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EN <br /> 25 March 1991 <br /> Page 4 <br /> Clint Rogers <br /> Chevron U.S.A. Inc. <br /> 1 i iz r r *i m D S cti n Bffici nc <br /> led for the SJCAPCD on 16 <br /> rc crit Table <br /> Initial destruction efficiencies for the <br /> c catalytic', <br /> . diat that time were 9P�o 96 D bar(EA, <br /> November. The destruction of given b the SJCA <br /> 3). Permission to Of the catalytic oxidizer was gi Y <br /> ROC). By 2$December the combined vino.oConcentration rthe thermal oxidizer as sV5, and hut dawn <br /> declined and stabilized at about 1,100 pp <br /> ction efficienciec <br /> in order to convert the treatment system �December were to catalytic Operation. <br /> 7.771.7,and 58.3 e�st sent ystem ), <br /> 3etetmined far the catalytic oxidizerPossible catalyst problems. <br /> well below the 95 percent efficiency required. It was decided s shut the <br /> Problems- <br /> order to start the first re-equilibration Period and to investigate reg p problem the of low destruction <br /> the Te their <br /> period,KBA was cuntac Wes hereason. On 21 January the catalytic <br /> During admitting dilution air. <br /> efficiency. It was their opinion that a lack of oxyg <br /> oxidizer was brought on line again. Oxygen content was increased by r The g <br /> in amounts of dilution <br /> content oftof <br /> the <br /> ai <br /> Destruction efficiencies were determined for varyingIn late combustion of the <br /> dilution air had no effect and tto be 18.1 percent,suffidestruction cient to addition,Pp t Completions had increased <br /> extracted soil vapor' fou <br /> extracted vapors with no added dilution air. Be ors w�e vapor <br /> To°red to the thermal oxidizer: <br /> during the re-equilibration period,the extracted vapors <br /> that the catalyst bed should be opera <br /> at he elevated <br /> Daring the next week,all operating dand concentration measurements for haeted at tic oxidizer <br /> were faxed to KBA and it was suggested <br /> temp crated at an elevated temperature of 950 F. Duringab s <br /> temperature(950-1,000 F)to back any high-boiling residue off theca catalyst <br /> On 28 January the catalytic oxidizer was Operated 6$4, and 78.5 percent Fere determined.( don <br /> time successive destruction efficiencies of 65.8, the runBecause <br /> 3), Because the destruction efficiencyinda was <br /> inct were 82.4$0 0yand 76.5 spercnt(Tale the catalytic <br /> efficiencies determined the following Y <br /> extracted vapor concentrations had again decreased and the destruction efficiency <br /> oxidizer was below 95 percent,the vapor extraction and treatment system was shut dawn again for <br /> a second re-equilibration period. <br /> Because no prog ld be installed and that the possibility that the catalyst was <br /> rets could be made in t7storing the efficiency of the existing catalyst bed,it was <br /> decided that a new catalyst bed thou <br /> hydrocarbons should be investigated.: On 8 March <br /> poisoned by either tetraethyl lead or chlorinated by <br /> d h dracdono s. Analytical results were ui the <br /> new catalyst bed was installed and sa�mp�eaa�f Y traction well vapors were�oioleciedj or the <br /> a l lead and chlorinated <br /> determination of tetraethyl st bed showed a distinct discoloration (bronze, gray) <br /> March: Inspection of the catalyst <br /> surface of the catalyst on the inlet side. catalytic ravided that ria <br /> eration of the VFTS will be resumed os a2.re found byarch ithe danalysie s of the well vapors- <br /> tetraethyl I lead or chlorinated hydrocarbon <br /> teuaethy <br /> ti n i R iu of th Va r Ex coon S stem <br /> he o erational radius of influence of the vapor extraction system has been estimated using <br /> T P <br /> - _equation_1,.---- <br />