ML20063A041
| ML20063A041 | |
| Person / Time | |
|---|---|
| Site: | Fort Calhoun  |
| Issue date: | 08/18/1982 |
| From: | William Jones OMAHA PUBLIC POWER DISTRICT |
| To: | Clark R Office of Nuclear Reactor Regulation |
| References | |
| LIC-82-279, NUDOCS 8208240165 | |
| Download: ML20063A041 (22) | |
Text
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Omaha Public Power District 1623 HARNEY e OMANA, NESRASMA 48102 s TE LEPHO N E S36 4000 AREA CODE 402 August 18, 1982 LIC-82-279 fir. Robert A. Clark, Chief U. S. fiuclear Regulatory Commission Offica of fiuclear Reactor Regulation Division of Licensing Operating Reactors Branch tio. 3 Washington, D.C.
20555
Reference:
Docket fio. 50-285
Dear Mr. Clark:
Report on the Spill and Cleanup of Glycol in the Fort Calhoun Station Spent Fuel Pool (SFP)
As requested by Omaha Public Power District's Project fianager, please find attached a report concerning the unintentional introduction of glycol into the SFP in October, 1981 and the subsequent methods and results of the pool cleanup.
On October 17, 1981, a maximum of 40 gallons of Texaco Type 46 hydraulic fluid was spilled into the SFP as a result of the failure of a fuel inspection stand hydraulic line.
The fuel inspection stand is owned by Combustion Engineering and has since been removed from the pool.
High turbidity, suspended solids, and a surface foam resulted from the spill. After a thorough analysis to determine the best course of cor-rective action and after completing the necessary manpower and hardware arrangements, a filtration process for clearing the pool was initiated in February,1982.
Several cleanup system variations and filtering iterations were completed over the next three months, as detailed in the attached report.
The SFP clarity was returned to normal conditions by June 5, 1982.
The steel bucket in the SFP, which was determined to be a contributing factor to the pool turbidity, will be removed from the pool before commencement of the 1983 refueling outage.
In the interim, the normal SFP cleanup and demineralization system will maintain the inte-grity of the pool water.
S'npers) l Y
W. C Jov}es Divisiori JManager Production Operations WCJ/TLP:jmm Attachment cc:
LeBoeuf 820 8 Z4 0 I(o9 h,1 amb, Leiby & MacRae
OMAllA PUBLIC POWER DISTRICT REPORT REGARDING Tile CLEANUP OF THE FORT CALHOUN STATION SPENT FUEL POOL FOLLOWING THE INTRODUCTION OF GLYCOL 1
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_ _ ~
3 i
i
SUMMARY
i A spill of hydraulic fluid into the Fort Calhoun spent fuel pool caused j
a degradation in visibility. This is believed to have been due to the glycol present in the hydraulic fluid which acted as a nutrient for the growth of a type of water fungus. Another contributing factor was the presence of colloidal iron, apparently from a carbon. steel bucket j
housing cut up incore detectors in the pool. A filtration project was instituted for the removal of suspended solids. The removal of the glycol was a secondary soal; however, this appeared to be the final solution to the turbidity problem.
The pool was initially stratified, with total suspended solids between 6 and 15 mg/ liter. This was apparently the fungus, which was 20 microns in diameter and 50 microns long. Glycol concentration was initially measured to be 27 ppm, with a pH of 4.5 to 5.0.
Subsequent glycol analysis showed concentrations up to 225 ppm.
This apparently was due j
to the hydraulic fluid breaking down into its pol,yalkylene glycol and ethylene glycol constituents.
The filtration took 13 weeks to return the pool to its original clarity.
The initial system was a dual-train header with a 10 micron cartridge filter followed by 2 charcoal beds in each train.
This provided a maximum system flow rate of 100 ppm.
System modifications were made during the project which added a coagulant injection system, 1 micron and 0.2 micron cartridge filters, and acid-washed charcoal beds placed in a 6 train system. Glycol removal by charcoal adsorption was found to-be flow dependent during testing.
