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US 8,128,735B1 78 As the input gas stream 102 passes through the bed of Zeolitesorbent104,C02 isadsorbedandaCO2 frontformsin theZeolitesorbentbedandtravelsthroughthebed,generating loadedZeolitesorbentcontainingatleastadsorbedCO2. Exo ther'micheatgeneratedbyC02 adsorptionontheZeolitebed isremovedfromthecapturevesselWitha?rstheattransfer0 1 to substantially maintain conditions at the ?rst temperature during the adsorption. A substantially CO2-depleted gas stream 105 may be draWn from the capture vessel. In a particular embodiment, input gas stream 104 is further comprised of H20, such that the Zeolite sorbent further adsorbsH20 andtheCO2-depletedgasstream105isfurther depletedofH20.Inanotherparticularembodiment,theCO2 depleted gas stream 105 poWers an Integrated Gasi?cation CombinedCycle. FirstheattransferQ 1may beaccomplishedusingavariety of heat sink means knoWn in the art. For example, the heat sink could be a coolant ?uid in a heat exchanger, another process technology requiring heat at about or less than the temperatureofadsorption,orsimplytheatmosphere.Non 20 sorbed components of the gas that contacts the adsorbing mediamay alsoremove some exothermicheatduringadsorp tion. In a particular embodiment, ?rst heat transfer Q l is accomplishedWithaheatexchangerusingWaterasacoolant ?uid. 25 In a further embodiment, process gas stream 101 has a temperatureexceedingthe?rsttemperature,andiscooledby heat transfer Q4, so that input gas stream 102 enters capture vessel 103 at a temperature beloW that of process gas stream 101.Inanexemplaryapplication,processgasstream101isa 30 shiftedsyngasstreamproducedinaWGSreactoratan approximatetemperatureof2500C.andthe?rsttemperature in capture vessel 103 is 120-1500 C., and heat transfer Q4 is utiliZed to remove heat such that input gas stream 104 enters capturevessel103Withintheapproximatetemperaturerange 35 120-1500 C. Heat transfer Q4 may be accomplished using a varietyofheatsinkmeans knoWn intheart,suchasacoolant ?uidinaheatexchanger,anotherprocesstechnologyrequir ingheatataboutorlessthanthetemperatureofadsorption,or simplytheatmosphere.Inaparticularembodiment,heat40 transfer Q4 is accomplished With a heat exchanger using a medium in communication With other heat exchangers uti liZed in the method, so that at least some portion of heat transferQ4 may beutiliZedelseWhereintheprocess,asdis cussedinfra. The input gas stream 102 and the Zeolite sorbent 104 are contactedinthecapturevessel103atthe?rsttemperatureand the ?rst CO2 pressure for a ?xed period of time Which is suf?ciently short in duration so as to prevent the break throughofcarbondioxideinCO2-depletedgasstream105.50 ThequantityofCO2 inCO2-depletedgasstream105Which designatesbreak-throughisnotspeci?edWithinthismethod and may be determined by an operator. FolloWingbreak-through,theZeolitesorbentisreferredto asloadedZeolitesorbentWithinthismethod.Regenerationof55 theloadedZeolitesorbentisdiscussedWithreferencetoFIG. 1B. At FIG. 1B, regeneration vessel 106 holds loaded Zeolite sorbent 107. Within regeneration vessel 106, loaded Zeolite sorbent107issurroundedbyaC02 atmospherecomprisedof atleast90mol%CO2atasecondCO2pressure,Wherethe60 secondCO2 pressureisgreaterthanthe?rstCO2 pressure.A second heat transfer Q2 increases the temperature of loaded Zeolitesorbent107toasecondtemperature,Wherethesecond temperatureisgreaterthanthe?rsttemperature.As aresultof theincreaseintemperature,loadedZeolitesorbent107des 65 orbssomeportionoftheCO2 adsorbedatthe?rsttempera ture.ThedesorbedCO2 enterstheCO2 atmosphereinregen