and filters of SDS will be retained under water in the spent fuel pool until removed. To transport spent lon-exchangers, they will be bulk dewatered, vacuum dewatered, and catalyst recombiner added, and loaded into shielded casks while under water and removed from the spent fuel pool. Following decontamination of the cask surface, the cask can then be loaded onto a trailer for transportation, e 0564X/LC
TER 3527-006 TABLE 1.1 Typical Results of Analysis from the Reactor Coolant System Mater and the Containment Sump Hater ; Radionuclide Concentrations (pC1/ml) Reactor Coolant RB Sump Isotope System Decon Sampling Date (5/86) (7/83) H3 0.085 0.12 Sr-90 2.4 1.6
- i. Sb-125 0.093 0.023 Cs-134 0.01 0.14 Cs-137 0.35 2.1 pH 7.58 7 Boron 5460 ppm 3193 ppm Na 1500 ppm 240 ppm P
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TER 3527-006 Chapter 2 Summary of Health and Environmental Effects 2.1 Occupational Radiation Exposure During Routine Operation The SDS has been designed to maintain radiation exposures to operating personnel as low as reasonably achievable. To implement the ALARA concept, the following features have been incorporated into the SDS design. o Shielding has been designed to limit whole body dose rates in operating areas to less than 1 mrem /hr. The filters and ion-exchangers are located approximately 16 feet underwater for shleiding. Components and piping carrying high activity water not contained underwater in the fuel pool have been provided with shielding to maintain external dose rates to acceptable levels. o Controls and instrumentation are located in low radiation areas. o Components containing high activity water have been designed for venting exhaust gases to the SDS Off Gas System. The Off-Gas System will minimize the potential for excessive airborne radioactivity releases in the work areas and to the environment. Additional design and operational ALARA features are given in Section 6. 0564X/LC
TER 3527-006 The occupational exposure for the EPICOR-II system was assessed in NUREG-0591. The occupational radiation exposure for the EPICOR-II system will be lower for the processing of the effluent from the SDS than previously processed by EPICOR-II since the influent activity to the EPICOR-II from-the SDS has been substantially reduced by processing the radioactively contaminated water through the SDS. 2.1.1 Exposure Planning Several activities will be implemented prior to and shortly after, the SDS start up to assure occupational exposures are minimized. These activities include: o Review of operating, maintenance and surveillance procedures to assure precautions and prerequisites are adequate. o Review of the installed system to identify potential problems during operation and the implementation of corrective actions. o Operational evaluations during preoperational testing and system training will be performed to update exposure estimates. o Determination of radiation dose rates during normal operations and maintenance evolutions will be performed. 0564X/LC k i
TER 3527-006 As these reviews are completed, operating and surveillance frequencies can be established; total occupational exposures can be updated for the various activities during SDS operation. This exercise will permit review of those activities estimated to yield the highest man-rem expenditure. Pre-examination to assure that every reasonable effort is expended to minimize personnel exposure may include the following considerations: o Reduction of the frequency of operation o Temporary or additional shielding o Tool modifications o Procedure modification o Personnel training to reduce work time o Component modifications 2.2 Exposures to the Public During Routine Operation of the SDS and EPICOR-II Refer to Chapter 6 for information on exposures to the public from routine operation of the SDS and EPICOR-II processing. 2.3 Evaluation of Unexpected Occurrences l The radiological assessment of unexpected occurrences includes the analysis of five hypothetical accidents that are postulated to occur during operation of the system. 0564X/LC
TER 3527-006 The first accident is an inadvertent pumping of RCS water into the fuel storage pool untti a total of 225 gallons of radioactive water is released to the pool. No exposures occur to the public since the contaminated water is contained in the pool. The maximum exposure rate at a distance of six feet above the pool surface is estimated to be 4.2 mR/ hour. Since the release of water occurs ur.derwater, no significant internal exposures are expected for workers. The primary impact of the accident is the contamination of water in the Spent Fuel Pool (233,000 gallons). (Refer to Section 7.1) The second hypothetical accident assumes a pipe is ruptured and RCS water is sprayed into the building and fuel storage pool. It is possible that workers could be contaminated, however, prompt implementation of emergency procedures would minimize radiation exposures. The radioactive materials would be contained within the building except small amounts of radionuclides that would become etrborae and subsequently be released through the monitored station discharge. This airborne radionuclide release woulf not result in significant exposures to the public. (Refer to Section 7.2) The third hypothetical accident evaluated considers the inadvertent raising of a loaded prefilter above the pool surface. The dose rate at a distance of 15 feet from the source is estimated to be 21 Rem / hour and could result in a dose of approximately 1.8 rem to workers who remain in the area for a five minute period. (Refer to Section 7.3) s. 0564X/LC 1 i
TER 3527-006 The fourth hypothetical accident evaluated considers the inadvertent raising of a loaded zeolite ton exchanger above the pool surface. The dose rate at a distance of 20 feet from the source is estimated to be approximately 340 Rem /hr. (Refer to Section 7.4) The final hypothetical accident considers the inadvertent drop of the SDS shipping cask containing a loaded zeolite ion exchanger. The SDS i shipping cask is assumed to be dropped from the maximum height of the Fuel Handling Building crane to the EL 205' floor. The dose rate resulting from a complete rupture of the SDS shipping cask at a distance of 20 feet is approximately 340 Rem /hr and assumes rupture of both the cask and the vessel. The small amounts of radionuclides assumed to become airborne would not result in significant exposures to the public. Also there would not be a significant effect from direct radiation exposure to the public. (Refer to Section 7.5) l The evaluation of unexpected occurrences for the EPICOR-II system was analyzed in NUREG-0591. The potential releases from processing 505 effluent water will be significantly lower because of the lower concentration of water being processed through EPICOR-II from the SDS. (See Table 3.1) t l 0564X/LC l
TER 3527-006 2.4 Industrial Health and Safety 2.4.1 Public Safety Operation of the Submerged Demineralizer System poses no risk from an industrial safety standpoint to the general public for the following reasons:
- 1. Lifting and handling activities described take place within the THI complex.
- 2. Hazardous chemical species, flammable or explosive substances, heavy industrial processes, and concentrated manufacturing activities are not involved in the installation or operation of the SDS.
- 3. No toxic substances are used in the 505.
2.4.2 Occupational Safety During the operation of the SDS, operating personnel will adhere to station requirements for occupational safety. l l Structural equipment and operating equipment used shall meet Occupational Safety and Health Administration requirements as applicable. Personnel protective equipment that would be required for the operation of the SDS will be utilized in accordance with standard station procedures. 0564X/LC
TER 3527-006 2.5 Non-Radioloaical Environmental Effects Adverse environmental effects from the construction and operation of the SDS are not anticipated. The system will be installed and operated in an existing, on-site facility and thus will not require any change in land-use. Additionally, the system is designed in such a manner as to allow zero discharge of liquid effluents to receiving waters. The final disposition of the processed water will be determined at a later date. Solid wastes (spent ion-exchangers, etc.) generated by the SDS will be stored and held until final disposal is accomplished. r 2.6 Ultimate Waste Disposition Radioactive material generated as a result of the accident at TMI is currently restricted to disposal at the commercial disposal site operated by U.S. Ecology at Hanford, Washington. SDS vessels meeting the criteria for disposal at this site will be disposed of by shallow land burial at this location. SDS vessels not meeting the Hanford Site criteria will be classified as abnormal waste and disposed of by the Department of Energy in accordance with the Memorandum of Understanding dated July 15, 1981, between the Nuclear Regulatory Commission and the Department of Energy dealing with the disposition of solid nuclear waste from the cleanup of TMt Unit 2. 0564X/LC
TER 3527-006 Chapter 3 i Process Description 3.1 Introduction A combined filtration-lon exchange process has been selected as the method for treating radioactive water contained in the reactor coolant system ar.d containment building. The filter ion-exchange method has been used successfully to reduce quantities of radionuclides in the process effluent to levels that are in compliance with 10 CFR 20 and 10 CFR 50. Furthermore, experiments conducted at ORNL, documented in ORNL report TM-7448, provide evidence that SDS processing, followed by EPICOR-II polishing, should provide an effective method for water decontamination. The initial processing of the waste water is flitration for the removal of solids to optimize the subsequent ton-exchange process. Filtration is believed to be necessary to protect the zeolite beds from particulates in the sump and RCS water. After filtration, radioactive ion removal from the waste water involves the use of lon-exchange materials. The two or three ion-exchange ,, columns (per train) contain homogeneously mixed inorganic zeolite material which effectively removes essentially all of the cesium and 0564X/LC
TER 3527-006 much of the strontium. Other trace levels of radionuclides are also partially removed by the zeolite media. The radioactivity content in the effluent stream of each bed is used to determine when the bed is cxpended and replaced. Final demineralization of the contaminated sump water and selected batches of RCS water is intended to be by the EPICOR-II system. Essentially, all remaining radionuclides excluding tritium are expected to be removed from the water during this process step. 3.2 Ion-Exchange Concepts Ion-exchangers are solid inorganic and organic materials containing exch;ngeable cations or anions. When solutions containing lonic species are in contact with the resin, a stoichiometrically equivalent amount of ions are exchanged. As an example, an ion-exchanger in the sodium (Na+) form will " soften" water by an ion-exchange process. Hard water containing CaCl 2 is " softened" by this exchange mechanism which removes the Ca" lons from solution and replaces them with Na+ tons. In a similar manner, Sr++ and Cs* tons are exchanged with the Na* tons from the solid zeolite material. Characteristic properties of ion exchangers involve micro-structural features contained in a framework held together by chemical bonds and/or lattice energy. Either a positive or negative electric surplus charge ! is carried within this framework which must be compensated for by ions l l of opposite sign. Because the exchange of ions is a diffusion process l 1 0564X/LC l l
TER 3527-006 within the structural framework, it does not conform to normal chemical reaction kinetics. The preference of lon-exchangers for a particular specie is due to electrostatic interactions between the charged framework and the exchanging lons which vary in size and charge number. The decontamination factor (DF) is the ratio of the concentration in the influent stream to that in the effluent stream and is used for determining the efficiency of a purification process for radionuclide removal. The following equation is a qualitative expression for the removal of a single ionic specie from solution. DF = 1 1 - Kn0Ew CV f where: Q = Total exchange capacity (meq/ml wet resin) n - Fraction of Q used E, = Equivalent weight of the nuclide under consideration C = Nuclide concentration (weight / volume) f V = Feed throughput (number of ion-exchange bed volumes) K = Unit conversion coastant Important variables which are considered as part of the evaluation of ion-exchangers for decontamination are ion exchange media type, selectivity and capacity, concentration of t!ie species to be removed, total composition of the feed stream, and the presence of contaminants. Operating parameters such as resin bed size, flow rate, flow distribution, pH, and temperatures are specified for the ion-exchange beds in order to maximize removal of the contaminating lons. 0564X/LC
TER 3527-006 Specifications which have been defined for this purification process include: (1) The flow rate to provide an acceptable residence time for ion diffusion and exchange to occur. (2) The cross-sectional area of the ion-exchange media to provide an acceptable linear velocity through the bed. (3) The bed depth to result in an acceptable pressure drop. (4) A uniform flow distribution and a uniform media distribution to reduce the potential for channeling. (5) The lon-exchange media bead size to minimize atrition and large pressure drops. (6) The curie loading to satisfy personnel exposure, radiation damage, transportation, and storage regulations. (7) The cation form and the amount of ion-exchange media impurities to maximize removal of specific nuclides. 3.3 Ion-Exchange Materials The ion-excharger media selected for use in this processing system are an inorganic zeolite material that is commercially available and known as Ion Siv IE-96 (Na* form of IE-95), and LINDE-A, to be used for SOS and caticn and anion resins to be used in EPICOR II. 1 0564X/LC I
=
r
TER 3527-006 Zeolites are aluminos111 cates with framework structures enclosing large and uniform cavities. Because of their narrow, rigid, and uniform pore size, they can also act as " molecular sieves" to sorb small molecules, . but to exclude molecules that are larger than the opening in the crystal framework. Other media are also being evaluated. Should our plans change wtth regard to ion exchange media to be employed, the NRC will be notified. Organic ton exchange resins are typically gels and are classified as cross-linked polyelectrolytes. Their framework, or matrix, consists of an irregular, macromolecular, three-dimensional network of hydrocarbon chains. In cation exchangers, the matrix carries ionic groups such as 50"3, COO , (P02 3, and in anion exchangers groups such as
< NH+, Na+, H+ are carried. The framework of the organic resins, 4
in contrast to that of the zeolites, is a flexible random network which is elastic, can be expanded, and is made insoluble by introduction of cross-links which interconnect the various hydrocarbon chains. The extent of crosslinking establishes the mesh width of the matrix and, thus, the degree of swelling and the ton mobilities within the resin. This, in turn, determines the ion exchange rates and electric conductivity of the resin. Since the mechanism of the ion exchange process involves the stoichiometric exchange of ions between the exchanger and the solution while electrical neutrality is maintained, the rate determining step is controlled by the interdiffusion of ions within the framework of the 0564X/LC
TER 3527-006 ion-exchanger. Since the rate of ion exchange is determined by diffusion processes, rate laws are derived by applying well-known diffusion equations to ion-exchange systems. However, complications arise from diffusion-induced electric forces, from selectively specific interactions, and changes in swelling such that rate laws are applicable for only a few limited cases. Experimental efforts have been conducted at the Savannah River laboratory to investigate the kinetics of cesium . and strontium ion-exchange with the zeolite exchanger. Cesium was absorbed so rapidly that only rough estimates of the diffusion parameter could be obtained. The resulting equation, used to calculate column performance, did not involve kinetic parameters but was suitable to described the equilibrium column behavior. 3.4 Resin Selection Criteria Technical information obtained from previous use of various lon-exchange materials and the results of recent experimental work with simulated and actual water samples from Three Mlle Island were used to support the selection of specific ion exchange materials for this processing system. The performance of an ton exchange system is controlled by the l physical and chemical properties of the exchange material as well as by the operating conditions specified in Section 3.2. The important l
- criteria which were used in the ton exchanger selection process included:
(1) Exchange capacity ! (2) Swelling equilibrium f (3) Degree of crosslinking (4) Resin particle size 0564X/LC l
TER 3527-006 (5) Ionic selectivity (6) Ion-exchange kinetics (7) Chemical, radiolytic and physical stability (8) Previous demonstrated performance (EFICOR-II) Experimental studies with reactor coolant water have been conducted to support and verify the selection of these lon-exchangers; refer to ORNL TM-7448. Further, onsite studies have been performed to support and verify selection of the lon-exchange media. The decontamination factors for the major contaminants were measured using a number of candidate ion exchangers including the organic resins, HCR-5 and SBR-OH, and the zeolite ION SIV IE-96 and LINDE-A. The results indicated the most favorable type of lon exchange media to be used in the cleanup process were the available cation-anion resins in combination with the zeolite exchanger. Furthermore, as a result of processing in excess of 2,000,000 gallons of radioactively contaminated water from the Auxiliary Building, Reactor Building and RCS, we are confident that the 505, with EPICOR-II used as a polishing system for treatment of SDS effluent, will continue to provide an effective means to decontaminate the contaminated waters. EPICOR-II resin loadings may be altered to improve polishing effectiveness, if required. 0564X/LC s
4 TER 3527-006 3.5. Predicted Performance of Ion-Exchangers The concentrations of radionuclides in samples of water from the Reactor Coolant System have been measured. Those radionuclides still detectable in June, 1984 include Sr-90, Cs-134, Cs-137, and Sb-125. The expected performance of the SDS lon-exchangers, and the EPICOR-II lon exchangers is shown in Table 3.2. The concentrations of strontium and cesium are expected to be significantly reduced by processing through the SDS and EPICOR-II system. Table 3,1 is included to provide historical data on Reactor Building Sump water processing. Antimony is expected to pass through the SDS ion exchangers and will end up as the predominant gamma emitter in the solution entering the EPICOR-II system. The Concentration of Sb-125 in the containment building sump sample is approximately 0.011 microcuries per milliliter. 3.6 Monitoring of Ion Exchangers Methods which may be used to monitor the effectiveness of the ion j exchangers include liquid sampling and in-line radiation detectors. Liquid samples of feed and effluent streams can also be used to i establish the approximate curie loadings in the loaded beds. 0564X/LC i i
, - r - . . _ _ , , . . . - _
TABLE 3.1 Actual activity concentrationsa in SDS process streams after 200 bed volumes through each zeolite bed (Based on continuous flow through four zeolite columns) Historical - RB Sump Processing Effluent concentrations, d UCi/ml. Zeolite columns Effluent Nuclide Feed Filter First Second Third fourth EPICOR-II 0.88 0.88 0.88 0.88 0.88 0.88 0.88 3w 60Co b b 2E-5 2E-5 2E-5 2E-5 2.3E-6 5.02 5.02 2.5 1.0E-1 8.5E-3 SE-3 <1.0E-5 90S r 4.0E-4 4.0E-4 4.0E-4 IE-6 106Ru b b 4.0E-4 b b 1.1E-2 1.1E-2 1.1E-2 1.1E-2 3.4E-7 125Sb 1.1E-4 1.1E-4 2E-8 1.39E+1 1.39E+1 1.7E+0 1.1E-4 134Cs 1.0E-3 1.0E-3 2E-7 1.23E+2 1.23E+2 1.5E+1 1.0E-3 137Cs 4.0E-4 4.0E-4 4.0E-4 IE-6 144Ce b b 4.0E-4 a In pC1/ml as of February 1982 based on actual samples b Not quantifiable by gamma spectroscopy due to overall sample activities. 0564X LC -;
- =
9 8, o
' j.
TER 3527-006 TABLE 3.2 Actual activity concentrationsa in SDS process streams
; , after 200 bed volumes through each zeolite bed
, (Based on continuous flow through two zeolite columns)
RCS Processing j Effluent concentrations. a UC1/ml. Zeolite columns Nuclide Feed Filter First Second Sand Filter 60Co <2.0E-3 2.2E-3 1.2E-3 <1.6E-4 (2E-4 90S r 3.4 3.1 0.084 2.8E-3 3.0E-3 106Ru 2.3E-2 <2E-2 <5.2E-3 <1.5E-3 <1.7E-3 125Sb 0.16 0.15 0.15 0.14 0.15 134Cs 0.025 0.023 1.2E-3 <1.1E-4 <l.2E-4 137Cs 0.56 0.51 3.0E-2 <1.7E-4 <1.6E-4 144Ce (1.2E-2 <l.2E-2 <4.5E-3 <1.8E-3 <2.0E-3 a In pC1/ml as of June 1984 based on actual samples b Not quantifiable by gamma spectroscopy due to overall sample activities. l 0564X/LC l l
T TER 3527-006 Chapter 4 Submerged Demineralizer System Design Basis 4.1 Introduction The Submerged Demineralization System (SDS) is an underwater ion-exchange system which has been specifically designed to process higher-level waste waters *, with inherent system features for reduction of occupational and environmental exposures. The SDS is submerged in the spent fuel pool (1) to provide shielding during operation, (2) to permit access to the system during demineralizer changeout. (3) to minimize the hazard from potential accidents, and (4) to utilize an existing Seismic Category I facility. In conjunction with the SDS, the EPICOR-II system may be used to provide final polishing of the SDS effluent water for removal of trace quantities of radionuclides. i. Design features for SDS include:
- 1. A prefilter and final filter in series, followed by two parallel trains of 2 or 3 zeolite ton-exchangers in series. These ion-exchangers are followed by two " cation" sand filters in l parallel followed by the EPICOR-II equipment. This combination of filters and lon-exchangers achieves the desired process flow rates and decontamination factors (DF's).
- Higher-level waste waters are those contaminated waters having gross activity concentrations in excess of 100 pCi/ml.
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- 2. Series operation logic that allows for sequencing the demineralization units to prevent activity breakthrough in the final zeolite bed and maximize activity loading on spent beds to accomplish the best possible activity concentration.
The design objectives are as follows:
- a. A totally integrated system that is as independent as possible from existing waste systems at the Three Mlle Island plant. The SDS is a temporary system for the recovery of TMI-2.
2
- b. A system that has the capability to reduce the fission product concentration in the contaminated water and has optional capabilities for removing chemical contaminants to permit future disposition of the concentrated waste form.
- c. A system that could be operated with a minimum of exposure to personnel and a negligible risk to the public.
- d. A system that could accomplish the objective listed above in a timely and cost effective manner,
- e. A system that incorporates known and demonstrated processing equipment, materials and techniques. (EPICOR-II) 0564X/LC O
, , , , - w--,~,--- --r,--- - - - ,
n
TER 3527-006 4.2 Components of the SDS Waste Processing System The SDS is comprised of the following components, all of which will be l located in the Unit 2 8 fuel pool, or in the near vicinity of the B fuel pool. (See Figure 5.6, General Layout Plan.)