Pool side testing was performed to evaluate the effectiveness of various media for the removal of suspended solids and glycol.
i The final chemical analysis of the spent fuel pool showed a turbidity of l
0.6 NTU with a pH of 5.7.
Visibility in the pool was restored to initial conditions. Techniques for glycol removal were not completely success-i ful as approximately 20 ppm of polyalkylene glycol is remaining in the j
pool. This glycol is expected to degrade and be removed by use of the in-line fuel pool demineralization system.
Assessment of the District's efforts in cleaning up the glycol spill and i
resultant fungus growth has provided two suggestions for mitigating similar accidents at other facilities maintaining such pools:
1)
Remove all sources of rusting iron in the pool as colloidal iron was believed to have a significant role in the. turbidity problems at the Fort Calhoun Station.
1 2)
Surface turbidity problems can be controlled by effectively skim-ming the surface of the pool for crud immediately following a glycol spill, since the surface turbidity was determined to be caused by aerobic fungi growing near the pool surface.
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I.
Ih"IRODUCI' ION On Oc+mber 17, 1981, hydraulic fluid was spilled in the spent fuel-pool (SFP) at the Fort Calhoun Station.
Estimates of the volme spilled 3
varied from a few gallons up to 40 gallons.
We constituents of the fluid were 40% ethylene glycol,19% polyalkylene glycol and 41% DI water.
The SFP visibility began degrading and on October 20, 1981, the +4p of the fuel racks were no longer visible.
On October 23, 1981, a transfer of water from the transfer canal caused a surface foam +o be formed.
This increased with agitation.
A microscopic observation of the SFP water on Novenber 10, 1981, identi-fled a filamentous fungus Phycomycetes (water mold) which was 20 microns in diameter and 50 microns long.
'Ihe layer of surface film contained a fungus (mono zerticillate penecilliun).
W e fungus was known to consume ethylene glycol; however, it was believed it would not madily consume the polyalkylene glycol.
Pool side testing was accomplished in December with a Halliburton filter and a 1 micron Gon-Nuclear filter. Rese tests showed the filters would remove solids without pluggiag with an extended throughput.
We Fort Calhoun Plant Review Omrnittee (PRC) and OPPD Technical Services met on December 31, 1981.
It was decided that filtration of the SFP to remove suspended solids should be initiated as soon as possible.
It was recognized, at this point, that removal of the glycol appeared +w be the final solution to the suspended solids and turbidity problem.
The options available for glycol removal were:
)
o Use of charcoal to adsorb the glycol. Bere was a wide range of estimates on the volune of charcoal required to accomplish this.
o Use of the Fort Calhoun vacuum evaporator to reprocess the SFP water.
Ecre is in excess of 12,000 lbs. of boric acid in the 215,000 gallons of water in the SFP.
Bis represented a signifi-cant volune of waste for solidification and disposal.
o A combination of the above methods, i.e; partial drain dowTi of the SFP to the evaporator and the filtration with charcoal of the remaining water.
On January 20, 1982, a planning meeting was held at Fort G1houn.
Pre-sent were representatives of the Fbrt &lhoun staff, OPPD Technical Ser-vices, Dmbustion Engineering (C-E) and m em-Nuclear Systems, Inc.
(CNSI).
A tentative schedule was generated and the filtration approach was agreed upon.
We initial physical and chemical characteristics of the SFP water were given as follows:
o Solids,20 x 50 micron, 7 to 14 ppn o Glycol - 27 ppn o pH
- 4.5 to 5.0
)
Rose. attending the meeting agreed upon the combination fioer filtering and charcoal filtering approach.
We proposed system was a dual-train header unit designed for 100 gpn with a maximum operating pressure of 150 psi. Each train would contain a 10 micron filter vessel followed by two charcoal vessels.
%e initial set-up is shown in the system diagram,
}
Figure 1.
II.
INITIAL OPERATIONS AND CHEMISTRY (A)
Week Ending February 20, 1982 Chem-Nuc1 car's personnel arrived on-site at Fort Otlhoun on Feb-ruary 15, 1982.
Af ter completion of site badge training and un-loading the filtration equipnent, system assembly was begun.
We cask decon pit adjacent to the SFP was assigned as the process area. Assembly was conpleted on February 16, 1982 and preparations made for initial fill of the vessels.
At this point, concern was expressed by C-E that trace elements could be released from the chrcoal.
Wis would be due to the low pH of the SFP water washing the ash content from the charcoal.