erationvessel106atthesecondCO2 pressure,andoutputgas stream108isgeneratedbydraWingsomeportionoftheCO2 atmosphereandthedesorbedCO2 fromregenerationvessel 106.Outputgasstream108therebymaintainsahighpurityof CO2 andisproducedataC02 pressureexceedingthe?rst CO2 pressureofinputgasstream102. The regeneration of loaded Zeolite sorbent 107 in a high CO2 pressure atmosphere is a novel aspect of the method disclosed herein, and facilitates a high purity and high CO2 pressure foroutput gas stream 108. This isinmarked contrast to standard temperature-swing adsorption processes, Which often produce a diluted product stream through the use of a hot,inertregenerationgasinordertoprovideahightempera ture,loWCO2pressureenvironmentfordesorption.Similarly, this is in marked contrast to typical pressure-sWing adsorp tion processes, Which by necessity result in a product stream havingaloWerCO2 pressurethantheinputgasstream.Within the novel method disclosed here, regeneration in an environ mentofincreasedCO2pressurealloWsfortheproductionof ahighpressure,highpurityCO2 streamWithoutthenecessity forfurtherseparationoperationsorsubsequentcompression, greatly aiding subsequent storage and sequestration opera tions. The second temperature and the second CO2 pressure are representative of an adsorption condition de?ned by an adsorptionisothermofZeolitesorbent107re?ectingadsorp tionofgaseousCO2 and,asspeci?edsupra,exceedthe?rst temperatureandthe?rstCO2pressurerespectively.Similarto the?rsttemperatureandthe?rstCO2 pressurediscussed supra,thesecondtemperatureandthesecondCO2 pressure may be mean values around Which slight variation occurs as aresultofoperationalconstraints.Theacceptablemagnitude of variation of the second temperature and the second CO2 pressureisnotalimitingvalue,exceptthatthemagnitudeof variationshouldbecontrolledsuchthattheloWestmagnitude of the second temperature exceeds the highest value of the ?rsttemperature,andsuchthattheloWestvalueofthesecond CO2 pressureexceedsthehighestvalueofthe?rstCO2 pres sure,sothatadsorptionincapturevessel103anddesorption inregenerationvessel106canbeexpectedtooccurWithinthe potential ranges of the ?rst temperature and the second tem perature, and an output gas stream can be produced at a secondCO2 pressureexceedingthe?rstCO2 pressure.Thus, Whenthemethodspeci?esmaintainingasecondtemperature orasecondCO2 pressure,itisunderstoodthatthisisintended to indicate maintaining these parameters Within the accept ablemagnitude ofvariationaboutthemean value. In a particular embodiment, loaded Zeolite sorbent 107 is Zeolite13XWithadsorbedCO2andH20,andthesecond temperature is at least 2750 C., so that loaded Zeolite sorbent 107desorbsbothCO2 andsubstantiallyalH2O inregenera tion vessel 106. In another embodiment, Where the loaded Zeolite sorbent 107 is Zeolite 13X and the input gas stream 102isshiftedsyngascomprisedofCO2andH20,asecond temperatureof2750C.-380oC.andasecondCO2 pressureof approximately 209-297 psig is utilized for desorption in regenerationvessel106,folloWingadsorptionincaptureves sel 103 under a ?rst temperature of 1200 C.-180o C. and a ?rst CO2pressureinaccordanceWithatotalpressurebetWeen 230-330psigandtheCO2mol% ininputgasstream102.In thelatterembodiment,theZeolite13XCO2capturecapacities are approximately 3.0 mol/kg sorbent in the capture vessel and 0.01 mol/kg in the regeneration vessel. The loW CO2 capturecapacityunderthesecondtemperatureandinan atmosphereof90mol% gaseousCO2alloWsregenerationat ahighsecondCO2 pressure. 45PDF Image | PROCESS FOR CO2 CAPTURE USING ZEOLITES
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