- 1. Feed filtering system;
- 2. Two parallel ion exchange trains, each comprised of two or three 10-cubic-foot vessels loaded with 8 cubic-feet (nominal) of homogeneously mixed IE-96 and LINDE-A zeolite exchange media;
- 3. Two parallel " cation" sand filters containing graded sand filter media;
- 4. A monitoring and sampling system for control of demineralizer unit loading;
- 5. A secondary containment system for the filters and zeolite beds and radiation shielding for piping, valves, sampling, and monitoring systems;
- 6. Two monitoring tanks for collecting treated water.
- 7. An off-gas system for treating and filtering gases and vent air from the system; 0564X/LC i
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- 8. A Liner Recombiner and Vacuum Outgassing System (LRVOS) designed to eliminate the potential of a combustible hydrogen and oxygen mixture existing'In the SDS liners.
- 9. Associated piping, valving, and structural supports required for placement of system components;
- 10. Auxiliary systems including underwater ion-exchange column storage, a dewatering system, and analytical equipment;
- 11. Vent system to allow for venting of stored vessels.
The EPICOR-II system is downstream of the SDS process flow stream for removal of trace fission products that are not removed in the ion exchange media of the SDS. 4.3 Submerged Demineralizer System Design Criteria 4.3.1 Desian Basis Regulatory guidance followed during the design of the Submerged Demineralization System was extracted from the following documents: o U.S. Nuclear Regulatory Guide 1.140 dated March, 1978 o U.S. Nuclear Regulatory Guide 1.143 dated July, 1978 0564X/LC
TER 3527-006 o U.S. Nuclear Regulatory Guide 8.8, dated June, 1978 o U.S. Nuclear Regulatory Guide 8.10, dated May, 1977 o U.S. Nuclear Regulatory Guide 1.21 Revision 1, June 1974 o Code of Federal Regulations, 10 CFR 20, Standard for Protection Against Radiation o Code of Federal Regulations, 10 CFR 50, Licensing of Production and Utilization Facilities. 4.3.2 Process The design shall provide for operations and maintenance in such a manner as to maintain exposures to plant personnel to levels which are "as low as is reasonably achievable", in accordance with Regulatory Guide 8.8. 4.3.3 Performance The isotopic inventory for the water to be processed is summarized in Table 1.1. The 505 followed by the EPICOR-II systems is designed and operated such as to reduce the average isotopic specific activity of the treated waste streams. The' expected performance of these systems is given in Table 3.2. j l 0564X/LC l-
TER 3527-006 4.3.4 Capacity Flow Rate - 5 to 30 GPM (up to 15 GPM per train). The system will have the ability to operate continuously, (subject to ggg periodic maintenance shutdown). 4.3.5 Performance and Design Reautrements The following system requirements nave been incorporated into the design of the SDS. o Leak P.otection and Containment o Shielding (Beta, Gamma) o Ventilation o Functional Design and Maintainability o Criticality Concerns o Decontamination - Decommissioning 4.3.6 Piping System (piping, valves and pumps)
- 1. The mechanical and structural design criteria and fabrication of piping systems and piping components are specified in ANSI B31.1, 1977 Edition with Addendum through Hinter 1978 or ANSI B31.1, 1980 for components added after 1980, and Table 1 of Regulatory Guide 1.143,
- 2. Piping system design shall be based on a maximum of 150 psi at 100*F.
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- 3. Piping runs are generally designed to permit water flushing.
- 4. Instrument connections to piping systems are located to provide clearance for attachment, operation and maintenance.
4.3.7 Vessels and Tanks
- 1. The mechanical and structural design criteria and fabrication of vessels and tanks will be in accordance with the requirements of the ASME Boller and Pressure Vessel Code, Section VIII, Division 1, 1977, Addendum through Winter 78.
- 2. The vessels shall be of two types:
- a. Primary lon-exchangers shall contain approximately eight (8) cubic feet of zeolite ton exchange media for the purpose of removing teslum and strontium fror.: the waste water. Should our processing scenario be changed it may be necessary to alter the volume of the zeolite media. Should changes occur, the NRC will be informed.
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- b. Influent and " cation" sand filter units are planned to contain cartridge type filter assemblies or sand capable of removing particles greater than approximately 10 microns. SDS effluent filter capability has been provided to incorporate the capability to filter out lon-exchange media fines from the process stream should fines carryover occur.
- 3. The SDS lon-exchangers and filters shall be capable of functioning submerged under approximately 16 feet of water within the spent fuel pool.
- 4. The ion-exchangers shall be designed for 15 GPM nominal process rate, filters shall be designed for 50 GPM nominal; volume velocity through the loaded lon-exchangers shall be limited to prevent channeling or breakthrough.
- 5. Pressure loss through the ion-exchangers should not exceed 15 psi when operating at 5 GPM with clean resins.
- 6. The ion-exchangers shall be equipped with a lifting arrangement compatible with the spent fuel pool crane to permit movement of the vessels in the pool.
- 7. The 10-cubic-foot vessels will be equipped with all required nozzles, including inlet, outlet, vent connections, and fill and sluicing connections.
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- 8. Each lon-exchanger shall be equipped with all internals required for media distribution, dewatering, and venting.
- 9. Desian Condition
- a. The 10-cubic-foot vessels will be compatible with the piping design conditions of 150 psig at 100'F. The vessel design conditions for continuous operation will be, at least, equivalent to the piping design conditions.
- b. The following additional design conditions have been imposed:
o Overall Height 54 1/2 inches o Overall Diameter 24 1/2 inches o Materials Stainless Steel - o Weight will have negative buoyancy (loaded with lon-exchange media)
- 10. Testing The vessels shall be hydrostatically tested at 1.5 times the design pressure per ASME Section VIII.
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TER 3527-006 4.3.8 Shieldina Desian The shielding shall be desigr.ed to reduce levels resulting from the SDS to less than imR/hr, general area. The shielding for the EPICOR-II equipment is adequate for the processing of the SDS effluent because the SDS effluent water activity will be lower than the activity level of the water for which EPICOR-II shielding was originally designed. 4.3.9 Leakage To minimize the operational impact of activity that can potentially leak from bad process connections to fuel Pool 8, SDS vessels are contained in secondary containment enclosures. Pool water is continuously drawn through these enclosures and passed through separate ion exchangers (Leakage containment). This design preven. t.1e pool water from eventually attaining high level concentrations of radionuclides. Monitoring of potential leakage is accomplished through the established SDS Sampling System. 4.3.10 Buildina and Auxiliary Service Interfaces The SDS has been designed to meet the following building interface requirements. 0564X/LC
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- 1. All components of the SDS located in the Fuel Handling Building do not exceed the normal load capacities of the cranes in this area. The Fuel Handling Building auxiliary and main cranes have capacities of 15 tons and 110 tons, respectively.
- 2. The SDS will operate in the ambient conditions of the Fuel Handling Building as supplied by the building heating, ventilating and air conditioning system, and lighting system.
- 3. Auxiliary services supplied to the 505 are from the Demineralizer Water, Electrical Distribution, Instrument Air and Service Air Systems.
- 4. During installation of the system, no equipment was permanently attached to the fuel pool liner and no penetrations were made in the fuel pool liner.
- 5. Structural support for the system will be designed to take the dynamic and static loads associated with the normal operation of the system.
=
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TER 3527-006 4.3.11. Controls and Instrumentation 4.3.11.1 General System Description l
- 1. The control and instrumentation systems shall be designed to control and monitor the various normal process functions throughout the system and will permit a safe, orderly shutdown of the system.
2 .. The controls and instrumentation systems will enable the operators to perform the designated functions efficiently and safely.
- 3. Where portions of the process must be operated remotely, sufficient instrumentation shall be included to assure safe operation and permit analysis of a process upset or remote detection of equipment malfunction.
- 4. Control and instrumentation systems shall be categorized as: (1) controls and instrumentation systems essential for the maintenance of process fluid confinement, and (2) process controls instrumentation systems essential for the determination of process operating parameters.
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- 5. Radiation monitoring and surveillance instrumentation essential for the protection of operating personnel, the public and the environment is provided.
4.3.11.2 Performance and Deslan Requirements
- 1. Remote controls and instrumentation shall have provisions for remote connection of electrical leads.
- 2. Alarms and/or indicators are provided for adequate surveillance of process operation.
- 3. Process-connected instrumentation shall be constructed of material compatible with that used for the construction of the process equipment.
- 4. Electrical wiring shall be designed in such a manner as to minimize noise and spurious signals.
- 5. Instrumentation identification and numbering should follow the standards and practices of the Instrument Society of America (ISA).
- 6. Radiation monitors shall be provided for the detection of gamma radiation. In-line radiation monitors were installed to monitor beta radiation, however to date have not been used or maintained, nor are they planned to be.
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4 1 I TER 3527-006
- 7. Specific instruments shall be designated to function in a fall-safe mode and will alert to a failure condition.
4.4 System Operational Concepts The following is a summary operation description. This operating sequence depicts the processing scenario as currently planned and could be changed based on operating experience. The SDS process logic as currently planned, is based on the following < steps: 4
- 1. Ion-exchanger units will be preloaded with new lon exchange media prior to placement in the system. The ion exchanger units will utilize a homogeneous mixture of zeolite media.
- 2. Water will be introduced to fill and vent the lon-exchange units.
i
- 3. These preloaded SDS lon-exchange units will be lowered into the Unit 2 spent fuel pool and placed in the containment enclosures.
- 4. Inlet and outlet header connections will be made to the J ion-exchange units.
- 5. The lon-exchange system isolation valves will be opened and treatment of the contaminated waste stream will begin at low flow rates untti system integrity and acceptable out water quality are verified.
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- 6. The flow rate to the lon-exchange units will be increased on a gradual basis until the desired operational flow rate is achieved.
- 7. When the first lon-exchange bed becomes depleted, the unit will be flushed with processed Water to ensure that radioactive waste water in the system piping is purged prior to disconnecting the quick disconnects on the domineralizer unit.
- 8. The lon-exchange unit will be decoupled remotely via the use of quick disconnects and will be stored in the spent fuel pool.
However, loading directly into a cask prior to shipment is possible.
- 9. After the first ion-exchange unit has been removed, the second ion exchange unit will be placed into the position of the first unit, and the third ion exchange Unit will be moved to the second position. A new lon-exchange unit will be installed in the third position. In some instances fewer than three (3) lon-exchange units will be required to achieve the desired decontamination factors. In these cases, jumpers will be installed to bypass the unused positions.
0564X/LC
TER 3527-006 Chapter 5
' System Description and Arrangement 5.1 Demineralizer System 5.1.1 Influent Water Filtration A flow diagram of the waste water influent system is shown in Fig. 5.1. Contaminated water is pumped into the SDS from the ,
containment sump, the RCS, the fuel transfer canal, or 11guldwaste (HDL) tanks. The containment sump will employ the presently installed SHS-P-1 pump (jet pump). i i Two filters have been installed to filter out solids in the untreated contaminated water before the water is processed by the ion-exchangers. These filters will be either cartridge or sand type. The cartridge filter elements are protected by ! 3/16 inch perforated metal plate serving as a roughing screen. The prefilter has 125 micron filter cartridges to remove debris and suspended solids from the contaminated water. The design of the final filter is similar to the prefilter except that the filter cartridge is designed for removal of suspended solids of greater than 10 microns in size from the contaminated water. The two sand filters are loaded in layers. The first layer is 200 pounds of 0.85 mm sand and the second layer is 700 pounds of 0.45 mm sand. Boros111cate 47 - 0564X/LC l i - j
TER 3527-006 glass with a normal Boron content of 22% is added uniformly through the sand to prevent potential criticality. The flow capacity through each filter is 50 gpm. Reverse flow through filters is prevented by a check valve in the supply line to each filter. Each filter is housed in a containment enclosure to enable leakage detection and confinement of potential leakage. The filters are submerged in the spent fuel pool for shielding considerations. Influent waste water may be sampled from a shleided sample box located above the water level to determine the activity of contaminated water prior to and following filtration. Inlet, outlet, ar.d vent connections on the filters are made i with quick disconnect valved couplings which tre remotely operated from the top of the pool. Inlet-outlet pressure gauges are provided to monitor and control solids loading. Load limits for the filters are based on filter differential pressure, filter influer.t and effluent sampling, and/or the j surface dose limit for the filter vessel. A flush line is attached to the filter inlet to provide a source of water for flushing the filters prior to removal. i 0564X/LC p
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TER 3527-006 5.1.2 Ion Exchanger Units A flow diagram of the ton exchange manifold and primary lon-exchange columns is shown in Fig. 5.2. This system consists of six underwater columns (241/2 in. x 541/2 tr..), each containing eight cubic feet of homogeneously mixed Ion Siv IE-96 and LINDE-A zeolite media and two underwater columns containing sand filter media. The six zeolite beds are divided into two trains each containing three beds (A, B, C ) with piping and valves provided to operate either train individually or both trains in parallel. The effluent from the first parallel train of three zeolite beds flows through either of the " cation" sand filters. Jumpers are provided to permit fewer than four (4) vessel per train operation. An in-line radiation monitor measures the activity level of the water exiting the cation exchanger. The valve manifold for controlling the operation of the primary Ion exchange columns is located above the pool, inside a shleided enclosure that contains a built-in sump to collect leakage that might occur. Any such leakage is routed back to the RCS manifold. A line connects to the inlet of each primary exchanger to provide water for flushing the exchangers when they are loaded. Radlonuclide loading of lon exchange vessels is determined by analyzing the influent and effluent from each exchanger. Process water flow is mcasured by instruments placed in the line to each lon-exchange train. 0564X/LC
TER 3527-006 Hnen processing containment sump water, effluent from the SDS-is directea to the EPICOR-II polishing unit, if desired. When the SDS is to be utilized to process reactor coolant, the effluent can be valved into the RCS clean-up manifold then back into the Reactor Coolant System via installed tankage, bypassing EPICOR-II. 5.1.3 Leakage Detection and Processing Each submerged vessel is located inside a secondary containment box that contains spent fuel pool water. During , operation the secondary containment lid is closed. This lid is slotted to permit a calculated quantity of pool water to flow past the vessels and connectors. Pool water from the containment boxes is continuously monitored to detect leakage and is circulated by a pump through one of the two leakage containment ton-exchangers (See Figure 5.2). Any leakage which occurs during routine connection and disconnection of the quick-disconnects will be captured by the containment boxes, diluted by pool water, and treated by lon-exchange before being returned to the pool. 5.1.4 EPICOR-!! 1 EPICOR-II (Figure 5.3) can provide final treatment of water after the water is processed through the 505. When processing containment sump water, the processing plan is to polish with EPICOR-II. When processing RCS water, EPICOR !! may be used 0564X/LC I
TER 3527-006 as necessary to remove Antimony 125 before being returned to RCS (prior chemical adjustment will be required). EPICOR-II consists of filters, lon-exchangers and receiver tanks. The purpose of EPICOR-II is to remove trace fission products they may be present in the water. The EPICOR-II safety assessment is provided in NUREG-0591. 5.1.5 Monitorino Tank System Effluent from the 505 ton-exchanger can flow into one of two monitorirg tanks (Figure 5.4) or in the case of RCS processing, directly to one of three RCBT's. The purpose of the monitoring tank system is to collect treated water. Each monitor tcnk is equipped with a sparger and tank level indicators that will automatically shut the inlet to the tank should a high level condition exist. Water in the monitoring tanks can be transferred back for reprocessing by 505 or used as flush water in the 505, or directed to existing tankage. 5.1.6 Off-Gas and Liauld Separation System t an off-gas and liquid separation system collects gaseous and liquid wastes resulting from the operation of the water treatment system. The off-gas system is illustrated in Figure ' 5.5. Gaseous effluent lines from the ion exchange vessels, sampling glove boxes and shielded valving manifolds are connected to the off-gas system. Gaseous effluent is passed through a mlst eliminator in the off-gas separator tank before being treated by an electric eff-gas heater to reduce the l-0564X/LC i
m-TER 3527-006 off-gas relative humidity to 70L A roughing filter and two HEPA filters are provided for further treatment. Air is moved through the system by a centrifugal blower rated at 1000 cfm. The discharge of this blower will be monitored and routed to the existing Fuel Handling Building HVAC system. Motsture collected by the off-gas system and waste returned from the continuous radiation monitoring system is directed into a separator tank. At the top of the tank a mlst eliminator separates moisture from effluent gas prior to the gas entering the off-gas treatment system. The tank is located in the surge pit and is covered with a concrete and lead shield. The level in the tank will be indicated and controlled manually to return collected water to the RCS manifold for reprocessing. Offgassing of the RCBT's during processing of the RCS to the RCBT's is handled by established station procedures involving the Waste Gas Decay Tanks. Discharge from these tanks is filtered through HEPA filters before being released through the station vent. 5.2 Samplina and Process Radiation Monitoring System The sampling glove boxes are shielded enclosures which allow water samples to be taken for analysts of radionuclides and other contaminants. The piping entering the glove boxes contains cylinders that permit draining a predetermined amount of sample into a collection bottle. Cylinders are purged by positioning valves to permit the water to flow through them and return to a waste drain header and into the 0564X/LC
TER 3527-006 off-gas separator tank. A water line connects to the inlet of the sample cylinders to allow the line to be flushed after a sample has been taken. 5.2.1 Sampling System Sampling of the SOS process to monitor performance is accomplished from three shielded sampling glove boxes. One glove box is for sampling the filtration system, the second is for sampling the feed and effluent for the first zeolite bed if there is significant breakthrough of the first zeolite bed and the third for sampling the effluents of the remaining zeolites beds. The entire sampling sequence is performed in shielded glove boxes to minimize the possibility of inadvertent leakage and spread of contamination during routine operation. 5.2.2 Process Radiation Monitoring System i The 50S is equipped with a process radiation monitoring system which provides indication of the radioactivity concentration in the process flow stream at the effluent point from each ion exchanger vessel. The purpose of this monitoring system is to provide indication and alarm of radionuclide breakthrough of the ton exchange media. i t 0564X/LC l
TER 3527-006 5.3 Ion-Exchancer and Filter Vessel Transfer in the Fuel Storage Pool Prior to system operation, ton exchanger and filter vessels are placed inside the containment boxes and connected with quick-disconnect couplings. When it is determined that a vessel is loaded with radioactive contaminants to predetermined limits as specified in the Process Control Program, the system will be flushed with low-activity processed water. This procedure flushes away waterborne radioactivity, thus minimizing the potential for loss of contaminants into the pool water while decoupling vessels. Vessel decoupling is accomplished remotely. Vessels are transferred using the existing fuel handling crane utilizing a yoke attached to a long shaft. The purpose of this yoke-arm assembly is to prevent inadvertent lifting of the ton exchange bed or filter vessel to a height greater than eight feet below the surface of the water in the pool. This device is a safety tool that will mechanically prevent lifting a loaded vessel out of the water shielding and preclude the possibility of accidental exposure of operating personnel. The ion-exchange vessels are arranged to provide series processing through each of the beds; the influent waste water is treated by the bed in position "A", then by the bed in position "B", then by the bed in position "C" and finally either of the " cation" sand filters "A" or "B". The first vessel in each train (position A) will load with radioactive contaminants first. The loaded vessel will then be stored until transfer to a shielded cask. At no time during the operation of the system will a loaded vessel be taken out of the pool before it has been placed in a shielded cask. The loaded cask will be transferred from the pool with the overhead crane. 0564X/LC i l
TER 3527-006 5.4 Arrangement of the Water Treatment System in the Fuel Storage Pool Figure 5.6 illustrates the arrangement of the SDS in the fuel storage pool (viewed from above). The filters, and zeolite ion exchanger vessels, are located underwater in containment enclosures in the "B" spent fuel pool. These enclosures and the exchangers are supported along one side of tne pool on a structural steel rack that is attached to the pool curb. The racks act as a support for the system and also provides an operating platform from which the remote connections can be made. The off-gas system is mounted on the curb near the surge tank area. A dewatering station is located in the "B" SFP cask pit below the water level and is used for displacing the water from expendad columns and filters and dewatering them prior to placement in the cask. An underwater storage rack, designed to handle 60 expended vessels is located in the pool. This storage capacity allows processing to continue without interruption due to handling operations or vessel disposal or shipping. Stored IX vessels will be vented via a common header connecting to the liquid separation module to continually vent gas byproducts that may be generated in the vessels during storage. 5.5 Liner Recombiner and Vacuum Outaassino System (LRVOS) The Liner Recombiners and Vacuum Outgassing System (LRVOS) is designed to eliminate the potential of a combustible Hydrogen and Oxygen mixture existing in the 505 Liners. This will facilitate the ultimate shipment and burial of the SDS Liners. 0564X/LC
TER 3527-006 The LRVOS will perform the following operations while maintaining the normal operating depth of water between the operators and the SDS liner.