C-E was particularly concerned about sulfates.
We reco'mendation was made that the charcoal be flushed with DI water and the effluent sampled for sulfates.
We charcoal was soaked overnight after filling.
Subsequently a total of 1300 gallons of DI water was flushed through the system at 10 gpn. W e sulfates analysis at the systen effluent showed less than 10 ppn.
In addition, the first 600 gallons of SFP water was used as a secondary flush.
We effluent was directed to a floor drain at a flow rate of 5 gpn.
This was to simulate the acidic environment the charcoal would be operating under. Sulfate analysis on the effluent was less than 10 h
pPn.
Recirculation of the SFP began on February 20, 1982. W e "B" train was placed in service at 40 gpn.
A total of 8,300 gallons were processed on Fbbruary 20, 1982.
(B)
Week Ending February 27, 1982 The radiation levels on the pressure vessels increased significant-ly within the first 12 hours1.388889e-4 days <br />0.00333 hours <br />1.984127e-5 weeks <br />4.566e-6 months <br /> of operation.
In particular, the charcoal vessels began loading activity, mainly Cobalt-58 and Cobalt-60 in the fonn of colloids that were suspended due to the
, pH.
Actual SFP pH (measured at the system influent) was 6.0 to
- 6. 5.
Decontamination factors (DF) varied from 2 to 30.
Olem-Nuclear recommended shielding be provided as soon as possible.
Four shields designed for use with CNSI pressure vessels were in-stalled on February 25, 1982.
Stratification of the SFP was indicated by solids analysis prior to beginning recirculation.
Bis was also indicated by system in-fluent pH, which varied with the depth of the suction hose.
On February 21, 1982, the suction hose was lowered to a depth of 9 feet. Bis was lowered to 12 feet on February 22, 1982.
We suc-tion hose was located at the opposite end of the pool from the dis-charge hose, providing a cross current in the SFP. Analysis run on 7)
February 23, 1982 showed that the SFP was no longer stratified.
On February 27, recirculation was put on a 24-hour per day
schedule.
(C)
Week Ending hhrch 6,1982 3
On Ehrch 2, 1982, the suction hose was lowered to a depth of 35
/
feet.
This action was taken because the recirculation was at the upper levels of the pool and there was little or no circulation below the suction hose.
A stratification study run on hhrch 2 showed a slightly higher turbidity at the SFP surface and at the 30 and 40 feet levels.
Appendix 3 contains the complete chemistry data received by Olem-Nuclear.
Throughout the first three weeks of recirculation, the turbidity across the system decreased.
his was in the range of 0.2 to 2.7 NTU.
However, the system influent turbidity gradually increased.
The cause of this increase could have been due to:
o he high velocity of the flow through the depth type filters and charcoal beds.
his would cause the organic matter to break down into snaller particles.
o lhe colloidal material at the bottom of the SFP migrating V) the upper levels of the pool.
The mechanism for this would be the disturbance caused by Fort Qtlhoun's SFP cooling system opera-ting or by the cross current fran the filtration sys*wm.
o A conbination of both.
Cn Ehrch 5, four 4) new charcoal vessels were installed.
These incorporated 1 ft of mixed bed resin for removal of any trace
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elements.
An acid-washed charcoal with a lower ash content and a higher Iodine nunber was identified and onployed in future vessels.
(D)
Week Ending March 13, 1982 poolside colunn tests were run on hhrch 9, using Rohm a lhas XAD-2 resin and the acid-washed charcoal. %e results were as follows:
XAD-2 Resin Charcoal Turbidity (NTU)
Glycol (ppn)
Turbidity (NTU)
Glycol (ppm)
Inf.
6.6 38 6.6 38 Eff.
1.0 20 0.2 25 1hc charcoal vessels were replaced on Mtrch 12 with the acid-washed charcoal vessels.
These also incorporated the 1 f t3 of mixed bed resin.
The results from a set of samples drawn 30 minutes af ter start-up at 3 gpn were as follows:
I Ig, Specific Conductivity Turbidity (NTU)
Glycol (ppn)
Inf.
5.6 46 7.3 48 l
Eff.
6.4 2.2 0.2 0
)
Subsequent samples at higher flow rates showed little change in the turbidity or glycol concentration.
