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1000 TPD CO 2 CAPTURE PLANT FEED STUDYDEVON JACKFISH 1 OILSANDS OPERATIONSFEED STUDY REPORTDEV-JA-03-001-1 (R1)The regenerated lean amine solution is removed from the Stripper bottom and passes through theLean/Rich Heat Exchanger and is cooled against the rich amine stream going to the Stripper. The leanamine solution is then sent back to the CO 2 Absorber Column via an air cooled Lean Solvent Cooler,which provides control of the temperature of the lean solvent.In the CO 2 absorption/stripping process, the base amine components in the solvent react with O 2 andother gases such as NO 2 , SO 2 and SO 3 in the flue gas to form “complex” heat stable salts that cannot bethermally regenerated. In addition, some organic degradation products can be formed through sidereactions between flue gas impurities, the amine solvent and/or the heat stable salts.Heat stable salts and degradation products, if allowed to accumulate in the solvent, will decrease thesolvent CO 2 capture efficiency. Therefore, a slip stream of lean amine solvent leaving the Stripperbottom is sent to a Reclaimer to remove degradation compounds and recover amine from the heatstable salts. Fuel gas is used to provide the necessary heat required to maintain the Reclaimer operatingtemperature. Evaporated solvent vapour is condensed by an air cooled heat exchanger and therecovered solvent is pumped back to the Amine Surge Tank. The Reclaimer waste stream, containing theheat stable salts, degradation products, as well as a small amount of unrecovered solvent, leaves thecapture plant battery limit for waste processing and/or incineration by a commercial wastemanagement company.3.3 KEY PERFORMANCE INDICATORSTable 5 presents a summary of the process simulation results for the plant inlet and outlet streams.Table 5- Process Design ConditionsParameterUnitGas Feed Gas FeedOff Gas(From OTSG (at Absorber(Treated)Exhaust) Inlet)CO2 ProductFlow Rate SCMH 2.891E+05 2.557E+05 2.361E+05 23,200Temperatureo C 182 35 36 35Pressure kPa (g) 0.2 4.4 0.2 68.5N 2 %mol 71.6 81.0 87.7 < 50 ppmvAr %mol 0.87 0.99 1.05 tracesCO 2 %mol 8.62 9.74 1.05 96.7O 2 %mol 2.6 2.94 3.18 < 10 ppmvH 2 O %mol 16.3 5.35 6.99 3.35Figure 2 shows the mass flow rate and enthalpy of each stream entering and exiting battery limit andprovides overall heat and mass balance for CO 2 capture plant as designed.HTC PURENERGYPage11 (19)
1000 TPD CO 2 CAPTURE PLANT FEED STUDYDEVON JACKFISH 1 OILSANDS OPERATIONSFEED STUDY REPORTDEV-JA-03-001-1 (R1)Off GastoAtmosphere276,900 kg/hr11,499 J/kg36 o C0.2 kPa (g)Battery limit for CO 2 Capture PlantBattery limit between DEVON and HTCCO 2 Capture PlantFlue gasOnce-Through SteamGenerator (OTSG)DEVON Jackfish 1ProductionFacilities342 ,000 kg/hr173,500 J/kg182 o C0.2 kPa (g)Flue GasBlowerFlue GasCoolerAbsorberwith WashSectionSolvent SurgeTankIntermittentSolvent MakeupSolvent StorageTankL/R HeatExchangerReclaimer(IntermittentOperation)Stripper &CondenserReboiler(129 .75 GJ/hr)42,331 kg/hr7,040 J/kg35 o C68.5 kPa (g)CO 2Compression& DehydrationCO 2 sendout pipelineElectrical Power Supply= 2575 kWSolventInstrument airTotal Cooling Duty= 230 GJ/hrFuel GasExhaust gas toAtmosphereExcess WaterResidue toDisposal22,745 kg/hr-2,403,000 J/kg35 o C349 kPa (g)Intermittent StreamFigure 2 - Heat and Mass Balance over battery limitHTC PURENERGYPage12 (19)
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