- 1. Reduce water in the SDS liner using vacuum outgassing to ensure enhanced operation of the recombiner catalyst.
- 2. Allow sampling of the liner gas at atmospheric pressures.
- 3. Provide capability to inert the SDS Liner with Argon or N2 to approximately 10 psig prior to tool removal. This will prevent any water intrusion during tool decoupling.
- 4. Provide a means to remotely insert the recombiner catalyst into the SDS liner vent port. The catalyst is retained inside the liner by the internal vent port screen.
- 5. Provide sufficient recombiner catalyst to recombine the hydrogen and oxygen produced by radiolosis of the water remaining in the liner.
- 6. Provide vacuum to defueling canisters at the DS to allow canister gas sampling.
4 03988/LC i
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1 TER 3527-006 Chapter 6 Radiation Protection 6.1 Ensuring Occupational Radiation Exposures are ALARA 6.1.1 Policy Considerations The objectives with respect to SDS operations are to ensure that operations conducted in support of the on-going demineralization program are conducted in a radiologically safe manner, and further, that operations associated with radiation exposure will be approached from the standpoint of maintaining radiation exposure to levels that are as low as reasonably achievable. During the operational period of the system, the effective control of radiation exposure will be based on the following I considerations:
- 1. Sound engineering design of the facilities and equipment.
- 2. The use of proper radiation protection practices, including work task planning for the proper use of the appropriate equipment by qualified personnel.
0564X/LC
TER 3527-006
- 3. Strict adherence to the radiological controls procedures as developed for TMI-2.
6.1.2 Desian Considerations The SDS was specifically designed to maintain exposure to operating personnel to as low as reasonably achievable. To implement this concept the components carrying high level activity water will be provided with additional shielding or are submerged in the spent fuel pool. Shielding has been . designed to limit whole body body exposure rates in operating areas to approximately 1 mR/hr. In addition, components carrying high level process fluids have been designed for exhaust to the SDS off-gas system. This method of off-gas treatment will minimize the potential for airborne releases in the work areas. The specific design features utilized in meeting this requirement are discussed in detail in Section 6.2.1. 6.1.3 Operational Considerations The system design reflects the following operational ALARA . considerations: 0564X/LC r--m-rr.- yy- e .- w ---,,..--,w - e , - - _
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TER 3527-006
- 1. Exposure of personnel servicing a specific component on the SDS will be reduced by providing shielding between the individual components that constitute substantial radiation sources to the receptor.
- 2. The exposure of personnel who operate valves on the SDS will be reduced through the use of reach rods through lead and steel shield boxes.
- 3. Controls for the SDS will be located in low radiation zones.
- 4. Airborne radioactive material concentrations will be minimized by routing the off-gas effluent from the SDS to the THI ventilation system for further treatment.
- 5. The sampling stations for the feedstream and filters that contain high levels of radioactive materials will be I exhausted through the SDS ventilation system.
- 6. All sampling is performed in shielded glove boxes to minimize the possibility of inadvertent leakage and spread of contamination during routine operation.
l l l \ 0564X/LC
TER 3527-006 , 6.2 Radiation Protection Design Features 6.2.1 Facility Desian Features The system is designed to take maximum advantage of station features already in place and operational in terms of protection of the public. In addition, design features provided by the system are intended for the reduction of releases of radioactive material to the environment. The following features provide for protection of individuals from radiological hazards during normal operations from external exposure and unanticipated operational occurrences, such as spills.
- 1. The SDS primary demineralization units are housed under approximately 16 feet of shielding water in the THI-2 spent fuel pool.
- 2. The entire process and all equipment is housed in the Auxiliary and Fuel Handling Buildings which are Seismic Category I structures with air handling and ventilation systems designed to mitigate the consequences of radiological accidents.
- 3. The system is designed in such a manner as to allow zero discharge of liquid effluents. The effluent processed water will be stored on the TMI site until final disposition has been determined.
0564X/LC O
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TER 3527-006
- 4. The o'ff-gas system effluent will be filtered and monitored before input to existing ventilation exhaust systems.
1
- 5. Filters, primary lon-exchange beds, " cation" sand filters, and their associated couplings are operated in containment devices. Each containment device is connected to a pump manifold and a continuous flow of approximately 10 GPM is maintained through each containment. The combined flow from the containment enclosures is then processed through a separate ion exchange column and then discharged back to the spent fuel pool.
- 6. Loaded vessels will be placed in a shielded cask underwater.
- 7. To the extent possible all-welded stainless steel construction is specified to minimize the potential for leakage.
l l
- 8. Lead or equivalent shielding is provided for pipes, valves, and vessels (except those located under water) where necessary for personnel protection.
- 9. Design of a sequenced multi-bed process - three (3) beds in series to preclude breakthrough and contamination of the outlet stream.
0564X/LC
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T'ER 3527-006 10.' The entire process stream is designed with appropriate pressure indicators.
- 11. Inlet, outlet and vent connection are made with remote-operated-valved quick release couplings.
6.2.2 Shielding 4 The minimum shielding thickness required for radiological protection has been designed to reduce levels in occupied areas to less than 1 mR/hr. Operating panels and instrumentation racks are located away from potential' sources of radiation or adequate shielding is provided to meet radiological exposure destgr; limits. All movements of the vessels out of the fuel pool will be performed utilizing a shielded transfer cask. 6.2.3 Ventilation The ventilation and off-gas system provided to service the SDS is designed to minimize airborne radiological releases to the - environment. Among these design features are: l
- 1. Manual level controlled off-gas separator tank with mist
, eliminator to receive vent connections from the ion exchange and filter' vessels, sample glove boxes, piping manifolds, and the dewatering station. 0564X/LC I
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TER 3527-006
- 2. Roughing filter with differential pressure indication.
- 3. Two HEPA filters with differential pressure indication. !
l l
- 4. A centrifugal off-gas blower with flow indication.
- 5. Sample ports for monitoring the system and DOP test ports for HEPA testing.
- 6. The effluent of the SDS off-gas system is routed to the existing THI-2 ventilation system exhaust, which is filtered again through the Fuel Handling Building exhaust HEPA filters prior to discharge from the plant.
6.2.4 Area Radiation Monitoring Instrumentation General area radiation monitors have been provided which will be utilized to alert personnel of increasing radiation levels during normal operations or maintenance activities. 6.3 Dose Assessment 6.3.1 On-site Occupational Exposures 0564X/LC
TER 3527-006 Normal Operation During the operation of the Submerged Demineralization System, there are operations that involve occupational exposures, but precautions have been taken in the design stage to minimize personnel exposures. Major operational activities involving such exposures are as follows: A. Sampling operations B. System start-up valve alignment C. Spent vessel changeout D. Cask removal, decontamination and survey operations E. System maintenance F. Vessel dewatering Decommissioning The SDS detailed decommissioning plan is being developed in conjunction with the operating procedures for the system. However, the modular design of the system is conductive to disassembly while minimizing exposure to personnel. 0564X/LC
TER 3527-006 6.3.2 Off-site Radioloalcal Exposures Source Terms for Llauld Effluents Liquid effluent from the system will be returned to station tankage for further disposition, therefore, no 11guld source term is required for this report. Radiological source terms for potential environmental releases are dependent on the processing schedule proposed for SDS and/or EPICOR-2. Review of this schedule shows that from the present (4/84) until the end of defueling, SDS, cnd possibly also EPICOR-2, will be dedicated to processing of RCS. Up to this time EPICOR-2 has not been used for RCS processing, but recent elevations in the Sb-125 concentration in the RCS may necessitate the use of EPICOR-2 to remove this contaminant. The assumption made here for potential source term generation purposes is that both SDS and EPICOR-2 will be dedicated to processing RCS. Miscellaneous small batches of liquid waste may be processed by EPICOR-2, but would be infrequent since liners dedicated for RCS more than likely could not be used for other waste streams. l Experience with previous operations within the RCS show that minor disturbances within the reactor vessel give rise to increased concentrations of a select number of isotopes which become candidates for potential releases to systems involved 0564X/LC j
. - _ _ = _ _
TER 3527-006 in RCS decontamination and therefore, potentially to the environment. A history of concentrations of the major radiologically significant isotopes with time is shown in Figure 6-1. Not reflected in this figure are the increases in Ce-144 and alpha concentrations that accompany disturbances within the RCS. Sample analysis results, tabulated below, show typical concentrations resulting from RCS disturbances. i 0564X/LC
TER 3527-006 Radiochemistry Analysis Results for RCS Sample of 4/9/84 (Sample #84-04966) Concentration Isotope (uC1/ml) Uncertainty Ag-110m <1.5E-2 Ce-144 1.1E+0 4.0E-2 Co-60 1.7E-1 1.0E-2 Cs-134 2.3E-1 1.0E-2 Cs-137 4.9E+0 4.2E-2 Ru-106 3.2E-1 5.8E-2 Sb-125 5.5E-1 3.lE-2 gross a 1.2E-3 6.1E-4 gross 0 1.9E+1 2.6E-1 H-3 3.5E-2 2.2% Sr-90 9.9E+0 35% The increased concentration of Ce-144 and associated alpha activity is expected for RCS dist rbances and is due to a colloidal suspension of finely divided fuel fines resulting from the accident. Concentration elevations of alpha bearing activity, and Ce-144, are projected to be much more significant than reflected in the table above. Short term concentration spikes may increase a factor of 103 or more depending on operations in the R.V.. However, for purpose of 0564X/LC
TER 3527-006 potential source term generation, these time averaged concentrations are assumed to be as tabulated above except for tritium which remains fairly stable at 0.04 pC1/mi, neglecting radioactive decay. Source Terms for Gaseous Effluents When the SDS Technical Evaluation Report was originally written a methodology was conceived for the definition of gaseous effluent source terms resulting from SDS/EPICOR-2 processes. This methodology used defendable, but highly conservative assumptions for defining gaseous effluent source terms. Since the beginning of SDS operation in August 1981, a significant amount of operating experience has yielded effluent data that allows more reasonable gaseous effluent source terms. The effluent data applicable to the EPICOR-2 and SDS operations is reviewed in the following section for purposes of arriving at gaseous source terms appropriate to the proposed future operations of these two systems. A review of the 6/83 version of the SDS TER shows that, according to Table 6.2, the following quantities of the applicable isotopes would have been released to the environment over the previous 27.5 months of SDS operation through the off-gas system had the release values been correct. 0564X/LC
TER 3527-006 Isotope Ovantity (uct) 0 H-3 5.20 x 10 pC1 Sr-90 11.5pC1 1-129 4.125 pC1 Cs-134 31.6 pC1 Cs-137 280 pCi Review of these values against airborne effluent release reports, shows the projected releases from the SDS off-gas system to be highly conservative. Because the data applicable to the SDS Off-Gas system has been reduced so that the amount attributable to this system can be separated from other sources, the following sources attributable to the future SDS/Epicor-2 operations are based on previous operations of these systems. Processed water concentrations, the ultimate source of airborne effluent concentrations, for previous operations will differ from water concentrations to be processed in the future. This initial water concentration difference has been factored into the projected release values considered for this evaluation. 0564X/LC
TER 3527-006 SDS Off-Gas System Releases for the Period 09/15/81 to 12/31/83 SDS Off-Gas Particulate & Tritium Releases Particulate and tritium data as measured by the Off-Cas PING-1A & H-3 bubblers was assembled for the period 9/14/81 to 12/31/83. The total amount of Tritium released through the off-gas system for this period was 7.18E-1 Curtes. The total particulates attributed to sampling through the PING-1A at the off-gas system was 3.15E-7 curies of Cs-137 and 2.52E-8 curies of Cs-134. Cs-134 appeared > LLD on one instance between 12-14-81 and 12-21-81. The SDS Off-gas system feeds to the exhaust ventilation of the Fuel Handling Building at 1000 cfm. The point of insertion into the Fuel Handling Building exhaust is before the HEPA filters, therefore, no increase in particulate is seen at the station vent. In addition, the Fuel Handling Building exhaust is diluted by a factor of 3 by the time it reaches the station vent. Table 6.1 lists the dates of positive particulate samples identified as Cs-137. As a condition to startup of SDS, a tritium sampler in the off-gas system was required. A sampling unit which consists of two Fisker-Milligan bubblers in series was installed downstream of the pump of the PING-1A in the SDS off-gas system. The total cumulative curies released through the off-gas system was integrated for the time period 09/14/81 to 12/31/83 and is 7.18E-1 curies of tritium, Table 6.2 lists the H-3 curies by month and compares amount" released from the station vent, the SDS amount as a fraction of the Station Vent Release and the curies of H-3 released through EPICOR-2. 0564X/LC o
TER 3527-006 Table 6.3 shows environmental release calculations for the groposed RCS processing through SDS and EPICOR-2. The values of column 3 of the table 6.3 are about a factor of 100 lower than would have been estimated by the method of the original SER but are considered to still be conservative. The values in column 3 are the assumed values for the release rate to the environment. The values in column 4 are the concentrations at a downwind distance of 0.5 miles from the station vent, assuming atmosphere dispersion is calculated by the most restrictive data published in NUREG-0683, (Table H-3). The highest value of X/0 from this table in 3.996 E-6 sec/M3 . Using this factor and the dose conversion factor for tritium from Reg. Guide 1.109, an inhalation dose was calculated for the most restrictive recipient, an adolescent. This dose was calculated to be 1.5 x 10-5 mrem /yr. As shown by the value of summation of the Cx/MPCx at the bottom of column 6, the total maximum yearly average concentration for all the isotopes is 16.5 million times more restrictive than allowable under the guidelines of 10 CFR 20 using the more restrictive of the " soluble"/" insoluble" form of each isotope. 0564X/LC
TER 3527-006 Figure 6-1 sues saasas..... y g i i i i i i . .i i _ ,i c, i d 77 ~~ ~ _. i* - g Il
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TER 3527-006 - Table 6.1 Positive Particulate Samples Identified as Cs-137 Dates Curies of Cs-137 Curtes of Cs-134 9-28-81 to 10-5-81 3.17E-9 -
- 12-7-81 to 12-14-81 1.64E-8 -
12-14-81 to 12-21-81 2.49E-7 2.52E-8 12-21-81 to 12-28-81 2.88E-9 - 1-18-82 to 1-25-82 4.53E-9 - 6-14-82 to 6-27-82 4.46E-9 - 9-20-82 to 9-27-82 6.16E-9 - ] 9-25-83 to 10-2-83 1.73E-8 - 11-20-83 to 11-27-83 1.09E-8 - Total 3.15E-7 Curies of Cs-137; 2.52E-8 Curies I of Cs-134 1 i l 4 0564X/LC
TER 3527-006 Table 6.2 Station Tritium Release Values SDS Ping 1A SDS Ping 1A Station Vent H-3, fraction EPICOR-II Dates H-3. C1 H-3. C1 of Station Vent H-3. Cl 9-14-81 to 9-30-81 2.99E-2 5.24E-1 0.0367 2.91E-1 Oct. 81 5.71E-2 3.25E0 0.0176 1.03E-2 Nov. 81 1.17E-1 1.30E1 0.0090 1.20E-2 Dec. 81 6.64E-2 1.14E0 0.0582 3.10E-2 Jan. 82 5.70E-2 5.77E0 0.0099 3.06E-2 Feb. 82 2.12E-2 1.68E-1 0.1262 5.77E-3 Mar. 82 3.54E-2 3.97El 0.0009 7.71E-1 Apr. 82 2.72E-2 1.80E0 0.0151 2.30E-3 May 82 1.02E-2 6.31E0 0.0016 1.26E-3 Jun. 82 9.80E-3 3.06E0 0.0032 6.39E-3 Jul. 82 8.50E-3 1.42E0 0.0060 6.5RE-3 Aug. 82 2.17E-2 1.40E1 0.0016 1.11f-2 Sep. 82 8.80E-3 1.48E1 0.0006 1.30E-2 Oct. 82 1.38E-2 1.17El 0.0012 1.33E-1 Nov. 82 2.84E-2 1.88E0 0.0151 6.50E-2 Dec. 82 2.05E-2 1.02E1 0.0020 2.02E-2 Jan. 83 1.44E-2 3.83E0 0.0038 3.00E-2 Feb. 83 1.08E-2 8.04E0 0.0013 1.01E-2 Har. 83 1.05E-2 3.58E0 0.0029 6.20E-3 Apr. 83 3.00E-2 3.03E0 0.0099 1.02E-3 May 83 7.80E-3 1.61E0 0.0048 3.71E-3 Jun. 83 2.13E-2 1.33E1 0.0016 4.82E-3 Jul. 83 9.50E-3 2.13E0 0.0045 3.56E-3 7.00E-3 3.15E0 0.0022 1.04E-2 Au9 83 Sep. 83 1.33E-3 2.60E0 0.0005 9.10E-3 Oct. 83 2.34E-2 2.15E0 0.0109 4.24E-3 Nov. 83 3.48E-2 2.41E0 0.0144 < LLD Dec. 83 1.38E-2 2.83E0 0.0049 < LLD Total 7.175E-1 177.4 .---- 1.44 C1/ month 2.61E-2 6.45 .---- 5.22E-2 . 0564X/LC
TER 3527-006 Environmental Release Calculations for the Proposed RCS Processing Through SDS and EPICOR-2 The amount of RCS to be processed over a years time is projected to be 1.3 x 10 6 gallons. Concentrations of the various radionuclides in this volume are assumed to be as tabulated below. Table 6.3 RCS Frocessing Release Parameters Conc. Conc. at 0.5 units 10 CFR 20 Cx Isotope (uC1/ml) C1/sec. (Ci/m5) Table II Col. 1 RPCx Ag-110m <1.5E-2 <4.7E-18 <1.9E-23 3E-10 <6.3E-14 Ce-144 1.1E+0 3.4E-16 1.4E-21 2E-10 7.0E-12 Co-60 1.7E-1 5.3E-17 2.1E-22 3E-10 7.0E-13 Cs-134 2.3E-1 7.0E-17 2.8E-22 4E-10 7.0E-13 Cs-137 4.9E+0 1.5E-15 6.0E-21 SE-10 1.2E-11 Ru-106 3.2E-1 9.9E-17 3.9E-22 2E-12 2.0E-12
. Sb-125 5.0E-1 1.6E-16 6.4E-22 9E-10 7.1E-13 Sr-90 9.9E+0 3.2E-15 1.3E-20 3E-11 4.3E-10 H-3 3.5E-2 2.9E-9 1.2E-14 2E-7 6.0E-8 U-235* 3.8E-7 1.2E-22 4.8E-28 4E-12 1.2E-16 U-238* 2.4E-6 7.4E-22 3.0E-27 3E-12 1.0E-15 Pu-238* 4.7E-7 1.5E-22 6.0E-28 7E-14 8.6E-15 Pu-239'. 8.4E-4 2.6E-19 1.0E-24 6E-14 1.7E-11 Pu-240* 2.1E-4 6.5E-20 2.6E-25 6E-14 4.3E-12 Pu-241* 1.4E-2 4.3E-18 1.7E-23 3E-12 5.7E-12 Am-241* 1.4E-4 4.3E-20 1.7E-25 2E-13 8.5E-13 Np-237* 1.1E-7 3.4E-23 1.4E-28 1E-13 1.4E-15 Np-339* 1.7E-8 5.3E-24 2.1E-29 2E-8 1.1E-21 (Gross a) (1.2E-3) (3.7E-19) (1.5E-24) (2E-14) .-----
Cx = 6.05E-8 TOTAL MPCx
- Values calculated according to the Ce-144/ fuel ratio value is calculated by the ORIGEN Computer code as programmed for the TMI-2 Operational history and a decay time of 5.5 years.
l I l I f 0564X/LC
TER 3527-006 Chapter 7 Accident Analysis Becaust of the inherent safety features of the Submerged Demineralizer System and maximum utilization of existing site facilities, potential accidents which involve the release of radionuclides to the environment are minimized. Hypothetical accidents during system operations are proposed and evaluated in the following assessment. The following accident analysis has been performed based on the assumption that zeolite beds are radiologically loaded to 60,000 C1. Should higher radiological loadings be determined to be appropriate, the accident analysis will be reassessed using the higher radiological loadings. 7.1 Inadvertent pumping of RCS water into the spent fuel pool. Assumptions: l The effluent line from the final filter develops a leak and is not detected immediately. Contaminated water is released into the pool at a ! rate of 15 gpm for a period of 15 minutes, (225 gallons or ~15 curies). It is assumed that the total activity is made up of 0.2Ci of Cs-134 and 4.2 C1 of Cs-137, 0.94 Ci of Ce-144, 8.4 C1 of Sr-90, and 0.5 Cl of Sb-125 (based upon the measured concentrations as reported in Chapter 6). Analysis of the accident also assumes uniform mixing in 233,000 gallons of pool water and results in pool water contamination 0564X/LC
TER 3527-006 levels of 0.017 pC1/ml of total activity or of 0.0075 pC1/ml of gamma emitters. This value is only about 37,of the value calculated for the same accident assuming RB " sump" water was inadvertently pumped into the fuel pool water. Occupational Exposure Effects: o The dose rate is calculated to an individual on the walkway at a point three feet above the surface of the water using the ISOSHLD-II computer code. The depth of water in the pool is 38 feet. The calculated maximum exposure rate at three feet above the surface is 4.2 mR/hr. After such an accidental leak the pool would contain -1 millicurie of alpha activity. Such a leak would require that more stringent contamination control procedures would have to be installed to prevent alpha activity from leaving the pool. Cleanup of the pool would require passing the water through 2 specially prepared 4x4 liners; one similar to the SDS liners and one similar to the EPICOR. Off-site Effects: A review of previous SDS operation shows that this accident does not release measurable activity to the environment. f l l No significant increases in the site boundary direct gamma exposure level is expected as a result of this hypothetical accident due to the , spent fuel pool configuratic, and inherent shielding properties of the pool side walls and the distance to the site boundary. 0564X/LC
TER 3527-006
Conclusions:
This hypothetical accident is evaluated under conservative assumptions. Although the analysis of this hypothetical accident provides results that indicate radiation field of 4.2 mR/hr at a level three feet above the pool surface, area radiation monitor alarms would indicate its presence. Personnel would be evacuated to ensure that occupational exposures are limited. Off-site radiological consequences potentially resulting from this hypothetical accident are insignificant. 7.2 Pipe rupture on filter inlet line (above water level) Assumptions: A pipe rupture occurs in the inlet line to the filters above water level at the southeast corner of the pool. The leak proceeds for fifteen minutes before the pump is stopped. Contaminated water sprays from around the lead brick shielding. A total of 38 gallons of water is spread onto a surface area of 100 ft.2 and 340 gallons of contaminated water are drained into the pool. It is further assumed that the contaminated water contains 0.065 C1/ gallon of activity in the same concentration ratios that were assumed.for the previous hypothetical accident. 0564X/LC l l t
TER 3527-006 Occupational Exposure Effects: As a result of this hypothetical accident, five significant effects are postulated:
- 1. The maximum gamma exposure rate at the surface of the contaminated floor area is calculated to be 100 mrem /hr.'