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In addition, two 1 micrt>n filters were installed dowr. stream of the 10 micron filters and prior to the charccal vessels.
Rese were 4
identical in design with the existing vessels.
Figure 2 shows the system diagram with these filters ins',allcd.
(E) hoek Ending March 20, 1982 A low flow test was conducted on %rch 17, 1982 to ascertain if the glycol Irmoval capability of charcoal was flow dependent.
Tests were conducted at 3, 6 and 12 gpn.
However, the length of the run times did not allow for thorough exchange of the water already in the vessels.
Following the low flow test, the suction hose was lowered to a depth of 40 feet.
We CNSI technician noted that the feed ptinp was straining and was limited +o 50 gpn.
(F)
Week Ending March 27, 1982 yat l On the morning of March 22, the bearing in the feed ptanp failed.
s he CNSI technician notified the Waste Processing Field thintenance g
Shop in ihrnwell, South Grolina and arrangenents were made to ship a replacement by air freight.
While the system was shutdown, CNSI set-up a poolside coltinn +est with Rohm & Haas IRA-938 macroreticular resin.
Eis test was needed to evaluate this resin's effectiveness in removing colloids fron the SFP water.
Testing had identified colloidal iron less than 1 micron in size.
It was believd the source of this-iron was a steel bucket irrnersed in the pool.
The' replacement ptrnp head arrived and was installed on March 24.
The system passed a pressure test using plant service wa'er.
Upon
.T start-up, a leak developed from the feed pump, which was due +4 a
/
defective shaft seal. Arrangernents were made +4 have the pump man--
ufacturer ship a replacement pump head to Fort Glhoun.
CNSI also sent a lead mechanic from South Grolina out to Fbrt 61houn +o assist the technicians.
On Shrch 26, the replacenent ptinp was installed and recirculation of the SFP restanal.
(G)
Week Ending April 3,1982 The low flow test was repeated on Ehrch 30, 1982.
E is test showed glycol renoval was dependent on flow.
pH, Conductivity Turbidity Glycol Inf.
5.4 46 5.5 24 3 gpn 5.4 53 6.6 8
6 gpn 5.4 53 6.3 14 12 gpn 5.4 53 5.7 16 Based upon these results, design work was begun on an addition *w the existing equipnent which would allow a reduced flow ra'a through the charcoal vessels without sacrificing the overall system flow rate.
We initial conception was a header which would divert a portion of the flow through a dual-train of charcoal vessels.
- h Wese were to be throttled at 10 gpn per train. l
__. (
1 Ihe filtration system was shutdown and disassembled on khrch 31.
ejf 1 This was in onier to move the system from the cask decon pit to allow renovRl and decontamination of the Superstand from the SFP.
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,j fIII. OPERATIONS AND g!EMISTRY WITH THE RECONFIGURED SYSTEM
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/d Tne. Oiem-Nuclear technicians returned to Fort Otlhoun on April 13 and began re-assembling the filtration systen the following day.
'Ihe system
/ was, initially set-up to be identical with the system shown in Figure 2.
The particle size analysis had identified sub-micron particles, so a stainless steel vessel with removable cartridges was purchased.
'Ihe L. '
cartridges chosen for use with this vessel wre conposed of inert poly-
/, >, i olefin fjbers in a plen.ted design capable of filtration drwn to 0.2 4
micron.
j A system for injecting a coagulant was also identified and design work begun. 'lhis coagulant was a polycationic polymer used to neutralize the negative charge on colloidal turbidity particles.
'Ihe initial rapid mixing of the coagulant with th'e SFP water was accomplished by injection
- on the suction side of the feed punp. 'lhe coagulant then neutralizes the surface charge of the particles.
'lhis allows collisions between the particles and removal through in-line filtration.
(A)
Week Ending April 17, 1982 The filtration equipnent was set-up on April 14 and pressure tested.
A visual observation by the CNSI lead Technician showed the pool was more turbid than when the system was shutdown.
'Ib r-bidity measurements were not made until a day af ter start-up and these showed no change.
Figure 5 shows turbidity measurements in
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NTU over the course of the job.
7 Filtration was restinal on April 15 at a flow rate of 50 gpn.
(B)
Week Ending April 24, 1982
~ The pressure vessel containing the 0.2 micron cartridge filters was installed on April 19.