- 2. The maximum beta exposure rate at a point three feet above the surface of the contaminated floor area is estimated to be 560 mrad /hr.
- 3. The exposure rate from the surface of the contaminated spent fuel pool waters, at a point three feet above the surface, would be approximately 6.3 mrem /hr gamma, and ~32 mrad /hr beta.
- 4. The pool water would contain about 1.5 millicuries of alpha activity, and i
l S. the floor surface would be contaminated with about 0.2 millicuries of alpha activity. i Offsite Effects: To calculate off-site concentrations it is conservatively assumed that 0.1% of the activity sprayed from the pipe becomes airborne within the l Fuel Handling Building. This airborne activity is evacuated from the 0564X/LC l
TER 3527-006 Fuel Handling Building by the FHB H&V system which is filtered through HEPA filters before the airborne effluent reaches the environment. The offsite concentration is maximized by assuming the activity is evacuated-from the FHB in a 15 minute time period and, consequently, the hypothetical release to the environment occurs over a 15 minute period. Release parameters for this accident are as tabulated below. Credit has been taken for only 1 of the 2 HEPA filter banks of the FHB exhaust filter system.
== Conclusions:==
Analysis of this hypothetical accident, show that even under the conservative assumptions of the accident, the effluent concentrations, for a period of 15 minutes, are calculated to reach a level such that the summation of the individual. C1/MPCg values is 79% of the allowable. Credit for the neglected HEPA filter and a less conservative X/Q would reduce this fraction to an even lower value. 0564X/LC
TER 3527-006 Release Parameters for a RCS Pipe Spray Leak Accident EA Concentration (C1/M3 ) Release rate Station Vent (at 610m with Isotope to FHB (ci/s) Release Rate (ci/s) X/0-1.3x10-3 s/g3)* Cx/MPCx Ag-110m <2.4E-8 <2.4E-11 <3.1E-14 <1.0E-4 1.8E-6 1.8E-9 2.3E-12 1.2E-2 Ce-144 - 3.5E-13 1.2E-3 Co-60 2.7E-7 2.7E-10 Cs-134 3.7E-7 3.7E-10 4.6E-13 1.2E-3 Cs-137 7.8E-6 7.8E-9 1.0E-11 2.0E-2 Ru-106 5.1E-7 5.1E-10 6.6E-13 3.3E-3 Sb-125 8.0E-7 8.0E-10 1.0E-12 1.1E-3 Sr-90 1.6E-5 1.6E-8 2.1E-11 7.0E-1 H-3 5.6E-8 5.6E-11 7.3E-11 3.7E-4 U-235 6.1E-13 6.1E-16 7.9E-19 2.0E-7 U-238 3.8E-12 3.8E-15 4.9E-18 1.6E-6 7.5E-13 7.5E-16 9.8E-19 1.4E-5 Pu-238 Pu-239 1.3E-9 1.3E-12 1.7E-15 2.8E-2 Pu-240 3.4E-10 3.4E-13 4.4E-16 7.3E-3 Pu-241 2.2E-8 2.2E-11 2.9E-14 9.7E-3 Am-241 2.2E-10 2.2E-13 2.9E-16 1.5E-3 NP-237 1.8E-13 1.8E-16 2.3E-19 2.3E-6 2.7E-14 2.7E-17 3.5E-20 1.8E-12 NP-239 C1 - 0.786 TOTAL APCg 3
- The X/Q value chosen for this analysis (1.3x10-3 S/M ) was used because of the short duration of the release. This precluded the use of the annual average X/Q.
l As shown at the bottom of column 5, the summation of the Cx is only 797. of the MPC, specified 1.0 for this scenario. 1 1 I 0564X/LC l -- - - - - __ _ __
TER 3527-006 Even though high surface contamination levels exist at the floor area and the spent fuel pool waters are contaminated such that the total body could be exposed to relatively high radiation levels, area radiation monitors would indicate trie presence of high radiation. Personnel would be evacuated from the area to ensure that occupational exposures are limited. 7.3 Inadvertent liftino of prefilter above pool surface Assumptions: It is assumed that due to a failure in the trane control system..the over head crane moves toward the loading bay after pulling one expended filter to the maximum height of eight feet below the pool surface. As the crane moves toward the bay, the handling tool hits the end of the pool and the filter is dragged from the water exposing operating personnel. Analysis of the accident is performed by using a point source approximation and calculating the dose rate at a distance of 15 feet from the filter. The calculated dose rate is 21 Rem /hr and is based on an assumed filter loading of 1000 curies. Occupational Exposure Effects: As the filter assembly nears the surface of the spent fuel pool water area, radiation monitor alarms will be sounded announcing the presence of high radiation fields. Personnel would be evacuated from the area to ensure that occupational exposures are limited. - 0564X/LC
TER 3527-006 Off-site Effects: Airborne contamination as a result of this hypothetical accident would not occur since the particulate activity is fixed on the filter elements which are contained within the filter housing. The increase in the radiation level at the site boundary would not be significant due to the shielding characteristics of the fuel building walls and the distance to the site boundary.
Conclusions:
The public health and safety is not compromised as a consequence of this hypothetical accident. , 7.4 Inadvertent lifting of zeolite ion exchancer above pool surface Assumptions: It is assumed that due to multiple failures, a zeolite vessel is lifted from the pool resulting in the exposure of plant operating personnel. Analysis of the accident is performed by modeling the zeolite ion exchanger bed in cylindrical geometry and calculating the dose rate at a distance of 20 feet from the surface of the zeolite ton exchanger. The calculated dose rate is approximately 340 Rem /hr based on an estimated zeolite ion exchange bed loading of approximately 2730 Curles of Cesium-134 and approximately 51,900 Curles of Cesium 137. I P 0564X/LC i l
TER 3527-006 Occupational Exposure Effects: l As the zeolite vessel nears the surface of the spent fuel pool water, area radiation monitor alarms will automatically sound announcing the presence of high radiation fields. Personnel would be evacuated from the area to reduce occupational doses. Airborne contamination would not occur since the activity is fixed on the zeolites. Offsite Effects: Airborne contamination as a result of this hypothetical accident would not occur since the activity is contained on the zeolites which are contained in the ion exchanger vessel. The increase in the radiation
. level at the site boundary would not be significant due to the shielding provided by the Fuel Handling Building walls and the distance to the site boundary.
Conclusions:
The public health and safety is not endangered as a result of this hypothetical accident. Occupational exposures are minimized by evacuation of the area. l l 0564X/LC l l l l
TER 3527-006 7.5 Inadvertent Drop of SDS Shipping Cask Assumptions: It is assumed that due to a failure in SDS shipping cask handling equipment an SDS cask containing a zeolite ion exchanger is dropped from the Fuel Handling Building (FHB) crane to the floor at EL 305'. The SDS shipping cask is assumed to drop from the maximum crane lift height. Upon impact with the floor at EL 305', the SDS shipping cask is assumed to experience rupture as well as rupture of the zeolite vessel, thus exposing the dewatered zeolite resins to the FHB atmosphere. The radiation source is approximately 2730 Curies of Cs-134 and approximately 51,900 Curies of Cs-137 on the zeolite ion exchange media. The contribution from other isotopes on the zeolite media and residual containment building sump water (Table 1.1) in the ion exchange media is negligible; it is assumed that a factor of 10-4 of the isotopes are instantaneously released to the FHB atmosphere. This assumption is conservative because the isotopes are absorbed onto the zeolite media. The Fuel Handling Building HEPA filters are assumed to have an efficiency of 997.. Occupational Effects: i l I Assuming that the SDS shipping cask ruptures completely exposing the zeolite ion exchanger containing the activity mentioned above, the calculated dose rate is approximately 340 Rem /hr at a distance of 20 feet. Upon the rupture of the cask, radiation monitors will sound i 0564X/LC
TER 3527-006 announcing the presence of high radiation fields. Personnel would be evacuated from the area to reduce radiation exposures. Airborne contamination will not occur if the zeollte ion exchange vessels remains intact. With the assumption that the vessels rupture and radioactive material becomes airborne, the airborne activity will be reduced to acceptable levels by the Fuel Handling Building HVAC System prior to atmospheric release. Operational Effects:
- 1. Impact on systems, structures and components has been considered which could possibly result in adversely affecting the ability to operate these Reactor Plants safely, transfer load or unload fuel safely, or maintain these Plants in a safe cold shutdown condition.
- 2. Analysis has been conducted which demonstrates that a postulated SDS Cask drop along the proposed travel path would not adversely affect either TMI Unit 1 or Unit 2.
Off-Site Effects: The increase in radiation level at the site boundary would not be . significant due to the shielding provided by the FHB walls and the distance to the site boundary, if the SDS cask ruptures exposing the zeolite ton exchanger. With the assumption that radioactive material escapes, the whole body dose due to the released activity at the site boundary will be less than 1 mrem for both beta and gamma radiation. 0564X/LC ,
TER 3527-006
Conclusions:
The public health and safety are not compromised as a consequence of this hypothetical accident. t I 0564X/LC l r
TER 3527-006 References Campbell, 0.0,. E.D. Collins, L.J. King, J.B. Knauer, " Evaluation of the Submerged Demineralizer System (SDS) Flowsheet for Decontamination of High-Activity-Level Water at the Three Mlle Island Unit 2 Nuclear Power Station," ORNL/TM-744:, July 1980. Clark, H.E., "The Use of Ion-Exchange to Treat Radioactive Liquids in Light-Hater-Reactor Nuclear Reactor Power Plants," NUREG/CR-0143, ORNL/NUREG/TM-204 (August 1978). Ga, J. H., E. H. Murbach, and A. K. Williams, 1979, " Experience and Plans for Effluent Control at LHR Fuel Reprocessing Plants", in Proc. Conf. on Controlling Airborne Effluents from Fuel Cycle Plants, AICHE Topical Meeting. Lin, K. H., "Use of Ion-Exchange for the Treatment of Liquids in Nuclear Power Plants," ORNL-4792 (December 1973). Lin, K. H., " Performance of Ion-Exchange Systems in Nuclear Power Plants," AICHE Symposium, Ser,11. (152), pp 224-35 (1975). Willingham, H. E., 1972, "The Vitro Engineering ISOSHLD User's Manual," VITRO-R-153. U.S. Department of Health, Education, and Welfare, 1970, Radiological Health Handbook, U.S. Government Printing Office, Washington, D.C. 0564X/LC
'1
TER 3527-006 Chapter 8 Conduct of Operations The SDS program for operations is divided into a phased approach. These phases are: 8.1 System Development System development activities have been performed to assure that components are developed specifically to meet the conditions imposed at TMI and perform in the intended manner. The ion-exchange process is a well understood process. Even though lon-exchange media have been in use for approximately 50 years or more, a development program was conducted at the Oak Ridge National Laboratory, the results of which are documented in ORNL TM-7448, to ensure that the media selected for use at TMI provided optimized performance characteristics of various media using samples of the waters to be processed at TMI. In some cases, SOS effluent will be polished by EPICOR-II. Additional development effort has been expended to verify that media . loading and dewatering can be accomplished in the intended manner and that the remote tools, necessary for the coupling and de-coupling of the vessels, operates in the intended manner. 0564X/LC
TER 3527-006 8.2 System Preoperational Testing Prior to use in the SDS each vessel will be hydrostatically tested in conformance with the reqairements of applicable portions of the ASME Boiler and Pressure Vessel Code. Upon completion of construction, the entire system will be pneumatically tested to assure leak-free operations. The system will be tested to an internal pressure of no less than 1.5 times the design pressure. Individual component operability will be assured during the preoperational testing. Motor / pump rotation and, control schemes will be verified. The leakage collection sub-system, as well as the gas collection sub-system, will be tested to verify operability. Filters for the treatment of the collected gaseous waste will be tested prior to initial operation. System preoperational testing will be accomplished in accordance with approved procedures. SDS system testing will be approved by the GPUN Start-up and Test Manager. 8.3 System Operations System operat10ns will be conducted in accordance with written and approved procedures. These procedures will be applicable to normal system operations, emergency situations, and required maintenance evolutions. 0564X/LC
TER 3527-006 Prior to SDS operation, formal classroom instruction will be provided to systems operations personnel to ensure that adequate knowledge is gained to enable safe and efficient operation. During system operations on-going operator evaluations will be conducted to ensure continuing safe and efficient system operation. 8.4 System Decommissioning The decommissioning plan for SDS is being developed. An outline of the planned approach to decommissioning is shown below. The basis for the decommissioning plan is that the Submerged . Demineralization System is a temporary system; its installation and removal will cause no permanent plant changes.
- 1) Equipment and interconnecting piping will be decontaminated: the levels to which decontamination is accomplished will depend on the intended disposition of individual items, i.e., disposal or reuse.
- 2) The system will be disassembled, component by component. .
- 3) Major system components can be stored for later use or disposed of at a licensed burial facility.
- 4) Small components, such as valves, piping, instruments, etc. can be disposed of as radioactive waste.
0564X/LC _ __- . -- _, _ _ _ _ _. _ ~- - _ _ _ _
TER 3527-006 s Appendix No. 1
- to Submerged Dem!qeralizer System I Technical Evaluation Report i
j REACTOR COOLANT PROCESSING PLAN WITH THE REACTOR COOLANT SYSTEM i j IN A PARTIALLY ORAINED CONDITION d I e i l l 1 t i
- . -,.~,,.--,-,---.-----~,-.nc. , . , . - - _ - -, . . . . --,,_.,n_.n.-.. ,_-.-r. . ., - - - - - . , , , , , . . . , , - , . . - - - . , . . , - - , . , , - - , - - - .
TER 3527-006 CONTENTS Chapter i Summary of Treatment Plan 1.1 Project Scope 1.2 Current RCS Radionucilde Inventory and Chemistry 1.3 RCS Processing Description Chapter 2 RCS Processing Plan Design Criteria 2.1 Introduction 2.2 Design Basis 2.2.1 Submerged Demineralizer System 2.2.2 Interfacing Systems ! 2.3 RCS Process Plan Goal Chapter 3 System Description and Operations 3.1 Introduction 3.1.1 Submerged Demineralizer System 3.1.2 Interfacing Systems 3.2 RCS Water Processing Preparation 3.2.1 RCS Preparation 3.2.2 SPC Operation 3.2.3 Reactor Coolant Liquid Haste Chain 3.3 RCS Water Letdown and Injection 3.4 RCS Processing by SDS 3.4.1 RCS Water Filtration 3.4.2 RCS Water Demineralization 3.4.3 Leakage Detection and Processing
TER 3527-006 CONTENTS (continued) Chapter 3 System Description and Operations (continued) 3.4 RCS Processing by SOS (continued) 3.4.4 Off Gas and Liquid Separation System 3.4.5 Sampling and Process Radiation Monitoring System 3.4.5.1 Sampling System 3.4.5.2 Process Radiation Monitoring System 3.4.5.3 Transurantc Element Honttoring 3.4.6 Ion-Exchanger and Filter Vessel Transfer 3.5 Zeolite Mixtures 3.6 Haste Produced 4.1 RCS Processing Safety Assessment
TER 3527-006 Chapter i
SUMMARY
OF TREATMENT PLAN 1.1 Project Scope The decontamination of the TMI-2 Reactor Coolant System (RCS) requires the processing of the radioactive contaminated water to reduce the activity therein. The present activity level of this water is given in Table 1.1. To date, in excess of 1,000,000 gallons of water have been processed from the RCS. The feed and bleed operation via the Submerged Demineralizer System (SDS) has reduced the radionuclide concentration of the RCS water; specifically the Cs-137 concentration has been reduced from 14.0 pC1/cc to the present value of approximately 0.3 pCl/cc. This report describes the processing of the RCS by the SDS while maintaining the RCS in the partially drained, open condition. The design features of this processing method will utilize:
- 1. proven processing capabilities of the SDS, and
- 2. Existing plant systems in support of the 505.
0862X LC
TER 3527-006 1.2 Current RCS Radionuclide Inventory and Chemistry Hater samples have been taken continuously from the RCS to identify specific radionuclides and concentrations, and plant chemistry. Typical results are listed in Table 1.1. This data is based on actual samples taken. RCS activity is decreasing due to radioactive decay and leakage from the RCS which is being made up by injection of clean water into the RCS, and du? to batches which have been removed for SDS processing. Figure 1.1 shows how activity for the major nuclides has decreased with respect to time. Currently Sb-125 concentrations have risen to radiologically significant levels due to changing RCS chemistry parameters. The Sb-125 will be removed by batching water from SDS through EPICOR using organic resins. 0862X LC
l TER 3527 005 Figure 1.2
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TER 3527-006 1.3 RCS Processing Description On a batch basis, radioactive RCS water is letdown to a Reactor Coolant Bleed Tank (RCBT) while clean water is injected into the RCS from another RCBT. RCS water is then pumped from the receiving RCBT through the prefilter and final filter. RCS water then goes through the RCS manifold and the SDS lon exchangers. The effluent from the ion exchangers is routed through the cation sand filter to another RCBT for chemical adjustment, if necessary, and injection back into the RCS as makeup. The above process is repeated untti the RCS water is decontaminated. ErfCOR II may be used for processing selected batches of RCS water unless needed for chloride control. The processing of the RCS will use the existing filter and ion exchangers of the 505. Existing sampling connections will be used on the influent and effluent of the filters and ion exchangers to determine radionuclide and chemical composition of the RCS before and after processing. As described in the SDS TER, the prefilters, final filters, and cation sand filters for the removal of particulate matter. The l prefilter and final filter are followed by a series of ion exchange 1 ! vessels containing about 8 cubic feet of zeolite ton exchange media. Location, operation, and handling of these vessels remains unchanged from the mode of operation used for processing of the Reactor Building sump water and the RCS water as described in the SDS TER. 0862X LC l i 1
TER 3527-006 TABLE 1.1 RCS RADIONUCLIDE AND CHEMISTRY DATA (May 1986) ISOTOPE RADIONUCLIDE CONCENTRATION pC1/cc H-3 0.085 Sr-90 2.4 Cs-134 0.01 Cs-137 0.35 pH 7.58 Boron 5460 ppm Na 1500 ppm i i l l l l. i I 0862X LC
.,_-e - _ _ ,
TER 3527-006 Chapter 2 RCS PROCESSING PLAN DESIGN CRITERIA 2.1 Introduction This RCS Processing Plan is designed to use the Submerged Demineralizer System (SDS) and portions of existing plant liquid radwaste disposal systems to decontaminate the RCS water. This will reduce plant personnel and off site radiation exposures. The design objectives of this processing plan are to utilize:
- 1. A system that is as independent as possible from existing radioactive waste systems at TMI-2. The SOS portion of this plan is a temporary system for the recovery of TMI-2. Only small sections of existing THI-2 plaat systems will be used.
- 2. A system that has proven performance in processing radioactive waste. The SDS portion of this processing plan has successfully decontaminated the Reactor Building sump and the RCS water.
2.2 Design Basis 2.2.1 Submerged Demineralizer Syste,m The Submerged Demineralizer System was designed in accordance with the following regulatory documents: 0862X LC
TER 3527-006
- 1. Code of Federal Regulations, 10CFR20, Standard for Protection against Radiation.
- 2. Code of Federal Regulations, 10CFR50, Licensing of Production and Utilization Facilities.
- 3. U.S. Regulatory Guide 1.21, dated June 1974.
- 4. U.S. Regulatory Guide 1.140, dated March 1978.
- 5. U.S. Regulatory Guide 1.143, dated July 1978.
- 6. U.S. Regulatory Guide 8.8, dated June 1978.
- 7. U.S. Regulatory Guide 8.10, dated May 1977.
The design basis for the SDS is presented in greater i detail in Chapter 4 of the SDS Technical Evaluation Report. 2.2.2 Interfacina Systems The interfacing systems with the SDS in the RCS Processing system are: 1 1. Radwaste Disposal (Reactor Coolant Liquid) System
- 2. Reactor Coolant Makeup and Purification System
- 3. Auxiliary and Fuel Handling Buildings Heating Ventilation and Air Conditioning Systems
- 4. Nitrogen Supply System .
- 5. Decay Heat Removal System
- 6. Haste Gas System
- 7. Standby Pressure Control System
- 8. Spent Fuel Cooling System
- 9. Instrument Air System .
i 0862X LC
TER 3527-006 The design criteria for these systems (except SPC) are presented in Chapter 3 of the THI-2 FSAR. Conformance to these criteria is presented in the respective sections for these systems in the TMI-2 FSAR. Standby Pressure Control System data may be found in the TMI Recovery System Descriptions and TER's. 2.3 RCS Processina Plan Goal The goal of the RCS Processing Plan is to reduce the total radionuclide concentration of Cs in the RCS to less than 1 pC1/cc. The RCS Chemistry will be maintained as follows as a minimum: Chlorides < 5 ppm pH > 7.5 but < 8.4 Boron > 4950 ppm The processing of water through the SDS is not expected to have any undesirable effect on the chemical characteristics of the RCS water. Maintaining proper chemistry of the makeup water will ensure that there will be no adverse effects on the RCS with respect to corrosion. The boron concentration of the makeup will also ensure that sufficient boron is present to maintain the core in a non-critical safe condition. Sampling of the RCS water will be continued in accordance with approved operating procedure. 0862X LC
TER 3527-006 Chapter 3 SYSTEM DESCRIPTION AND OPERATIONS 3.1 Introduction This RCS Processing Plan is designed specifically for the controlled decontamination of the radioactive water in the RCS and the treatment of the radioactive gases and solid radioactive waste which are produced. This plan will use the SDS as the means of decontamination of the RCS with support from other existing plant systems. 3.1.1 Submerged Demineralizer System The SDS consists of a liquid waste processing system, an off gas system, a monitoring and sampling system, and solid waste handling system. The liquid waste processing system decontaminates the RCS water by a process of filtration and demineralization. The off gas system collects, filters, and adsorbs radioactive gases produced during pro;essing, sampilng, dewatering, and spent SDS liner venting. The sampling system provides measurement of process performance. The solid waste handling system is provided for moving, dewatering, storage, and loading of filters and demineralizer vessels into the shipping cask. Tte SDS will be unchanged from that described in the SOS TER. i
-g. 0862X LC l
i e
TER 3527-006 3.1.2 Interfacing Systems Interfacing with the SDS are existing plant systems, as given in Section 2.2. The Reactor Coolant Liquid Waste Chain provides a staging location for the SDS for collecting and injection of RCS water from and to the RCS. The Fuel Handling Building and Auxillary Building HVAC systems provide tempered ventilating air and controlled air movement to prevent spread of airborne contamination with the plant and to the outside environment. The Nitrogen Supply system provides N2 for blanketing the Reactor Coolant Bleed Tanks. The Makeup and Purification and Spent fuel Cooling Systems provide piping for the transfer of the waste water. The Waste Gas System processes the gases from the vents from the RCBT's. The Instrument Air System provides air pressure for air-operated valves in the Interfacing Systems. The Standby Pressure Control System, installed as a temporary TMI-2 recovery I system, will be used as a backup system to ensure a source of additional makeup to the RCS. 3.2 RCS Water Processing Preparation 3.2.1 RCS Preparation The RCS will be maintained in a partially drained condition vented to atmosphere. Its water level may vary from Elevation 347' to 323'6" depending on the needs for access to the reactor vessel. i 0862X LC l
TER 3527-006 The minimum water level is expected to be 323'6" (l' above the reactor vessel flange). At this level and at all levels above this, the Waste Transfer pumps will be used to inject RCS makeup water into the RCS for the RCS cleanup process. The maximum discharge pressure of these pumps is 74 psig at a flow rate of 40 gpm. Flow to the RCS will be controlled by valve HDL-V-36A or 36B depending on which waste transfer pump is used for feed and, if necessary, MU-V-9. MU-V10 will also be open to permit makeup flow to the RCS. The flow rate to the RCS will be maintained at less than 5 gpm to match the letdown flow rate. Minor adjustments in flow rate will be made to maintain the RCS water level within the limits required. The decay heat analysis as reported in Appendix B TMI-2 Decay Heat Removal Analysts, April 1982, submitted as a part of the Safety Evaluation for Insertion of a Camera into the Reactor Vessel Through a Leadscrew Opening Rev. 2 July 1982, is applicable for the RCS processing described herein. The average incore coolant temperature will be limited to less than 170'F. This criterion was adopted as a conservative value for the recovery program to maintain a positive margin to bolling. ' 0862X LC
TER 3527-006 3.2.2 SPC Operation The Standby Pressure Control System (SPC) will serve as a backup system to ensure that the RCS level is maintained during RCS processing. 3.2.3 Reactor Coolant Llauld Waste Chain Prior to starting RCS water processing, an RCBT will be filled with more than 50,000 gallons of borated, suitable, processed water. The radionuclide and chemistry data for this water will be similar to that used for RCS makeup during the previous RCS processing period. Chemicals will be added to this water if required to ensure that this water complies with the plant chemistry specified in Section 2.3. 1 3.3 RCS Water Letdown and Injection RCS letdown will be performed by a bleed and feed process of simultaneously removing the radioactive RCS water and injecting l borated processed water at the same flow rate to maintain RCS water volume constant. The bleed and feed process will be controlled from the Control Room in coordination with the Radwaste Control Panel. The RCS water is letdown through the normal letdown line on the loop cold leg before Reactor Coolant Pump RC-P-1A. The letdown i rate is 5 gallons per minute if the waste transfer pumps are used 0862X LC I
TER 3527-006 or 10 gpm if a newly in.nlled sandpiper pump (fig. 3.4), which is normally disconnected, is used. The RCS water is letdown through the letdown coolers to a RCBT. The plugged block orifice and isolated Makeup Demineralizers and Filters are bypassed. As the RCS water is letdown, simultaneously the borated processed water located in another RCBT is injected into the RCS. After the RCBT l has been filled to more than 50,000 gallons, the letdown and injection of water from and to the RCS will be secured. The RCBT l will be recirculated prior to processing. After recirculating, decontamination of the RCS radioactive water by the SDS will commence. 3.4 RCS Processing By SDS 3.4.1 RCS Water Flitration Two filters have been installed to filter out solids in the untreated contaminated water before the water is processed by the ton exchangers. Both filters are sand type. The two sand filters are loaded in layers. The first layer is 0.85 mm sand and the second layer is 0.45 mm sand. Mixed uniformly with the sand is approximately 6 pounds boros111cate glass which is at least 22 weight percent boron. The loading of these filters may be changed if applicable. The purpose of the boros111cate is to prevent the possibility of criticality should any fuel fines be transported in the let down. The flow capacity through each filter is 50 gpm. Reverse flow through filters is prevented by a check valve in the , supply line to each filter. 0400B/LC i
TER 3527-006 Each filter is housed in a containment enclosure to enable leakage detection and confinement of potential leakage. The filters are submerged in the spent fuel for shleiding considerations. Contaminated water can be pumped through the filters and the RCS manifold to the ion exchangers. Influent waste water may be sampled from a shielded sample box located above the water level to determine the activity of contaminated water prior to and following filtration. Inlet, outlet, and vent connections on the filters are made with quick disconnect valved couplings which are remotely operated from the top of the pool. Inlet / outlet pressure gauges are provided to monitor and control solids loading. Load limits for the filters are based on filter differential pressure, filter influent and effluent sampling, and/or the surface dose limit for the filter vessel. A flush line is attached to the filter inlet to provide a source of water for flushing the filters prior to removal. 3.4.2 RCS Water Demineralization This system consists of eight underwater columns (24 1/2" x 54 1/2"), each capable of containing eight cubic feet inorganic zeolite sorbent. Homogeneously mixed Ion Siv IE-96 and LINDE-A 0862X LC t ,,
TER 3527-006 zeolite are the medias of choice to efficiently immobilize the Cesium and Strontium in the RCS. Six zeollte beds are divided into two trains each containing two or three beds (A, B, C) with piping and valves provided to operate either train individually or both trains in parallel. 3.4.2 RCS Water Deminaralization (cont'd) The effluent from the zeolite trains flows through the remaining
" cation" sand vessel. Jumpers are provided to permit 2, 3, or 4 vessels per train operation. An in-line radiation monitor measures the activity level of the water exiting the last ten exchanger vessel. The valve manifold for controlling the operation of the primary lon exchange columns is located above the pool, inside a shielded enclosure that contains a built-in sump to collect leakage that might occur. Any such leakage is routed to the off gas bottoms separator tank and pump. A line connects to the inlet of t
eachlonexchangertoprovidewaterforfjushingthelonerchangers when they are loaded. Radionuclide loading of ion excbange vessels is determined by analyzing the influent and effluent from each exchanger. Process water flow is measured by instruments placed in the line to t each lon-exchange train. The effluent from the " cation" sand vessel is routed back to a RCBT, as shown in Figure 3.3. The l remaining SOS equipment and EP:COR*II are not used for RCS water processing.
, 0862X LC
( l' , ( , 4 ,
-1..__ - - - - - _- . __
i TER 3527-006 3.4.2 RCS Water Demineralization (cont'd) I l Periodic sampilng of the process stream will occur during the l processing of a batch of water. At the completion of processing a batch, the contents of the receiving RCBT will be sampled to determine acceptability for injections of this water into the RCS. If the water is within specification, it is injected into the RCS. The types of samples to be taken at RCBT after letdown and prior to reinjection are shown in Table 3.1. 3.4.3 Leakage Detection and Processing Each submerged vessel is located inside a secondary containment box that contains spent fuel pool water. During operation the secondary containment lid is closed. This Ild is slotted to permit a calculated quantity of pool water to flow past the vessels and connectors. Pool water from the containment boxes is continuously monitored to detect leakage and is circulated by a pump through one of the two leakage containment ton exchangers. Any leakage which occurs during routine connection and disconnection of the quick-disconnects will be captured by the containment boxes, diluted by pool water, and treated by ion exchange before being returned to the pool. l 0862X LC l i
TER 3527-006 3.4.4 Off Gas and Liould Separation System An off gas and liquid separation system collects gaseous and liquid wa:tes resulting from the operation of the water treatment system. 3.4.5 Sampling and Process Radiation Monitoring System The sampling glove boxes are shielded enclosures which allow water samples to be taken for analysis of radionuclides and other contaminants. The piping entering the glove boxes permits the withdrawal of a volume limited amount of sample into a collection bottle. Cylinders are purged by positioning valves to permit the water to flow through them and return to a waste drain header and into the off gas separator tank. A water line connects to the sample line to allow the line to be flushed after a sample has been taken. The entire sampling sequence is performed in shielded glove boxes to minimize the possibility of inadvertent leakage and spread of contamination during routine operation. 3.4.5.1 Sampling System Sampling of the SDS process to monitor performance is accomplished from three shielded sampling glove boxes. One glove box is for sampling the filtration system, the second is _ 17 - 0862X LC
TER 3527-006 for sampling the feed and effluent for the first zeolite bed, and the third from sampling the effluents of the remaining zeolite beds and the " cation" sand filter. 3.4.5.2 Process Radiation Monitoring System The SDS is equipped with a process radiation monitoring system which provides indication of the radioactivity concentration in the process flow stream at the effluent point from the last ion exchanger vessel. The purpose of this monitoring system is to provide indication and alarm of radionuclide breakthrough. 3.4.5.3 Transuranic Element Monitoring Filter and process train samples are being analyzed for isotopes of Uranium and Plutonium. 3.4.6 Ion Exchanger and Filter Vessel Transfer in the Fuel Storage Pool Prior to system operation, ion exchanger and filter vessels are placed inside the containment boxes and connected with quick-disconnect couplings. When it is determined that a vessel is loaded with radioactive contaminants to predetermined limits as specified in the Process Control Program, the system will be 0862X LC
TER 3527-006 flushed with low activity processed water. This procedure flushes away waterborne radioactivity, thus minimizing the potential for loss of contaminants into the pool water while decoupling vessels. Vessel decoupling is accomplished remotely. Vessels are transferred using the existing fuel handling crane utilizing a yoke attached to a long shaft. The purpose of this yoke-arm assembly is to prevent inadvertent lifting of the ton exchange bed or filter vessel to a height greater than eight feet below the surface of the water in the pool. This device is a safety tool that will mechanically prevent lifting a loaded vessel out of the water shielding and preclude the possibility of accidental exposure of operating personnel. The ion exchange vessels are arranged to provide series processing through each of the beds; the influent waste water is treated by the bed in position "A", then by the bed in position "B", then by the bed in position "C", and finally by the bed in the " cation" sand filter "A" or "B" position. 3.5 Zeolite Mixtures The SDS lon exchangers will contain a uniform mixture of 10NSIV-96 and LINDE-A lon exchanger media. These two zeolites were selected for their proven capabilities while processing Reactor Building Sump water to remove radionuclides. IONSIV-96 primarily removes 0862X LC
TER 3$27-006 I the isotopes of Cesium and LINDE-A removes the isotopes of 1 l Strontium. i The ratio of loading the two types of lon exchanger media will be determined by experimental data to determine the optimum loading. Periodic sampling of the process stream will be used to verify the performance of the ton exchange media. If necessary revisions will be made to the loading ratios if conditions warrant to achieve the proper decontamination factors. Verification of the performance of the ion exchange media will be made in accordance with the Process Control Plan. 3.6 Waste Produced Based on operating experience processing the Reactor Building sump water, the useful life of a zeolite resin bed is in excess of 100,000 gallons of waste water processed. At this point the DF of the zeolite bed for Strontium goes to 1. 0862X LC
TER 3527-006 Table 3.1 f RCBT HATER SAMPLING RCBT LETDOWN SAMPLE RCBT INJECTION SAMPLE Gama Scan Gama Scan Gross Beta - Gama Gross Beta - Gama Sr-90 Sr-90 pH pH at 77'F Conductivity Conductivity Boron Boron Na Na C1 C1 Sulfates Sulfates H-3 H-3 0xygen Fluorides i 0862X LC
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l TER 3527-006 l 4.1 RCS Processina Safety Assessment Processing of the RCS while in a partially drained condition does 1 not present a unique safety concern. The actual processing of Reactor Coolant is adequately addressed in the SDS Technical Evaluation Report and the maintenance of the Reactor Coolant System in a partially drained condition is adequately addressed in the Quick Look Safety Evaluation. The only evolution not previously addressed is the simultaneous feed and bleed of the Reactor Coolant System in a partially dr?ined configuration. During this evolution, RCS water level will be monitored and maintained by operating procedures. Such procedures will maintain the water level to within six (6) inches of the predetermined level set point. At the present RCS level, to permit incore inspections, this level is 210" 1 6". This level is the same as that established for the Quick Look program and will be monitored in a similar fashion. Thus this evolution will not increase the probability of occurrence or consequences of an accident previously evaluated or create the possibility of a different type accident, nor will the margin of safety as defined in the basis for any Technical Specification be reduced. C 0862X LC e L 3
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1 i: J TER 3527-006 F i 4 4 i
' Appendix No. 2 l' to Submerged Demineralizer System Technical Evaluation Report i
i i Title Internals Indexing Fixture Processing System ]. June 1983 j (Deleted) i i k l l l I \ b I l' i i k l-i v.-,. - _ _ ,,,.-- - - -,-- . . - - - , , , - - - ,
TER 3527-006 Appendix No. 3 to Submerged Demineralizer System Technical Evaluation Report TITLE FUEL TRANSFER CANAL ORAINING SYSTF.H (FCC) JUNE 1985
TER 3527-006 CONTENTS Chapter 1 Summary of Treatment Plan 1.1 Project Scope 1.2 Current Fuel Transfer Canal Activity and Chemistry 1.3 FCC Processing Description Chapter 2 FCC Processing Plan Design Criteria 2.1 Introduction 2.2 Design Basis 2.2.1 SDS 2.2.2 Interfacing Systems 2.3 FCC Processing Plan Goal Chapter 3 System Description and Operations 3.1 Introduction 3.1.1 SDS 3.1.2 Interfacing Systems 3.2 FCC Transfer Operations 3.3 FCC Instrumentation 3.4 FCC Processing by SDS 3.4.1 FCC Water Flitration , 3.4.2 FCC Water Demineralization 3.4.3 Leakage Detection 1
TER 3527-006 CONTENTS (continued) j Chapter 3 System Description and Operations (continued) 3.4 FCC Processin'g by SDS (continued) 3.4.4 Off Gas and Liquid Separation System 3.4.5 Sampling and Process Radiation Monitoring System 3.4.6 Ion-Exchanger and Filter Vessel Transfer in the Fuel Storage Pool 3.5 Zeolite Mixtures Chapter 4 Radiation Protection 4.1 Ensuring Occupational Radiation Exposures are ALARA 4.1.1 Overall Policy
- 4.1.2 SDS Design and Operation 4.1.3 Existing Plant Considerations 4.2 Dose Assessment 4.2.1 On-Site Assessment 4.2.2 Off-Site Radiological Exposures Chapter 5 Conduct of Operations 5.1 System Performance 5.2 System Testing 5.3 System Operations Chapter 6 Additional Accident Scenarios 6.1 Possible Accident Scenarios 6.2 Design Features to Mitigate Effects of Casualty Events 1
TER 3527-006 Chantor i
SUMMARY
OF TREATMENT PLAN 1.1 Project Scope The capability to maintain water clarity and radionuclide concentrations in the fuel Transfer Canal (Deep End) during early defueling operations must be available. The design features of this processing method are:
- 1. Use of the proven processing capabilities of the SDS.
- 2. Use of existing plant systems in support of S05.
- 3. Use of FCC-P-1 (canal drain pump).
- 4. Use of DHC system piping.
This report is presented as an addendum to the previously submitted SOS TER to provide greater detail in those aspects of system design and operation which are unique to the processing of the Fuel Transfer Canal. 1.2 Current Fuel Transfer Canal Activity & Chemistry Water samples are taken weekly to monitor radionuclide activity and chemical parameters of the Fuel Transfer Canal. Current results are listed in Table 1.1. Activity decreases due to decay, however activity in water may increase due to leaching from plenum or activity on canisters being transferred through the Fuel Transfer Canal. 1518X LC I
TER 3527-006 1.3 rec processina Descriotion Figure 1.1 shows a block diagram of the FCC processing flow path. The Fuel Transfer Canal may be processed on a continuous basis through the SDS pre & final filters, one or both trains of ion exchangers, and the cation sand filter with the effluent routed back to the FTC or the 'A' Spent Fuel Pool. In addition the FTC may be processed through the SDS to
- any of the RCBT's. The FCC processing will use the existing SDS filters and ion-exchangers. Existing sampling capabilities will be used to monitor the process as in past processing. Further information on the SDS system may be found in the main sections of the TER. This system will be in service until complete installation of the DHCS.
l l t 1518X LC
't TER 3527-006 Table 1.1 i FTC Radionuclide and Chemistry Data (05/14/86) i Co60 3 x 10-4 pC1/ml Sr90 3.3 x 10-2 pC1/mi Rul06 < 6.1 x 10-5 pCi/ml
- Sb125 3.3 x 10-3 pC1/ml Cs134 3.2 x 10-4 pC1/ml Csl37 1.3 x 10-2 pC1/mi ,
Cel44 < 4.8 x 10-5 pC1/mi Boron 4990 ppm Turbidity 1.25 NTU i ( 4
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TER 3527-006 Chapter 2 FCC PRDCESSING PLAN DESIGN CRITERIA 2.1 Introduction The FCC Processing Plan is designed to use a high capacity submersible pump (FCC-P-1), the Submerged Demineralizer System, and portions of the Defueling Water Cleanup System to maintain water clarity and activity levels in the Fuel Transfer Canal. The design objectives are:
- 1. A system to maintain FTC clarity and radioactivity levels.