It was positioned downstream of the char-coal beds af ter the dual trains had been recombined.
Initial differential pressure was 3 psi.
The poolside tests with binn and IRA-938 resin were run on April 16.
'lhe resin reduced the turbidity to 0.22 NTU.
'1his resin was being utilized by GSI for ranoval of colloidal particles at other utilities.
Fabrication of the charcoal header system was begun. 'lhe configur-7
'.rV ation was a 6-point header that would allow the complete flow of the filtration systen to pass through six parallel charcoal beds.
The average flow rate through each vessel would be 10 to 12 gpn.
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i (C) Week Eading May 1, 1982 Differential pressure on the 0.2 micron filter increased throughout the first week it was in service.
By April 27, the flow through the system was being limited by the differential pressure.
Recir -
culation was secured and the cartridges replaced.
(D) Week Ending May 6, 1982 On May 3, the charcoal system headers and coagulant injection system arrived at Fort Calhoun.
Included were two pressure vessels loaded with strong base anion resin.
The anion vessels were to be installed as the last vessel of the system to remove any phosphate, sulfate, or chloride ions. The recirculation was secured on thy 3 and the new system installed.
(E) Week Ending May 13, 1982 The recirculation system, in its new configuration, was returned to service on May 10.
The system diagram is shown in Figure 3.
The coagulant was injected via a metering pump on the feed pump suction.
A 1% solution of the coagulant in DI water was injected at a rate of 4 ml/ minute + 0.5 m).
The turbidity of the influent on May 10 was 4.9 NTU.
The effluent turbidity, using the coagulant inj ec tion system, was 0.2 NTU.
Individual samples showed the majority of the particles were removed on the 1 micron vessel.
This removal rate continued throughout the remainder of the project.
(F) Weeks Ending May 20 c.nd 27, 1982 Processing continued utilizing the coagulant injection system. The terbidity gradually decreased throughout this period.
By bby 27, the SFP turbidity was measured at approximately 0.6 NTU.
At this point, the fuel racks were visible without underwater lighting.
The filtration system suction and discharge was moved to the transfer canal on May 29.
A submersible, air-driven pump was installed on the suction line as a booster pump.
Recirculation of the transfer canal was begun.
The process was completed on May 28 and the transfer canal water was discharged to the SFP.
The system was secured and returned to the SFP.
Prior to startup, four of the charcoal vessels were removed and replacements installed.
Final recirculation of the SFP was begun.
On June 5, the recirculation system was secured and disassembly begun. The final chemistry profile of the pool was:
pH:
5.7 Conductivity
42 pmho Chlorides:
0.02 ppm Phosphates:
2.2 ppm Boren:
2209 ppm Turbidity:
0.6 NTU APPENDIX 1 Chronological Sunmtry
.)
February 15:
Gem-Nuclear technicians and supervisor on-site for badge training.
Feburary 17:
System assembled and vessels pre-filled.
February 19:
DI water flush of 1300 gallon complete.
February 20:
"B" Train start-up - 40 gpn.
February 21:
Suction hose lowered to 9 foot level.
February 22:
Suction hose lowered to 12 foot level.
February 23:
Conmenced processing 16 hours1.851852e-4 days <br />0.00444 hours <br />2.645503e-5 weeks <br />6.088e-6 months <br /> / day.
February 25:
Shielding installed on charcoal vessels.
February 27:
Conmenced processing 24 hours2.777778e-4 days <br />0.00667 hours <br />3.968254e-5 weeks <br />9.132e-6 months <br /> / day.
March 2:
Suction hose lowered to 35 foot level.
hhmh5:
manged charcoal beds based on turbidity measuronents.
Suction hose at 30 foot level.
3 March 12:
Acid washed charcoal vessels (with 1 ft3 mixed bed msin "1
in each) installed. One micron cartridge filters installed downstream of ten micron filters.
hitmh 17:
low flow test conducted. Suction hose lowered to 40 foot level.
httrch 22:
Feed ptrnp bearing failed.
March 24:
New punp returned due to seal leak.
Shmh 26:
Gem-Nuclear mechanic and new ptrnp head sent to Fort Otlhoun. Filtering restrned.
httrch 30:
Low flow test repeated.