- 2. A system that is as independent as possible from existing plant systems. The only portions of this system that are not temporary recovery systems are plant services connections (water, air, electric) and if water is to be processed to a RCBT, the inlet header to the RCBT's (HDL System).
- 3. A system that has proven performance in radioactive waste
~
processing. The SDS has successfully decontaminated to date almost i four million gallons of contaminated liquids. 2.2 Deslan Basis 2.2.1 SDS The design basis of the SDS is presented in Chapter 4 of the SDS TER. 1518X LC
TER 3527-006 2.2.2 I_nterfacina Systems The interfacing systems with the SDS in the FCC Processing system are:
- 1. Reactor Coolant Liquid Waste System
- 2. Reactor. Auxiliary and Fuel Handling Butidings Heating, Ventilation and Air Conditioning Systems.
- 3. Haste Gas System
- 4. Plant Air, Electric, Nitrogen and Demin. Water Systems
- 5. RB Jet Pump
- 6. DHCS-Reactor Vessel Filtration System
- 7. Fuel Transfer Canal Shallow End Drainage System. l The Design Criteria for Systems 1-4 above are presented in the THI-2 FSAR. Systems 5 thru 7 are covered in the SDS System Description.
2.3 FCC Processing Plan Goal The goal of the FCC Processing Plan is 1) to maintain Gross By activity less than 1 x 10-4 pCi/ml to minimize the source term and 2) to maintain turbidity less than INTU to maintain underwater visibility. The processing of this water through SDS has no effect on the chemical characteristics of the water. 4 1518X LC
y _ - _ _ - - _ - _ TER 3527-006 Chantor 1 SYSTEM DESCRIPTION AND OPERATIONS 3.1 Introduction The FCC Processing Plan is designed to maintain radioactivity levels and water clarity in the Fuel Transfer Canal until the OHCS is completed and operational. 3.1.1 Submerged Demineralizer System The 505 consists of a liquid waste processing system, an off gas system, a monitoring and sampling system, and solid waste handling system. The liquid waste processing system decontaminates the FTC l water by a process of filtration and demineralization. The off gas system collects, filters and absorbs radioactive gases produced during processing, sampling, dewatering and spent 505 liner venting. The sampling system provides measurements of process performance. The solid waste handling system is provided for moving, dewatering, vacuum drying, inerrization, storage, and loading of filters and demineralizer vessels into the shipping cask. 1518X LC
TER 3527-a06 3.1.2 Interfacina Systems Canal water is transferred from the FTC using a commercially available high capacity submersible pump. This pump (Canal Drain Pump FCC-P-1) takes suction in the 4" drain located in the deep end of the canal. A 1 1/2 inch 10 rubber hose with quick-disconnect
- two way shut-off type fitting connects the discharge of the pump to -
l the fuel transfer canal drain manifold. The manifold serves as a tie-in point for 3 systems; the Reactor Bldg. Basement Pump system, the fuel transfer canal drain system, i and the FTC Shallow End Drainage System. Double isolation of the FCC processing system from the other two is provided by ball valves j FCC-V003 and FCC-V002 in addition to disconnected / capped 1 connections located on each of the other bra.1ches of the manifold. ! From the manifold, the system uses an existing flow path through Reactor Building penetration R-626, Fuel Handling Building penetration 1551 to tie-in and interface with the 505 system. Power for the pump is supplied from distribution panel PDP-6A, breaker #12. Flos from the FTC may be manually throttled via CN-V-FL-1 or CN-V-FL-3 in SOS if desired. 1518X LC
TER 3527-006 The Fuel Handling Building, Auxiliary Building, and Reactor . Building HVAC systems provide tempered ventilating air and controlled air movement to prevent spread of airborne contamination with the plant and to the outside environment. The Nitrogen Supply system provides N 2 for blanketing the Reactor Coolant Bleed Tanks, should the system effluent be routed to them. The Waste Gas System processes the gases from the vents from the RCBT's. The principal components of the SDS are located in Spent Fuel Pool "B", as shown in Appendix No. 2 Figure 3.1. The piping and components of the systems interfacing with the 505 are located in the Fuel Handling and Auxiliary Buildings. Tanks, pumps, valves, piping, and instruments are located in controlled access areas. Components and piping containing significant radiation sources are located in shielded cubicles, such as the Reactor Coolant Bleed Tanks and the Waste Transfer pumps WDL-P-5A and WDL-P-58 (see Appendix No. 2 Figure 3.2). 3.2 FCC Transfer Operations 3.2.1 Normal Operations The FTC will be filled with RCS grade water. The function of the FCC system is to possible a controlled means of draining or processing this water from the canal. I _9- 1518X LC
TER 3527-006 To start the FCC processing stem, the valves must be aligned and the SDS must be configured per the approved operating procedure and both the connections from SHS-P-1 and DHC-P-1 must be disconnected. The pump FCC-P-1 is started and valves are operated per the procedure to ensure effluents is routed where desired. 3.3 FCC Instrumentation Pump FCC-P-1 is controlled via hand indicating switch FCC-HIS-1, which is located on SDS control panel CN-PNL-1 at El. 347'-6" of the fuel handling building. The switch starts and stops the pump and shows, via a light, that power is being delivered to the pump. The starter FCC-STR-1, for the pump is mounted adjacent to panel CN-PNL-1. Pressure gauge FCC-PI-3 is provided on the canal drain manifold to sense the line pressure downstream of the manifold isolation valves. Fuel Transfer Canal Water level FCC-LI-102 is provided by a bubbler (FCC-VICV-104) through proportional controller FCC-LT-102, with Local s Level indication FCC-LIS-103 which also actuates high/ low level alarms (FCC-LAHL-103). 1518X LC
TER 3527-006 3.4 FCC Processino by SOS 3.4.1 FCC Water Filtration Two filters are installed to filter out solids in the untreated contaminated water before the water is processed by the lon-exchanger. The filters are loaded in layers using various sand sizings to optimize filter performance. Mixed uniformly with the sand is approximately 6 pounds of borosilicate g? ass which is at least 22 weight percent boron, to prevent the. remote possibility of criticality should any fuel fines be transported to the filters. The filters and their containment enclosures, sampling, etc. are unchanged from that in previous sections of this TER. 3.4.2 FCC Water Demineralization This system consists of two trains of lon exchangers consisting of 2 or 3 ton exchangers each. Each ion exchanger contains eight cubic feet of ion organic zeolite sorbent. Piping and valves exist allowing operation of either train individually or both in parallel. The effluents from the two trains of lon exchangers is routed through one of two sand filters installed in the " cation" positions. These sand filters were installed in place of the original cartridge type post filter, and is used to trap zeolite fines and improve effluent clarity. These ion-exchangers, their containment enclosures, sampling, etc. are discussed in more detail in previous sections of this TER. 1518X LC
TER 3527-006 3.4.3 Leakage Detection and Processing Each submerged vessel is located inside a secondary containment box tnat contains spent fuel pool water. During operation the secondary containment lid is closed. This lid is slotted to permit a calculated quantity of pool water to flow past the vessels and connectors. Pool water from the containment boxes is continuously monitored to detect leakage and is circulated by a pump through one of the two leakage containment ion-exchangers. Any leakage which occurs during routine connection and disconnection of the quick-disconnects will be captured by the containment boxes, diluted by pool water, and treated by ton-exchange before being returned to the pool. 3.4.4 Off-Gas and Liquid Separation System An off-gas and liquid separation system collects gaseous and liquid wastes resulting from the operation of the water treatment system. 3.4.5 Sampling and Process Radiation Monitoring System The sampling glove boxes are shielded enclosures which allow water samples to be taken for analysis of radionuclides and other contaminants. The piping entering the glove boxes permits the withdrawl of a volume limited amount of sample into a collection bottle. Cylinders are purged by positioning valves to permit the water to flow through them and return to a waste drain header and into the off-gas separator tank. A water line connects to the sample line to allow the line to be flushed after a sample has been taken. 1518X LC
,s. ,>
y TER 3527-006 n Y
-3 The entire sampling sequence is performed in shielded ^ glove boxes x to minimize the possibility of inadvertent leakage and scread of contamination during routine operation.
3.4.5.1 Samplina System
- 1 Sampling of the SDS process to monitor performance is x, j
accomplished from three thielded sampling glove boxes. One gloveboxisforsamplingthefiltrationsyste.m.the\e:ondis 3 u for sampling the feed and effluent for the first zeolite bed - andthethirdfromsamplingtheeffl[enYsoftheremaining zeolite. e
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3.4.5.2 Process Radiation Monitorina System 6 I The 50S is equipped with a process radiatt'on monitoring system which provides indication of the radioactivity concentrat1,on in the process flow stream at the effluent point from the last ton exchanger vessel. The purpose of this monitoring system is to provide indication and alarm of radionuclide breakthrough. 41 t 1518e LC 1 r . . _ _ _ _ _ _ _ _ _ _ . . _ _ _ . _ _ _ _ _ ________________ _ __. _ _ -
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'!; %' 's i Prior to system operation. ion exchancer and filter vessels are 3 7- ', Q T placed inside fu containment boxes'ind connected with quick-s .
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%Q loaded with radioaktive contaminants to o,rsdatermined . t limits as g y ., '
C . speci,fidt in the Process Control Program, 'the systtii will be I 3' '
+
flushedf1NAlow-activityprocessedwa'ter.[jhisprocedureflushes1,' s, r; d s O away waterborne radioactivity, thus ininimizliig the potertial for , t + . g. 2 , ,g. ,
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g into the pool water wi,lle decoupling vessels. -
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f i Vessel'decoupling is accompiishf.i e, 5ret, W 9.41y. .. 3 Vesseh(sre g [$ransferredusingtheexistingfuelh'a'ndli'nej i crane'5utbzine a'yoQ .,
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, 3; vessel to a height greater than eight' feet below the sur%
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a, t; N,"s ' ! j,' - g d ' t,- 3y y ( y g' Theion-exchangervesselsarearrangedtoprovideseriespr'oce; sing
. . s 3 ,G ' througheachofthebeds;~theinfluentwastewaterisdreatedby '
e 4 the bed in position "A", then by the bed in position '8",[90es s through a bed or jumper in position "C", and U nally by'th'e sand M
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TER 3527-006 3.5 Zeolite Mixtures The SDS lon exchanger: will contain a uniform mixture of 10NSIV-96 and LINDE-A lon exchanger media. These two zeolites were selected for their proven capabilities while processing Reactor Building Sump water to remove radionuclides. IONSIV-96 primarily removes the isotopes of Cesium and LINDE-A removes the isotopes of Strontium. The ratio of loading the two types of ion exchanger media will be determir.cd by experimental data to determine the optimum loading. Periodic sampling of the process stream will be used to verify the performance of the ion exchange media. If necessary, revisions will be made to the loading ratios if conditions warrant to achieve the proper decontamination factors. 1518X LC
i TER 3527-006 CHAPTER 4 Radiation Protection 4.1 Ensuring Occupational Radiation Exposures are ALARA 4.1.1 Overall Policy The objectives with respect to FCC processing operations are to ensure that operations conducted in support of the on-going demineralization program are conducted in a radiologically safe manner, and further, that operations associated with radiattor exposure will be approached from the standpoint of maintaining radiation exposure to levels that are as low as reasonably achievable. During the operational period of the system the effective control of radiation exposure will be based on the following considerations:
- 1. Sound engineering design of the facilities and equipment.
- 2. The use of proper radiation protection practices, including work task planning for the proper use of the appropriate equipment by qualified personnel.
- 3. Strict adherence to the radiological controls procedures as
- developed for TMI-2.
1518X LC
TER 3527-006 4.1.2 SDS Design and Operation The SDS design and operational considerations are given in Chapter 6 of the SDS TER. These design and operational considerations and features remain unchanged from this evaluation. The radiation dose exposures to plant personnel during FCC processing will be lower due to the fact that the radionuclide concentration in the FTC water is significantly lower than those experienced during processing of Reactor Building sump water. The design basis for shielding the SDS equipment is to reduce radiation levels to less that 1 mrem /hr using the radionuclide concentration of 200 pC1/cc of predominately Cesium. The radionuclide concentration of Cesium in the FTC water is currently much less than 0.1 pC1/cc. 4.1.3 Existing Plant Considerations The radiation protection features for the existing plant system , whicti interface with the SDS are described in Chapter 12 of the TMI-2 FSAR. The existing radiation shielding within the Auxiliary Building for the following systems is adequate to reduce the radiation levels to below the design basis of 2 mrem /hr in areas requiring access:
- 1. Reactor Coolant Liquid Waste Chain
- 2. Haste Gas System 1518X LC s
TER 3527-006 4.2 Dose Assessment l 1 l 4.2.1 On Site Assessment Operation of the SDS in the FCC processing mode is expected to require intermitted processing of the FTC as required to maintain water clarity and Gross By activity <1 x 10-4 pC1/ml until DHCS is fully operational. Based on current experience with the SDS this amount of processing is expected to result in a negligible exposure for SDS operating area activities. 4.2.2 Off-site Radioloalcal Exposures Source Terms for Liquid Effluents Liquid effluent from the system will be returned to station tankage for further disposition. Therefore, no liquid source term is identified for this evaluation. Source Terms for Gaseous Effluents The plant vent system is a potential pathway for carrying airborne radioactive material and release. Radionuclides in the gaseous effluent arise from entrainment during transfer of contaminated water to various tanks, filters, ion exchange units, and also from water sampling. For further information, see section 6.3.2 of the SDS TER. 1518X LC i
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TER 3527-006 Cha.pter 5 CONDUCT OF OPERATIONS 5.1 System Performance
- By processing the Reactor Building sump water and RCS successfully assurance has been granted that components developed specifically to meet the conditions imposed at TMI will perform in the intended manner.
The lon-exchange process is a well understooo process. The 505 has demonstrated that high decontamination factors can be achieved by the use of zeolite ion exchange media. i l During FCC processing, the SDS system flow rates may be higher than during all previous processing. An eight hour test was performed to assure that these increased flowrates will not adversely affect zeolite performance. Also, calculations have been performed by ORNL to l l. demonstrate that system performance will not be jeopardized. Although radionuclide breakthrough may occur sooner in the betch, it will progress more slowly. This breakthrough will be allowed to occur to extend zeolite life (minimize wastes) since the effluent is routed back to the Fuel Transfer Canal. Zeolite media loading and dewatering can be accomplished in the intended manner and remote tools, necessary for the coupling and decoupling of the l vessels, operate in the intended manner. l f 1518X LC 6..
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TER 3527-006 5.2 System Testina Prior to use in the SDS each vessel will be hydrostatically tested in conformance with the requirements of applicable portions of the ASME Boiler and Pressure Vessel Code. Upon completion of construction, the entire system was pneumatically tested to assure leak-free operations. The system will be retested prior to IIF processing at the design pressure. Individual component operability will be assured during the _ preoperational testing. Motor / pump rotation and, control schemes will be verified. The leakage collection sub-system, as well as the gas collection sub-system, will be tested to verify operability. Filters for the treatment of the collected gaseous waste will be tested prior to initial operation. System preoperational testing will be accomplished in accordance with approved procedures. 5.3 System Operations System operations will be conducted in accordance with written and approved procedures. These procedures will be applicable to normal system operations, emergency situations, and required maintenance evolutions. 1518X LC
TER 3527-006 Prior to FCC operation, formal classroom instruction will be provided to systems operations personnel to ensure that adequate knowledge is gained to enable safe and efficient operation. During system operations on-going operator evaluations will be conducted to ensure continuing safe and efficient system operation. o 1 1518X LC i
TER 3527-006 Chapter 6 ADDITIONAL ACCIDENT SCENARIOS 6.1 Possible Accident Scenarios 6.1.1 A breech of the system pressure boundary while delivering water from the fuel transfer canal could result in additional contamination of reactor building surfaces. 6.1.2 Introduction of reactor building sump water into the fuel transfer canal would contaminate the canal and could result in a potential criticality problem. 6.2 Desian Features to Mittaate Effects of Casualty Events 6.2.1 A hose or pipe break will result in loss of line pressure. Pressure and flow indication are provided at various locations on the pump discharge flowpath. The piping and hoses are hydrostatically tested to 1.5 times their maximum operating pressure per ANSI B31.1. To ensure pressure boundary integrity, hoses are to be inspected prior to operation of the FCC canal drain network. 1518X LC i
TER 3527-006 6.2.2 The fuel transfer canal drain system and the IIF processing or fuel transfer canal shallow end drainage system connections of the canal drain manifold contain double isolation, which includes a check valve in each line. This is to prevent reactor building sump and ? flush water from being delivered into the canal. In addition, the a coupling connections on the canal drain and fuel transfer canal shallow end drainage branch lines of the manifold are 1 1/2-inches and incorporate a two-way shut-off feature. All other manifold coupling connections, including the reactor building basement jet pump system connection, are 1-inch diameter. This prevents connecting a 1 1/2-inth pump discharge hose to the 1-inch RB i basement jet pump system connection which does not include a check valve. QC is to verify that each hose is connected to the proper manifold branch connection prior to system turnover. i l l l l 4 1518X LC
TER 3527-005 REFERENCES
- 1. SDS System Description Appendix 18.
- 2. TMI-2 Radiochemistry Summary Sheet, Sample No. 86-07106 dated May 14, 1986.
- 3. Bechtel Dwg. No. 2-M75-DHC04, Schematic Diagram: Interim Fuel Transfer Canal Processing System.
1518X LC
E
.TER 3527-006 Appendix No. 4 to Submerged Demineralizer System Technical Evaluation Report TITLE FUEL TRANSFER CANAL SHALLOW END DRAINAGE SYSTEM JUNE 1985
TER 3527-006 CONTENTS Chapter 1 Summary Plan 1.1 Project Scope 1.2 FTC (Shallow End) Activity and Chemistry 1.3 Shallow End Drainage Description Chap +er 2 Design Criteria 2.1 Introduction 2.2 Design Basis 2.2.1 SES 2.2.2 Interfacing Systems 2.3 System Goal Chapter 3 System Description and Operations 3.1 Introduction 3.1.1 SDS 3.1.2 Interfacing Systems 3.2 Shallow End Drainage Operations 3.2.1 Normal Operations 3.3 Shallow End Drainage Instrumentation 3.4 Shallow End Filtration by SDS j 3.4.1 Flitration 3.4.2 Leakage Detection and Processing 3.4.3 Off Gas and Liquid Separation System 3.4.4 Sampling System 3.4.5 Filter Vessel Transfer in the Fuel Storage Pool j i l d
TER 3527-006 CONTENTS (continued) Chapter 4 Radiation Protection 4.1 Ensuring Occupational Radiation Exposures are ALARA 4.1.1 Overall Policy 4.1.2 SDS Design and Operations 4.1.3 Existing Plant Considerations 4.2 Dose Assessment 4.2.1 On Site Assessment 4.2.2 Off Site Assessment Chapter 5 Conduct of Operations 5.1 System Performance , 5.2 System Testing 5.3 System Operations < Chapter 6 Accident Scenarios 6.1 Casualty Events 6.2 Design Features to Mitigate Effects of Casualty Events i 8 e r ._ .,rm,.~.,,r _y, -- . - _ , . - . _ _ - , , -,,,,.-m , , - ,.. _ , - , - - . ,, , . ~ , , , _ . ,--_-,.,w.._-,--,-, .-,--,,___-._--_.~y .
TER 3527-006 F Chapter 1
SUMMARY
PLAN 1.1 Project Scope The capability to transfer water from the shallow end of the Fuel Transfer Canal to the deep end or a RCBT is necessary to deal with FTC dam leakage or overflow, or inleakage from some other source. This report is presented as an addendum to the previously submitted SDS TER to provide details of the transfer of water frcm the FTC shallow end. 1.2 FTC (shallow end) Activity Chemistry j There are r. number of sources which may contribute water to the i shallow end (IIF Leakage, FTC dam leakage, decon, etc.) and therefore it is impossible to state the actual activities or chemistry of the water to be transferred. However water from all of these sources has been transferred / processed through SDS in the past, and any possible sources have been covered in detall in previous sections of this TER. i 1 l j 1519X LC v - , n- c-- - n e , ,-- ,-r--r - - - , - - + - - , - - , , . , - s- ----- -v--,-,,-,- ,-,,-m
TER 3527-006 , 1.3 Shallow End Drainage Description Figure 1.1 shows a block diagram of the shallow end drainage flow paths. The shallow end of the FTC may be transferred to the deep end of the FTC, or the RCBT's, with or without filtration through the SDS pre- & final-filters. i i I i l. l l l l l l 1519X LC j l i
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1 TER 3527-006 Figure 1.1 5 Jbhk US -o ' b 2 2 e i \ l. e 6 -n 4 EI *3
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TER 3527-006 Chapter 2 DESIGN CRITERIA 2.1 Introduction The FTC Shallow End Drainage System is designed to use a submersible pump (DHC-P-1) previously used as the IIF Processing Pump, and portions of: the SDS Feed & Filtration subsystem, the Reactor Coolant Liquid Haste Disposal System and the Fuel Transfer Canal Drain System. The Shallow End Drainage System design objectives are:
- 1) capability to drain shallow end by transfer to deep end or existing tankage.
- 2) as independent from existing plant system as possible.
- 3) use SDS or portions thereof.
2.2 Desian Basis 2.2.1 SDS See Chapter 4 of the SDS TER. 1519X LC
. - ~ . _ ,_._ , ,._ -------- , -.. .. _ , , , _ _ . , , ,__ _ , _ . -- _. .,.,y, ,y ,, ._ , _ y. ,__._......m _-._,_.
TER 3527-006 2.2.2 Interfacina Systems The interfacing systems with the SDS in the Shallow End Drainage System are:
- 1) Reactor Coolant Liquid Waste System
- 2) Reactor, Auxiliary and Fuel Handling Building Heating, Ventilation and Air Conditioning System
- 3) Haste Gas System
- 4) Plant Services (Air, Electric, Nitrogen and Demin. Water)
- 5) RB Jet Pump
- 6) DHCS - Reactor Vessel Filtration System
- 7) FCC - Fuel Transfer Canal Drainaga System.
The design criteria for systems 1-4 are presented in the THI-2 FSAR. The remaining systems are covered by the SDS System Description. 2.3 System Goal The goal is to provide a system capable of transferring water from the shallow end of the RTC back to the deepend or the RCBT's. , I i 1 1519X LC
l 1 TER 3527-006 Chapter 3 l l I SYSTEM DESCRIPTION AND OPERATIONS 4 3.1 Introduction The FTC Shallow End Drainage System is designed to allow pumping of water from the shallow end back to the deepend or to the RCBT's for future processing as necessary. 3.1.1 SDS The portions of the SDS used, consist of a liquid filtering system, an off gas system and a sampling system. The liquid filtering system if used removes soltas from the transfer stream. The off gas system collects, filters and absorbs radioactive gases produced I during sampling, dewatering and vessel venting. The sampling system provides measurements of flitration performance. 3.1.2 Interfacing Systems i Canal water is transferred from the shallow end using a commercially available submersible pump. This pump, DHC-P-1 (formerly the IIF processing pump) is installed on Elev. 308'-0" and takes suction in an existing 4" drain located in the New Fuel Pit. A 1 1/2" ID rubber hose with quick-disconnect two way shut-off fitting connects the pump discharge to the FCC manifold. 1519X LC
TER 3527-006 The manifold server as a tie-in point for 4 systems; the RB Jet Pump, the Fuel Transfer Canal Drain System (FCC), the DHCS-Reactor . Vessel Flitration System (Early Defueling) and the FTC Shallow End Drainage System. Double isolation of all other systems from the Shallow End Drainage system is provided by manifold isolation valves and the disconnecting of the SHS, FCC and DHC hoses from the manifold. From the manifold, the discharge hose is either routed to the FTC deep end or through the existing flow path through RB penetration R-626 and FHB penetration 1551 to the RCS manifold at SDS. Power for the pump is supplied from circuit 11 of distribution panel PDP-6-A. From the RCS manifold, flow may be filtered through the SDS Pre and Final Filters, or may bypass the filters. The receiving tank in either case is one of the RCBT's. The Fuel Handling, Auxiliary and Reactor Building's HVAC systems provide tempered ventilating air and controlled air movement to prevent the spread of airborne contamination within the plant or to the environment. The Nitrogen system provides Ny for blanketing the RCBT's when transferring to them. The Waste Gas system stores and processes the gases from the RCBT vents. 3.2 Shallow End Drainage Opr ations 3.2.1 Normal Operation 1 The fuel transfer canal shallow end drainage system is a temporary modification In the reactor building designed to pump water from the shallow end of the canal and deliver the water to the deepend i of the canal or the reactor coolant bleed tanks (RCBT)'s. 1519X LC
TER 3527-006 During defueling operations, the shallow end of the FTC may require drainage as a result of leakage, spills, or deliberate flooding of the canal. This system provides the means to accomplish this drainage. The fuel transfer canal shallow end drainage opera +1on is started and stopped by opening or closing valve FCC-V003 and using on/off hand switch DHC-HIS-1. Tils, in turn, automatically starts or stops pump DHC-P-1. 3.3 Shallow End Drainaae Instrumentation Pump DHC-P-1 is controlled via hand indicating switch OHC-HIS-1, which is located on 505 control panel CN-PNL 1 at El. 347'-6" of the fuel handling building. The switch starts and stops the pump and contains indicating lights for pump status. The starter, DHC-STR-1, for the pump is mounted adjacent to panel CN-PNL-1. A local emergency stop switch, DHC-HS-1, is located in the Reactor Building near the pump on El. 347'-6". This local switch overrides the indicating switch, and the pump can be started again only after the local switch has been reset. Pressure gauge FCC-PI-3 is provided on the canal drain manifold to sense the line pressure downstream of the manifold isolation valves. IS19X LC 1
TER 3527-006 Air-operated valve FCC-V003 is interlocked with the pump such that the valve must be opened before the pump will start. A high level alarm is provided at control panel CN-FNL-1 to inform the operator to begin draining the pit. A low level alarm is also provided at CN-PNL-1 to inform the operator to stop the pump. The low level alarm will not alarm when the pump is off. 3.4 Shallow End Filtration by SDS 3.4.1 Filtration Two sand filters are installed to remove solids from the canal water prior to storage in tanks for future processing. The filters contain layers of variously sized sand uniformly mixed with borosilicate glass which is added to preclude criticality conceras. The filters and related SDS subsystems are uce. hanged ( from that discussed in pre /lous sections of this TER. 3.4.2 Leakage Detection and Processing The filters are located inside submerged containment boxes which are monitored rnd recirculated through the SOS Leakage Containment System which is unchanged from that discussed in previous sections this TER. 3.4.3 .. Gas and Licuid Seperation System An off-gas and liquid separation system collects gaseous and liquid wastes resulting from the operation of the filtration system and sampling. IS19X LC
F. TER 3527-006 3.4.4 Samplina System Sampling of the filtration influent and effluent to monitor filter performance is accomplished using the shielded High Rad Filter Sampic Glove Box. This system is discussed in detail elsewhere in this TER. 3.4.5 Filter Vessel Transfer in the Fuel Storage Pad Prior to system operation, filter vessels are placed inside the containment boxes and connected to the system using quick-disconnect couplings. When it is determined that a filter is loaded with solids (based on ap), the filter is flushed with low-activity processed water, transferred to a storage location in the pool or the dewatering station, and replaced with a new filter. I .i d 1519X LC
TER 3527-006 Chapter 4 RADIATION PROTECTION 4.1 Ensurina Occupational Radiation Exposures are ALARA 4.1.1 Overall Policy The objectives with respect to Shallow End Drainage Operations are to ensure operations are conducted in a radiologically safe manner and radiation exposure will be maintained as low as reasonably achievable. The effective control of radiation exposure will be based on the following considerations:
- 1. Sound engineering design of facilities and equipment.
- 2. Use of proper radiation protection practices and qualifiable personnel.
- 3. Strict adherence to THI-2 radio'ogical controls procedures.
4.1.2 SDS Deston and Operation The SDS design and operational considerations are given in Chapter 6 of the SDS TER. These design and operational considerations and features remain unchanged from this evaluation. The radiation dose exposures to plant personnel during Shallow End Drainage operations will be lower due to the fact that l 1519X LC
TER 3527-006 activities of canal water should be significantly lower than that experienced during processing of RB sump or initial RCS processing. The SDS shielding design basis is levels less than 1 mr/hr using 200 pC1/cc Cesium. 4.1.3 Existina Plant Considerations The radiation protection features for the existing plant and systems which interface with the SDS are described in Chapter 12 of the THI-2 FSAR. 4.2 Dose Assessment 4.2.1 On Site Assessment Operation of the 505 Filtration system in the FTC Shallow End Drainage mode may be required intermittently to drain the shallow end of the canal. Based on past SDS operating experience, the exposure for SDS operating area activities due to this operation is expected to be negligible. 4.2.2 Offsite Assessment Source Terms for Liould Effluents All liquid effluent from the system 111 be retained in station tankage. Source Terms for Gaseous Effluents The plant vent system is a potential pathways for gaseous or airborne release, see section 6.3.2 of this TER. 1519X LC 1
TER 3527-006 Chapter 5 CONDUCT OF OPERATIONS 5.1 System Performance Past processing experience i.e., filtering RB sump and Tank Farm water, assures that the filtration system will perform in the intended manner. During Shallow End Drainage Operations, the flow rates through the filters,may approach 50 gpm. Filters will be taken out of service on high differential pressure. Filter changeout and dewatering can be accomplished in the intended manner using remote long-handled tools. 5.2 System Testina Prior to use, each SDS vessel will be hydrostatically tested in conformance with the requirements of applicable portions of the ASME Boller and Pressure Vessel Code. Upon completion of construction, the entire system was pneumatically tested to assure leak-free operations. Individual component and subsystem operability was preoperationally tested satisfactorily in accordance with approved procedures. 1519X LC
TER 3527-006 5.3 System Operations System operations will be conducted in accordance with written and approved procedures. These procedures will be applicable to normal system operations, emergency operations, and required maintenance evolutions. During system operations on-going operator training and evaluation will be conducted to ensure continuing safe and efficient system operations. I i 1
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1519X LC
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1 TER 3527-006 Chapter 6 ACCIDENT SCENARIOS 6.1 Casualty Events 6.1.1 A breech of the system pressure boundary while removing water from the shallow end of the fuel transfer canal could result in additional contamination of reactor building surfaces. 6.1.2 Introduction of this water into the fuel transfer canal could contaminate the canal. 6.2 Design Features to Mitigate Effects of Casualty Events 6.2.1 A hose or pipe break will result in loss of line pressure. Pressure and flow indication are provided at various locations on the pump discharge flowpath. The piping and hoses are hydrostatically tested to 1.5 times their maximum operating pressure per ANSI B31.1. To ensure pressure boundary integrity, hoses are to be inspected prior to operation of the canal shallow end drainage network. 1519X LC
r TER 3527-006 6.2.2 The fuel transfer canal and the shallow end drainage system branch connections of the fuel canal drain manifold contain double isolation, which includes a check valve in each line. This is to prevent reactor building sump and flush water from being delivered into the canal. In addition, the coupling connections on the canal drain and shallow end drain lines of the manifold are 1 1/2-inches and incorporate a two-way shut-off feature. All other manifold coupling connections, including the reactor building SHS system connection, are 1-inch diameter. This prevents connecting a 1 1/2-inch pump discharge hose to the 1-inch SHS system connection which does not include a check valve. QC is to verify that each hose is connected to the proper manifold branch connection prior to system turnover. i Ifl9X LC
TER 3527-006 Appendix No. 5 to Submerged Dominera11zer System Technical Evaluation Report TITLE EARLY DEFUELING DWC REACTOR VESSEL FILTRATION SYSTEM JUNE 1985
TER 3527-006 CONTENTS Chapter 1 Summary of Treatment Plan 1.1 Project Scope 1.2 Current RCS Radionuclide Inventory and Chemistry 1.3 Early Defueling DWC Reactor Vessel Filtration System Description Chapter 2 RV Flitration Processing Plan Design Criteria 2.1 Introduction l 2.2 Design Basis i 2.3 RV filtration Processing Plan Goal Chapter 3 System Description and Operations 3.1 Introduction 3.2 Reactor Vessel filtration System Operations 3.2.1 Normal Operations 3.2.2 Infrequent Operations 3.3 Reactor Vessel filtration System Instrumentation and Control ! 3.3.1 Controls 3.3.2 Power 3.3.3 Monitoring 3.3.4 Trips and Interlocks 3.4 RV/11F Processing by the Reactor Vessel Filtration System /SDS 3.4.1 Filtration 3.4.2 Demineralization
F TER 3527-006 CONTENTS (continued) Chapter 4 Radiation Protection 4.1 Ensuring Occupational Radiation Exposures are ALARA 4.1.1 Overall Policy 4.1.2 SDS Design and Operation 4.1.3 Existing Plant Considerations 4.2 Dose Assessment 4.2.1 On-Site Assessment 4.2.2 Off-Site Assessment Chapter 5 Conduct of Operations 5.1 System Performance 5.2 System Testing 5.3 System Operations Chapter 6 Additional Accident Scenarios 6.1 Possible Accident Scenarios and Design features to Mitigate their Effects. 6.1.1 Loss of Power 6.1.2 Loss of Instrumentation / Instrument Air 6.1.3 Filter Media Rupture 6.1.4 Line and Hose Break
-q TER 3527-006 Chapter 1
SUMMARY
OF TREATMENT PLAN 1.. Project Scope During early defueling, after the removal of the IIF pump, Reactor Vessel water clarity will be maintained using the Reactor Vessel Filtration portion of the DHCS. Prior to the completion of the remaining portions of the DHCS, a capability of processing the kCS must be available to maintain or decrease activity levels in the water and respective dose rates to workers over the vessel. To achieve this, a slipstream from the Reactor Vessel filter Trains will be routed through the Filter Canister Post Filter and hosed to the existing FCC Drain Manifold / flow path to 505 for demineralization. The effluent from SDS will be routed to a RCBT while concurrently making up to the RCS from another RCBT. This report describes the post IIF pump removal processing of the RCS by the Reactor Vessel Filtration System, SDS and other interfacing plant systems for the maintenance of RCS water clarity and radionuclide concentrations. This report is presented as an addendum to the previously submitted SDS Technical Evaluation Report (TER) to provid's greater detall in those aspects of system design and operation which are unique the processing of the RCS using the Early Defueling DWC Reactor Vessel Flitration System. 1520X LC
TER 3527-006 1.2 Current RCS Radionuclide Inventory and Chemistry Water samples are taken weekly from the RCS to identify radionuclide concentrations and water chemistry. Current results are listed in Table 1.1. RCS activity decreases due to decay, leakage and subsequent makeup, and RCS processing. RCS activity may increase due to leaching or disturbance of core material. The RCS activity when the Reactor Vessel Flitration System begins operation is expected to be essentially the same as Ilsted in Table 1.1 (Antimony activity may increase by a factor of 2). 1.3 Early Defuelino OWC Reactor Vessel Filtration System Description Figure 1.1 shows a block diagram of the Early Defueling DWC Reactor Vessel Flitration System flowpath. RCS water is continuously filtered through one or both filter trains and returned to the Reactor Vessel at a rate of up to 200 gpm per filtration. If water requires demineralization due to increasing radionucilde concentration, a shipstream from the filter train effluents may be processed through SDS at up to 15 gpm to a RCBT while concurrently making up with RCS grade water to the RCS from another RCBT. The flow path from the filter train effluents passes throJgh the Filter Train Postfilter and is hosed to the FCC Orain Manifold on to 505 and the receiving RCBT. The return (makeup) flow path is identical to that used during !!F processing and pre-headlift processing. 1520X LC
TER 3527-006 .' 4 The processing system will use the existing lon exchangers and effluent sand filters of the SDS. Existing sampling connections will be used on ' the influent and effluent of all SDS filters and ion exchangers to determine radionuclide and chemical composition of the process stream before and after processing. As described in the SDS TER, the sandfilters and lon exchangers, their locations, operation and hand 11ng of, remain unchanged from the mode of l operation used for OF and pre headlift processing. Both trains of lon-exchangers may be used. I i 4 f t + 1 t i i - 1520X LC I r
rT' TER 3527-006 TABLE 1.1 RCS RADIONUCLIOE AND CHEMISTRY DATA (05/19/86) ISOTOPE RADIONUCLIDE CONCENTRATION pC1/cc H-3 0.085 Sr-90 2.4 Sb-125 0.093 Cs-134 0.01 Cs-137 0.35 CHEMISTRY pH 7.58 Boron 5460 ppm Na 1500 ppm C1 1.15 ppm Turb 13 NTU 1520X LC
1 TER 3527-006 Figure 1.1 M u & R -M- M u g n _L , .- [ l i
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F TER 3527-006 Chapter 2 RV FILTRATION PROCESSING PLAN DESIGN CRITERIA 2.1 Introduction The Early Defueling DHC Processing Plan is designed to use high capacity submersible pumps (DWC-P-2A and B) and two trains each consisting of two filters. Additionally, portions of both the 505 and existing plant Liquid radwaste disposal systems are used to clarify and decontaminate the RCS water. This will reduce radiation exposure to plant personnel and will reduce the possibilities for off-site radiation exposures. The design objectives of this processing plan are:
- 1) to filter the water in the Reactor Vessel and RCS to remove suspended solids and maintain water clarity at or below 1 NTU.
- 2) to remove soluble fitslon products from the water through demineralization by batch processing through 505 to the RCBT's, thus reducing the dose rate contribution of the water to defueling personnel.
- 3) to use the 505 which has proven its performance in the decontamination of RCS water.
- 4) to use the proven reinjection pathway to the RCS previously used ,
during !!F and prehead lift processing of the RCS. I l 1520X LC 1 l t
TER 3527-006 2.2 Desian Basis 2.2.1 101 The design basis for the SDS is presented in detall in Chapter 4 of the SDS TER, 2.2.2 Interfacina Systems The interfacing systems with the RV Filtration System /SDS are:
- 1) Reactor Coolant Liquid Waste Train.
- 2) Purification and Makeup System
- 3) AFHB HVAC.
- 4) Nitrogen Supply System.
- 5) Waste Gas System.
- 6) SPC System,
- 7) Instrument Air System.
- 8) Fuel Transfer Canal Orain System.