March 31:
System shutdoun and disassembled to allow removal of Superstand.
April 13:
Ocm-Nuclear technicians ;eturned to Fort Otlhoun.
April 14:
Equipnent set-up begins. SFP is more turbid than when system was shutdown.
April 15:
Filtering restmed.
r. _
April 19:
0.2 micron filter installed downstream of last two charcoal bcds.
]
April 21:
Pbolside tests with binn and Hohm & Haas resin.
April 27:
Ganged cartridges on 0.2 micron filter due to high differ-ential pressure.
May 3:
New system on-site. Filtering shutdown to reconfigure sys-tem.
Instructed by OPPD to re-install the first four char-coal beds used.
May 10:
Syston returned to service with coagulant addition system and 6-train charcoal systen with one anion vessel installed on effluent.
May ll:
Oom-Nuclear on-site staff increases to three due 'a ex-posure.
Qmnenced 24 hour2.777778e-4 days <br />0.00667 hours <br />3.968254e-5 weeks <br />9.132e-6 months <br /> / day operations.
May 27:
Begin processing water in transfer canal.
hhy 28:
Transfer canal complete and discharged to SFP.
Installed four new charcoal txxis. Begin final recirculating of SFP.
June 5:
Filtering conplete, systen shutdown.
Begin disassembly of system and preparing vessels for disposal.
June 24:
All pressure vessels prepared for disposal.
)
June 28:
CNSI equipnent and technicians leave Fort Glhoun.
APPENDIX 2 Weekly Volume Sumtry Week Ending A Train B Train Combined Total 2-20-82 8,300 8,300 2-27-82 135,425 134,075 269,500 3-06-82 159,250 182,415 341,665 3-13-82 159,605 256,475 416,080 3-20-82 140,400 221,175 361,575 3-27-32 71,000 106,500 177,500 4-01-82 75,700 122,400 198,100 4-10-82 NO IROCESSING - SUPERSTAND REMOVAL 4-17-82 59,500 89,250 148,750 4-24-82 179,100 268,650 447,750 5-01-82 175,490 259,665 435,155 5-08-82 32,100 48,150 80,250 i
5-15-82 130,795 131,080 261,875 5-22-82 163,400 163,400 326,800 5-29-82 120,870 118,950 239,820 6-05-82 79,000 71,100 150,100 4
TOTAL 1,681,635 2,181,585 3,863,220 I
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APPENDIX 3 Chemistrv Summary 3
The following surrnary is based upon chemistry data obtained by Oxnbustion Engineering and Onaha Public lbwer District as reported to 01cm-Nuclear Systems, Inc.
1.
OPPD Poolside Filter Tests Date Halliburton Filter Test 12/2/81 Sufficient water passed through filter to show it vould not plug.
Olem-Nuclear Filter Test 12/7/81 Sufficient water pssed thruugh (1 micrun filter) filter to show it would not plug.
Test Amberlite IRA-93d Resin Glycol Out Turb.
Oond. pH (PP)
(MU) 3/25/82 58 0.15 50 5.8 4/16/82 70 0.22 81 5.9 Birm Capacity Test 4/16/82 (Milky Reagents) 0.5 610 6.9 2.
OPPD Measurements (a) Total Suspended Solids Profile (mg/ liter)
November March 2 March 10 March 16 Surf.
15 2
5.6 2.8 10 6-9 2
6.6 20 6-9 3
5.8 4.0 30 6-9 67*
- 5. 2 40 6-9 3
6.2 4.8
% e Fungus Organisn In Sample (b) Particle Size Profile (microns)
Obasure 5 Particles At Random) l March 2 March 10 March 16 Surf.
15.3 + S 21.4 9.8 10 11.6 + 10 16 20 27.5 + 8.6 7.8 9.2 30 39.2 + 30 10.8 40 35 + 12 17 18,
(c) Glycol Concentration Profile (ppn)
Febntary 23 February 25 March 2 Surf.