The Design Criteria for systems 1-5 and 7 above are presented in Chapter 3 of the TMI-2 FSAR. System 6 is covered in the SPC System Description. System 8 is covered in the SOS System Description. 1520X LC i
n TER 3527-006 2.3 RV Filtration Processina Plan Goal , The goal of this system is to maintain reactor vessel water clarity at 1 NTU or less, and the concentrations of Cs I37 and Sb 125 less than or equal to 0.02pCI/ml and 0.15pC1/ml respectively. It should be noted 125 that $b will be Ilmited by processing through EPICOR as necessary. The RCS chemistry will be maintained as follows: Chlorides < 5 ppm ; pH > 7.5 but < 8.4 Boron > 4750 ppm r The filtering / processing of RCS water by the RV Filtration System /SDS does not have any effect on the chemical characteristics of the RCS water. The specified chemistry will ensure there are no adverse effects on the 505 with respect to corrosion while ensuring boration sufficient to maintain the core in a noncritical safe condition. 1520X LC
[ TER 3527-006 Chapter 3 SYSTEM DESCRIPTION AND OPERATIONS I i 3.1 Introduction 1 J The Early Defueling DNC Reactor Vessel Flitration system is a temporary Ilquid processing system which is designed to process water contained in the reactor vessel. The system is comprisG of the flitration portion of the Reactor Vessel Cleanup System, the Submerged Domineralizer System i i (SDS), Reactor Coolant Bleed Tanks (RCBT) and the return pathway from the RC8Ts to the reactor vessel used for the !!F Processing System, See figure 1.1 for a compilefied diagram of the OWC RV Filtration System I Flowpath, ! 3.1.1 10.1
- The SOS consists of a liquid waste processing system, an off gas i system, a monitoring and sampling system, and solid waste handling system. The 11 gold waste processing system decontaminates the RCS water by a process of filtration and domineralization. The off-gas system collects, filters and absorbs radioactive gases produced during processing, sampling, dewatering and spent SOS liner
- venting. The sampilng system provides measurements of process i
j performance. The solid waste handling system is provided for moving, dewatering, vacuum drying, Inertiration, storage, and loading of filters and domineralizer vessels into the shipping cask. ! 1520X l.C )
e TER 3527-006 3.1.2 Interfacina Systems The RCS water is transferred from the RV/!!F using two commercially available submersible pumps (OHC-P-2 A/B). The water is filtered by one or both of the RV Filtration System Filter trains and returned to the RV/IIF. A slip stream from the filter train effluents may be routed through the filter train postfilter and hosed to the FCC Drain Manifold. The manifold serves as a tie-in point for 4 systems; the Reactor Bldg. Basement Pump system, the Fuel Transfer Canal Orain System, the New Fuel Pit Drain System, and the Reactor Vessel Filtration (OHC) System. Double isolation of the OHC system from the other three is provided by air operated ball valve FCC-V003 and check valve FCC-V016 in addition to manual valves and disconnected / capped connections located on each of the other branches of the manifold. From the manifold, the system uses an existing flow path through Reactor Building penetration R-626, fuel Handling Building penetration 1551 to tie-in and interface with the SOS system. Subsequent makeup to the RV/!!F is accompitsbed by transferring reactor coolant grade water from a RCBT to the RV/11F via a waste l transfer pump and an existing flow path through the HDL and MU systems to a cold leg of the reactor coolant system. The roles of the RCBT's can be interchanged provided valves are properly realigned and the tank used to fill the !!F contains reactor coolant grade water. 1520X LC
TER 3527-006 Flow from the RV/!!F may be manually throttled at valves CN-V-!X-25 and CN-V-!X-26 in SDS if desired. Flow to the RV/11F may be automatically controlled by valve MU-V9 based on RV/!!F water level or manually controlled using WOL-V-167 and WOL-V-36A. Shutoff of the RV/!!F supply (via WOL-V40) is achieved automatically in the event of unacceptable water level in the !!F and may also be manually accomplished at several locations. The Fuel Handling Building, Auxiliary Building, and Reactor Building HVAC systems provide tempered ventilating air and controlled air movement to prevent spread of airborne contamination with the plant and to the outside environment. The Nitrogen Supply system provides N2 for blanketing the Reactor Coolant Bleed Tanks. Reactor Coolant grade water currently contained in the RCBT's provides borated water for injection into the RV/!!F for the initial fill operation. The Waste Gas System processed the gases from the vents from the RCBT's. The Standby Pressure Control System, installed as a temporary THI-2 recovery system, will be used as a safety system to ensure that a secondRCSinjectionpathisavailable. The principal components of the 505 are located in Spent Fuel Pool "B". The piping and components of the systems interfacing with the 505 are located in the Fuel Handling and Auxillary Buildings. Tanks, pumps, valves, piping, and instruments are located in controlled access areas. Components and piping containing 1520X LC
TER 3527-006 significant radiation sources are located in shleided cubicles, such as the Reactor Coolant Bleed Tanks and the Waste Transfer pumps WOL-P-5A and WOL-P-58, 3.2 Reactor Vessel Filtration System Operations 3.2.1 Normal Operations Normal operation of the system is in one of the modes shown in Table 1. The mode of operation chosen is based on the particulate and radioactivity concentrations in the Reactor Vessel. Table 1 Early Defueling DHC RV Filtration System Operational Configurations FILTER FLOW (GPM) SDS FLOW (GPM) Return to Reactor Vessel With Equivalent Return to Reactor Vessel 400 (200) 0 . 385 (185) 15 (Numbers in brackets indicate flow if only one train is in operation.) The operational mode is determined by the solids loading in the i reactor vessel. Normally, 400 gpm from the reactor vessel is filtered and 7 to 15 gpm of the filtrate is domineralized. As the filters load up, the pressure differential across the filter train increases. As the differential pressure increases, the flow rate is maintained constant by manually adjusting remote valves V015A and V0158 (HV-30A and 308). 1 1520X LC !
TER 3527-006 3.2.2 Infreauent Operations Flushing of the system may be performed when the internal contamination level gets high or prior to internal maintenance work. The system is shutdown prior to flushing. One flushing option allows a gravity flush from SPC-T-4. Borated water is stored in the charging water storage tank, SPC-T-4, located at the 347 ft. elevation in the Fuel Handling Building. This tank is connected to the Early Defueling DHC RV Filtration System. Elther filter train may be flushed without stopping f*ow through the other. Flushing may be accomplished by opening one of the inlet valves from the flushing system (depending on which portion of the system is to be flushed) and then opening the drain valve to the fuel transfer canal. After sufficient time has been allowed to flush the system, tne draln valve is closed and then the inlet valve is closed. The system is then restarted. System inventory can be decreased or increated as needed by mismatching flow routed to/from the RCBT's. This may be done by changing the set point on RC-LIC-102. Also, the water can be routed to the RCBT as required for processing to remove Sb-125. 1520X LC
TER 3527-006 3.3 Reactor Vessel Flitration System Instrumentation and Control 3.3.1 Controls The majority of system control is handled remotely from a control panel which is located in the Fuel Handling Building. This is due to the fact that much of the system is located in the Reactor Building which has 11mited access. The reactor vessel cleanup pumps do have local hand switches to shut the pumps down. Filtered water flow back to the reactor vessel is monitored by the operator and adjusted by remotely controlled valves V015A and V0158 , (HV30A&B). On/off controls for the waste transfer pumps are located on radwaste panel 3018, and in the control room on control panel 9. ! P Valve HDL-40 has existing open/close controls located on radwaste panel 301B and in the control room on control panel 9. Additional , open/close controls are located on SOS control panel CN-PNL-1. . WOL-V40 terminates flow in the event of high or low water level in the !!F. A block switch is located on CN-PNL-1 which can be used to block the low level trip to permit filling the !!F to the desired level. f 1520X LC < t
1 TER 3527-006 . Water level is automatically maintained at a prescribed level (approximately 327'-6") in the !!F by valve MU-V9. Section 2.2 documents the actual set points. The control signal to valve MU-V9 1s provided by the reactor water level monitoring system (bubbler) through proportional controller RC-LIC-102 which is located on control panel SPC-PNL-3. 3.3.2 Power The pump motors are supplied with 480V power through a motor control center (2-32C) which is energized by an existing unit substation located in the Aux 111ary Bu11 ding. 120 VAC power will be supplied from the control panel or local sources. 3.3.3 Monitorina Monitoring equipment is provided to evaluate the performance of the system and to and in proper operation of the system. The discharge pressure of the submersible well pumps is monitored (PI-4A f. 48) to determine if the pump is operating correctly and also to provide another Indication that the pump is operating. In order to determine the degree of filter loading, the primary filter canisters and the secondary post filter are equipped with remote indication of differential pressure across the filters (DPI-5A, OPI-58 and DP!-33). The differential pressure across the canisters will be used to determine when the filters are loaded to capacity. 1520X LC
r-- TER 3527-006 The process fluid conditions are monitored to deteraine thc-effectiveness of the system. The turbidity level in the fluid is monitored (Al 43A & 438) prior to its return to the source. Also, the capability to obtain grab samples of process fluid has been provided for at several locations in the system. 3.3.4 Trios and Interlocks The reactor vessel cleanup well pumps, P-2A/B, are provided with low level setpoint trips to ensure that the pumps do not operate under potential cavitation conditions. A low level in the !!F will also trip pumos P-2A and P-28. The reactor vessel cleanup well pumps P-2A/B are equipped with interlocks to prevent them from being started during a low level condition. Valve HOL-V40 will be tripped closed on high level in the IIF. This prevents over filling of the !!F. 3.4 RV/I!F Processina by Reactor Vessel Filtration System / SOS 3.4.1 Filtration The system has two submersible type pumps (deep well pumps), P-2A and 28, which are housed in wells and located in the fuel storage pit in the shallow end of the fuel transfer canal in the Reactor 1520x LC
l TER 3527-006 Building. The suction from the reactor vessel is through the Westinghouse work platform via hoses which connect the nozzles provided on the work platform to the wells. The system has four particulate filters, F-1, 2, 3 and 4. The filters are composed of sintered filter media which is contained in modified fuel canisters. These filters are capable of removing debris, mainly fuel fines (U0 2) and core debris (Zr0 2), down to a 0.5 micron rating. Since the canisters contain fuel fines, they are designed to prevent a criticality condition from cxisting when they have been loaded. Also, the filters are submersed in the transfer canal to provide the appropriate radiation shielding. The two pumps and four filters are arranged so that one pump discharges to two filters. Therefore, the filtration portion of the system is divided into two trains, each train contains one pump which feeds two filter canisters. The two pump arrangement allows for greater flextbt11ty in system operations and provides redundancy to allow system operation during maintenance. A filter is used continuously until the differential pressure reaches a predetermined setpoint. At this point the system is shutdown and then, after a waltiig period (approximately 5 min.), it is restarted. The differential pressure is noted and if it returns to a low value the system will be run again to the pressure setpoint. This process is repeated until the differential pressure 1520X LC
I TER 3527-006 at restart reaches a value near the shutdown setpoint. When this occurs within one hour, the train is shutdown and the filters are replaced. Loaded canister s are expected to generate small quantitles of oxygen and hydrogen gas due to radiolysis of water. Pressure relief valves R-4, R-5, R-6, and R-7 are provided on the filter canister outlet lines upstream of their isolation valves. Their purpose is to prevent overpressuring the filter canisters when isolated due to the small quantitles of H and 2 02 produced (approximately 0.029 ft 3/ day.) Once the water has been filtered, all, or a portion of, the flow can be returned to the Reactor Vessel. The amount of water returned is controlled by remotely adjusted valves V015A'& B (HV30A&B). Each of these lines will connect, via flexible hoses, to the separate inlet nozzles on the work platform. A sparger has been placed on each return line to maintain a positive pressure in the attached hoses. Sample points are provided upstream and downstream of each filter train. These samples are routed to sample box 1, a glove box located in the FHB. The glove box has a self contained blower and HEPA filter which discharge to the FHB ventilation system. 1520X LC
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TER 3527-006 3.4.2 Demineralization To remove soluble fission products, flitrate not returned to the reactor vessel, can be batch processed through SDS and then routed to a RCBT while concurrently returning an equal amount of reactor coolant grade water to the RV from another RCBT. A 1 1/2 inch hose, equipped with " quick disconnect" two way shutoff fittings, connects the Early Defueling DHC RV Filtration System to the SDS via the fuel transfer canal drain manifold. The manifold serves as a tie-in point for 3 other systems; the surface suction system (sump-sucker), the fuel transfer canal drain system, and the Shallow End Drainage System. Double isolation of the Shallow End Drainage System from the other two is provided by air operated ball valve FCC-V003 and check valve FCC-V016 in addition to manual valves located on each of the other branches of the manifold. The Early Defueling DHC RV Filtration System will use the same connections to the manifold as otherwise used by the fuel transfer canal drain system. From the manifold, the system uses an existing flow path through Reactor Building penetration R-626 and fuel handling building penetration 1551 to SDS and then to a RCBT. The SDS pre and final l filters may be bypassed when processing using the Early Defueling DHC Reactor Vessel filtration system. N The roles of the RCBT's can be interchanged provided valves are , properly realigned and the tank used to fill the IIF contains reactor coolant grade water. 1520X LC C
r TER 3527-006 Flow from the IIF may be manually throttled at valves CN-V-IX-25 and/or CN-V-IX-26 in SDS if desired. Flow to the IIF is. controlled automatically or manually by valve MU-V9 based on IIF water level. Shutoff of the IIF supply (via WOL-V40) achieved automatically in the event of unacceptable water levels in the IIF and may also be manually accomplished at several locations. The details of the SOS ton exchanger trains and related components may be found elsewhere in this TER. i j 1520X LC i
TER 3527 005 CHAPTER 4 Radiation Protection 4.1 Ensurina Occupational Radiation Exposures are ALARA 4.1.1 Overall Policy The objectives with respect to RCS processing operations are to ensure that operations conducted in support of the on-going demineralization program are conducted in a radiologically safe manner, and further, that operations associated with radiation exposure will be approached from the standpoint of maintaining radiation exposure to levels that are as low as reasonably achievable. During the operational period of the system the effective control of radiation exposure will be based on the following considerations:
- 1. Sound engineering design of the facilities and equipment.
- 2. The use of proper radiation protection practices, including work task planning for the proper use of the appropriate equipment by qualified personnel.
- 3. Strict adherence to the radiological controls procedures as developed for THI-2.
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( TER 2527-006 4.1.2 SDS Desian and Operation The SDS design and operational considerations are given in Chapter 6 of the SDS TER. These design and operational considerations and features remain unchanged from this evaluation. The radiation dose exposures to plant personnel during RV/IIF processing will be lower due to the fact that the radionuclide concentration in the RCS water is significantly lower than those experienced during processing of prehead lift RCS water, IIF water and Reactor Building sump water. The design basis for shielding the SDS equipment is to reduce radiation levels to less that 1 mrem /hr using the radionuclide concentration of 200 pC1/cc of predominately Cesium. The radionuclide concentration of Cesium in the RCS water is currently less than 0.5 pCl/cc. 4.1.3 Existing Plant Considerations eb The radiation protection features for the existing plant system which interface with the SDS are described in Chapter 12 of the ! THI-2 FSAR. The existing radiation shielding within the Auxiliary Building for the following systems is adequate to reduce the radiation levels to below the design basis of 2 mrem /hr in areas requiring access:
- 1. Makeup and Purification System
- 2. Reactor Coolant Liquid Haste Chain
- 3. Miscellaneous Waste Chain
- 4. Haste Gas System 1520X LC i
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TER 3527-006 4.2 Dose Assessment 4.2.1 On Site Assessment Operation of the SDS in the RV/IIF processing mode is expected to i require 50,000 gallons of processing per week from installation of the Reactor Vessel Filtration system until the completion of the Defueling Water Cleanup System. This amount of processing is required to maintain Cs-137 concentration at less than 0.1 pC1/mi in order to maintain radiation levels in the reactor vessel head area as low as reasonably achievable. Based on current experience with the SDS this amount of processing is expected to result in an ' exposure for SDS operating area activities of < 0.225 man-rem / week. 4.2.2 Off-site Radiological Exposures i Source Terms for Liauld Effluents i Liquid effluent from the system will be returned to station tankage for further disposition. Therefore, no liquid source term is identified for this evaluation. 1 1 s t 1520X LC
C TER 3527-006 Source Terms for Gaseous Effluents The plant vent system is a potential pathway for carrying airborne radioactive material and release. Radionuclides in the gaseous effluent arise from entrainment during transfer of contaminated water to various tanks, filters, ion exchange units, and also from water sampling. For further information, see section 6.3.2 of the SDS TER. l l 1520X LC
T TER 3527-006 Chapter 5 CONDUCT OF OPERATIONS 5.1 System Performance By processing the Reactor Building sump water and RCS successfully assurance has been granted that components developed specifically to meet the conditions imposed at TMI will perform in the intended manner. The lon-exchange process is a well understood process. The SDS has demonstrated that high decontamination factors can be achieved by the use of zeolite ton exchange media. During RV/IIF processing, the 505 system flow rates will be higher than during all previous processing. An eight hour test was performed to assure that these increased flowrates will not adversely affect zeolite performance. Also, calculations have been performed by ORNL to demonstrate that system performance will not be jeopardized. Although radionuclide break through may occur sooner in the batch, it will progress more slowly. This breakthrough will be allowed to occur to extend zeolite life (minimize wastes) since the effluent is routed back to the RV/IIF. l Zeolite media loading and dewatering can be accomplished in the intended manner and remote tools, necessary for the coupling and de-coupling of l the vessels, operate in the intended manner. 1520X LC
F TER 3527-006 5.2 System Testino Prior to use in the SDS each vessel will be hydrostatically tested in conformance with the requirements of applicable portions of the ASME Boller and Pressure Vessel Code. Upon completion of construction, the entire system was pneumatically tested to assure leak-free operations. The system will be retested prior to RV/IIF processing at the design pressure. Individual component operability will be assured during the preoperational testing. Motor / pump rotation and, control schemes will be verified. The leakage collection sub-system, as well as the gas collection sub-system, will be tested to verify operability. Filters for the treatment of the collected gaseous waste will be tested prior to initial operation. System preoperational testing will be accomplished in accordance with approved procedures. 5.3 System Operations System operations will be conducted in accordance with written and approved procedures. These procedures will be applicable to normal l l system operations, emergency situations, and required maintenance l evolutions. 1520X LC
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r TER 3527-006 4 Prior to RV Filtration System operation, formal classroom instruction will be provided to systems operations personnel to ensure that adequate knowledge is gained to enable safe and efficient operation. During a system operations on-going operator evaluations will be conducted to l ensure continuing safe and efficient system operation. 1 h r i 1520X LC
( TER 3527-006 Chapter 6 ADDITIONAL ACCIDENT SCENARIOS 6.1 Possible Accident Scenarios and Design Features to Mitigate their Effects 6.1.1 Loss of. Power A loss of power to the entire system would simply shut the system down. A loss of power to the well pumps would shutdown the filtration portion of the system which would in turn cause level control RC-LC-102 to close MU-V9 terminating flow from the RCBT. Loss of power to individual components would place the component in its safe mode. An air operated valve, for example, would fall to a position that ensures no damage to other components. Loss of power to the control panel would cause the loss of all information and fall all control and solenoid operated valves. The system would be shutdown until power is restored. 6.1.2 Loss of Instrumentation / Instrument Air loss of instrumentation would hamper operations but no adverse conditions would result and the system could be safety shut down-until the problem is resolved. I 1520X LC
r-TER 3527-006 Loss of a single instrument channel will result in the loss of indication for that channel and, for those channels that have control features, a flow mismatch. This flow mismatch will result in an automatic shutdown of the affected portion of the system. Loss of the internals indexing fixture (IIF) level indication system (bubbler) will result in an erroneous level indication which will be noted when compared with a redundant level indication system. Since this system has no control features, no adverse system conditions will result. Loss of instrument air will take the individual components to their fail safe position. Flow mismatches induced by loss of air will result in automatic trips. Loss of air to the IIF level monitoring system will initiate a low air supply pressure alarm. 6.1.3 Filter Media Rupture A failure of the filter media in the canister could potentially release fuel fines to the SDS portion of the system. A post filter is located downstream of both filter trains in the line to the SDS. This filter will trap any fuel fines which would be transported past the filter canisters in the event of filter l failure. The post filter is designed to be criticality safe and is sized so that a small accumulation of debris will increase the differential pressure to the alarm setpoint. Also, the nephelometers in the return line would alert the operator to a possible media rupture since the turbidity would increase rapidly. 1520X LC
TER 3527-006 The recovery procedure is to isolgte the filter trains and find the ruptured filter by observing the differential pressure versus flow for each individual canister. Lower differential pressure for a given flow will indicate that this filter is ruptured. That canister or canisters and the post filter cartridge would be replaced and the system restarted. 6.1.4 Line and Hose Break The consequences of any line and hose break is a loss of reactor vessel inventory. The system has been designed to mitigate the consequences of such an incident to the extent possible. To help prevent a hose rupture, all process hoses are armored. In case of a hose rupture or line rupture, downstream of the reactor vessel pumps, P-2A & 28, the system is equipped to trip these pumps on the IIF low level and alarm to the control panel. This event could deliver aoproximately 500 to 1000 gallons of reactor vessel water to the area of the break. The potential areas affected would be the Reactor Building and the fuel Handling Building, each of which has sumps or drains to the Aux. Bldg. sumps to contain the I spill. I l i If a suction hose to the well pumps or a return hose to the reactor vessel should rupture, a siphoning of reactor vessel water would take place. The two 4 inch suction connections provided in the Westinghouse work platform are provided with two 3/4 inch holes drilled 18 inches below the water level which will act as a siphon 1520X LC l l
TER 3527-006 breaker. The}tjee2inchreturnlinesareequippedwithspargers, which are simply holes drilled into the pipes. The first holes are drilled 18 inches below the water level which will act as a siphon breaker. The sample return line is terminated 18 inches below the water level. Therefore, a maximum of approximately 3000 gallons of reactor vessel water would spill into the fuel transfer canal following a hose rupture. Approximately half of this water would be contained in the New Fuel Pit. The recovery from these events would be accomplished by isolating the ruptured section and replacing the ruptured hose / pipe. 6.1.5 Deboration Boron dilution of the Defueling Water Cleanup System will be addressed in Revision 2 of the GPU Nuclear TMI-2 Division " Hazards Analysis Potential for Boron Dilution of RCS" (4430-84-007R). 1520X LC i}}