47 32 30
]
10 43 35 33 20 45 57 36 30 42 49 32 40 42 31 (d) Glycol Decomposition Test (ppn)
Sample Drawn And Analyzed Oi Mamh 19:
42 ppm Sample He-analyzed On April 19:
70 ppn (e) Glycol (ppn)
Pat Inlet 01tlet Inlet Position A B February 20 170 25 February 21 225
- 210 5 Feet February 22 152 63,202 9 Feet Febrtnry 24 82 62, 56 12 Feet February 26 40 29, 31 12 Feet February 27 52 28, 60 12 Feet February 28 40 48, 52 12 Feet March 1 42 62, 68 12 Feet hurrh 2 31 29, 30 35 Feet New Olaroal Vessel (3/S)
)
hurch 6 44 40, 47 30 Feet March 7 48 47, 48 30 Feet hhrch 8 42 40, 42 30 Feet March 9 38 25, 20 30 Feet 1 Micron Filter (3/12) hhrch 15 45 56, 53 35 Feet March 19 42 40, 37 40 Feet hurch 30 24 18, 12 40 Feet April 16 48 56, 51 35 Feet 0.2 Micron Filter (4/20)
April 20 32 35 Feet May 10 42 32, -
S-Train System (5/10)
Ahy 20 28 28, 22 New Q1arcoal Vessel (5/28) hhy 28 38 8, -
June 3 30 40, -
) _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _
(f) Turbidity (NTU Units)
Inlet Outlet A B
}
February 20 2.0 1.0 February 21 2.5 1.3 February 22 2.6 1.8,1.8 February 23 3.2 2.5,2.5 February 24 3.7 3.5,3.2 February 26 5.1 4.4,4.3 February 27 5.3 4.8,4.7 February 28 5.8 5.4,5.2 hurrh 1 6.3 7.4,6.5 March 2*
- 6.8 6.2,6.3
-New Q1arcoa.1 Vessels (3/5)
March 6 7.2
- 4.5,6.2 March 7 6.9 6.4,6.3 kurch 8 6.7 6.4,6.3 March 9 6.6 6.5,6.2 hhrch 10 6.4,6.1 March 13 7.2 8.3,7.7 1 Micron Filter (3/12)
March 15 7.2
- 7. 7 hurch 19 6.8 6.6 March 30 5.5 5.2 April 16 5.2 5.2,5.1 April 20 5.2
, 5.1 0.2 Micron Filter (4/20)
)
Gagulant Systan (5/10)
May 11 5.3 0.2 Shy 12 4.5 0.1 May 13 3.9 0.1 hhy 14 35 0.1 May 15 3.5 0.2 nhy 16 2.8 0.1 May 17 2.2 0.2 Ahy 18 2.3 0.4 l
May 19 2.0 0.3 l
hhy 20 1.8 0.1 June 2 0.9 0.2 i
- Effluent Through A New Garcoal Vessel At 8 GBt (g) Inw Flcw Rate Through Charcoal Glycol In Glycol In Glycol Removal Flow Influent (ppm)
Effluent (ppm)
Rate (Gal /Dav) 3 gpn 24 8
.07 i
6 gpn 24 14
.09 12 gtm 24 16
.14
)
l. _
-~
(h) Qlorides In RIol (ppb)
November 22, 1981 300 March 5, 1982 Ialet 50 Outlet Irss han 5 Anion Vessel Installed (5/10) 130 Mty 12 May 13 140 Miy 14 60 May 16 50 Mty 17 30 May 18 10 shy 19 10 June 2 20 (i) Transuranic Analysis (Eberline Hesults On February Ibol Sample)
(Picoeuries/ Liter)
Np-237 2+_
9 Am-241 100 + 300
~
Am-243 2
9
~
Pu-236 4
20 Pu-238 90 + 20 Pu-239 + Pu-240 40 + 10 Pu-242 Less 'Ihan 1 3.
C-E Analysis (a) Glycol (PPM) (Measures Only Ethylene Glycol) o February sample contains no measurable concentration of glycol (less than 1 ppn).
o hhrch 12 sample also contains no glycol (less than 1 prm).
o Transfer canal water contains less than 1 ppn.
(b) Turbidity (JTU Units)
OPPD Sample OPPD OPPD April 1 AP&L BG&E Drawn Date Feb. 20 Mar. 12
?
Feb. hhrch Depth
?
40 ft.
(Trans. Gnal)
?
?
As Received-3.4 6.0 1.7 0.5 0.16 0.8 Micron Filter 2.4 4.2 0.82 0.4 0.65 Micron Filter 4.8 0.22 hiicron Filter 1.5 2.4 0.84 0.2 Tap Water 1.9 DI Water 0.2 o 'Ibrbidity Test Following Filtering 'Ihrough Anberlite IRA-938 Resin As Heceived - 3.4 JTU Filtered 'lhrough.8 Micrun Filter - 2.4 JTU Filtered 'Ihrough Hesin - 0.16 JTU
)
(Pre Borating Hesin Does Not Affect Hesult)
(
(c)
Impurity Concentrations (PP1)
(minus indicates less than)
Ion Wet Dtte Depth Atonic Absorption Granotography O cnistry
]
Pool Drawn (ft)
Fe Ni Cr Mt Li K
SO4 NO3 101 C1 AP&L Feb.
.01
.02
.01.52
.13
.47
.22
. 61 IkisE khrch
.1
.1
.1
.3
.05
.05 OPPD hild-Feb.
1.4
.12
.01.15
.35
.07
.69 0.0
-1.0
.44 OPPD hhrch 12 40 2.5
.1
.05.3
.01
.02 14.5 OPPD hhrch 12 30 1.95 0.15
.05.29
.01
.02
.40 OPPD hhrch 12 20 2.0 0.05
.05.3
.01
.02 14.5 OPPD hhrch 12 10 2.0 0.2
.1
.29
.01
.02 14.5 4
OPPD hhrch 12 Surf 2.05
.01
.05.3
.01
.02 14.5
.30 NPPD April 1 0.62 0.22 -0.1
.46
.2
.58
-1.0
- Transfer Gnal Water 1
(d) Particle Size, Iron, Turbidity Test hhrch 12 Sample (Influent Turbidity = 0.0 JTU)
Filter Size Turbidity (JTU)
(Micron)
PBf Iron Of Effluent J
- 0. 8
- 2. 5 5.1 0.65 1.8 5.0 0.2
- 1. 7
- 2. 8 4
i 5
i
't i
(
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4 I N a t 1 A t.
d i d t r.M o t nu nart FIGURE I as-g
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4
FIGURE 2 SECOND SYSTEM DIAGRAM l
7 e
se<.,,m os-i (es.ur a)p.,P'n5ML th.
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s** utL os.es MV4-t>
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s * %+d I 3E h3 un fac. 3 p PIA. O s.:
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To SFA
{._
r s i. o n i, a FINAL S Y S'I DI DIAGRAM hiso PSl4 syy7 d
poet..
COAQULAN[
-D4-k TO SPENT FloccvLANT FUEL Poot '
M X
x x
x x
x 2
4 2
OW
+40 l
l
}>
l l
O I
W Y/
V T/
T/
V g
5 MICRold A
v FILTER BEDS V
g 4
q l
N N
a
_ i MICRoM a
V FILTER GED$
O rPI
_ y M_
SERilCE
.2 MICRON g
WATER FILTER BED gvf
}<
V i
c n
o
.[;ii.
L\\
t r
I N
U5 J
Y A9 I
2 F
Y A2 M2 Y
, A5 M1 Y
- A8 YA1
, M l
i p1 A2 E
M I
R T
p7 A1 S
V t
N t
p0 4
O i A1 I
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k A
'l i
n t
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p3 l
F E
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i 1
0 R
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A7 T
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A0 M2 R
A3 M1 t
l
- A6 M
i l
- E7 P2 l
l I
0 F2 5
0 0
0 7
5 0
5 1
1 1
AoUsAg
- ,FaC l
ei 1.
4:
- i !;
- i J;1 lii14'
'l t
b
.i,I
- lI1
- 3:1! -
l
,j
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t
i i
FIGUKE 3 1
TURBIDITY VS TIME t
i 10 t
9
.i l
g.
1 7..
1 j
6 t
@ >8 i
5 l
H (n
O H Z D.
cc s E in 1
D 4
j b
t l
1 3
i i
i 2
i 1
1 e
4 FEB ITB RTR MTR RTR RTR APR APR APR APR MTY MW MTY RTY MW JUNE' i
20 27 6
13 20 27 3
10 17 24 1
8 15 22 29 5