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US 8,128,735B1 9 10 SecondheattransferQ2 isappliedindirectlytotheadsor bentmaterialthroughaheatingcoil,electricalheatsource,a heat exchanger in intimate association With the adsorbent material, or other heat source means knoWn in the art. In a particularembodiment, secondheattransfer02 isaccom plished With a heat exchanger using some portion the steam generatedbyanIGCC plantpoWeredbyatleastaportionof 002-depleted gas stream 105. In a particular embodiment, output gas stream 108 is indi rectly cooled to a third temperature beloW the second tem peraturebyheatexchanger119,andatotalpressureofatleast thesecondCO2 pressureismaintainedbybackpressureregu latingmeans 120,inordertoproduce?nalCO2 stream110.In an application Where the output gas stream 108 encounters back pressure regulating means 120 Without substantial change in the output gas stream 108 composition, the total pressuremaintainedby backpressureregulatingmeans 120 is thesecondCO2 pressure.Thereductionintemperaturetothe third temperature is particularly advantageous When further compressionof?nalCO2stream110outsidethemethod20 disclosedhereinisdesired,andtheloWerthirdtemperatureof the?nalCO2 streamservestoreducesubsequentcompressor Work required. In such applications, output gas stream 108 may be indirectly cooled to the third temperature using a varietyofheatsinkmeansknoWnintheart.Forexample,the 25 heat sink could be a coolant ?uid in a heat exchanger, another process technology requiring heat at about or less than the temperature of adsorption, or simply the atmosphere. In a particular embodiment, output gas stream 108 is indirectly cooledWithaheatexchangerusingWaterasacoolant?uid. 30 Similarly,backpressureregulatingmeans 120may bevariety ofpressureregulatingdevicesknoWnintheart.Forexample, back pressure regulating means 120 may be a back pressure regulatorvalve. Inaparticularembodiment,Whereinputgasstream102is 35 furthercomprisedofH20 andoutputgasstream108contains H2O, moisture removing means 111 may be employed fol loWingheatexchanger119 inordertoremove someportionof theH20 atthethirdtemperature,suchthat?nalCO2 stream 110hasareducedmoisturecontentascomparedtooutputgas 40 stream108.Inaparticularembodiment,thethirdtemperature isbeloWthesaturationtemperatureforH2O inoutputgas stream108,andtheH20 isremovedasacondensateusing screens or other tortuous ?oW paths in moisture removing means 111 asisknoWn intheart. Inafurtherembodiment,theCO2 atmosphereinregenera tionvessel 106 isprovidedby regeneration stream 109, com prised of a portion of output gas stream 108 as indicated at FIG.1B.WhentheCO2 atmosphereisprovidedbyregenera tionstream109,backpressureregulatingmeans120servesto 50 maintain regeneration stream 109 at the total pressure of output gas stream 108, and regeneration stream 109 isheated by a heat transfer Q3 to match or approach the second tem peratureconditioninregenerationvessel106.Inaparticular embodiment,theheattransferQ3isaccomplishedWithaheat55 exchangerusingamedium incommunicationWithotherheat exchangers utilized in the method, so that at least some por tion of heat transfer Q3 may be comprised of heat removed elseWhere in the process, as discussed infra. Additionally, Wheninputgasstream102isfurthercomprisedofH20and 60 outputgasstream108containsH2O,regenerationstream109 folloWs moisture removing means 111 to reduce the moisture content of regeneration stream 109. Regenerationisgenerallyconductedinregenerationvessel 106fora?xedperiodoftimeWhichissu?icientlylongin 65 durationtodesorbsubstantiallyalCO2 andH20 Whenappli cable from the loaded Zeolite sorbent, hoWever the ?xed period of time for regeneration is not speci?ed Within this method and may be determined by an operator using various indications knoWn to those skilled in the art. For example, comparison of ?oW rates betWeen output gas stream 108 or ?nal CO2 stream 110 and regeneration stream 109 may be utiliZed as an indication of regeneration completion, or the ?xed period of time may be speci?ed based on past experi ence With the system, orusing othermethodologies knoWn to those skilled in the art. Following regeneration, the Zeolite sorbent is referred to as unloaded Zeolite sorbent Within this method. Regenerationinthemannerprovidedthusprovidesahigh purity product stream of CO2 having a higher CO2 pressure than input gas stream 102 and having a total pressure com miserateWithorgreaterthanthe?rstCO2 pressureofinput gas stream 102. Additionally, in a particular embodiment, ?nalCO2 stream110may beproducedatathirdtemperature beloW the ?rst temperature, greatly reducing subsequent compressionburdensifdesired.Inanexemplaryembodiment Where input gas stream 102 is shifted syngas comprised of CO2 andH20 andadsorptionoccursundera?rsttemperature of150°C.anda?rstCO2 pressureofapproximately 109psig (re?ectingatotalpressureof280psigandCO2 contentof39 mol%),folloWedbyregenerationatasecondtemperatureof 350°C.andasecondCO2 pressureofapproximately252psig (re?ectingaC02 atmospheretotalpressureof280psigata C02 contentofatleast90mol%),a?nalCO2 stream110With apurityof98mol% CO2andhavingatotalpressureof280 psigatatemperatureof76°C.maybeproduced.Thepro ductionofthishighpressure,highpurityCO2 streamWithout thenecessityforfurtherseparationoperationsorsubsequent compressionisbasedonregenerationinaC02 atmosphereof atleast90mol% CO2,andisanovelaspectofthisdisclosure. Itisunderstood thatWhile capture vessel 103 atFIG. 1A and regeneration vessel 106 at FIG. 1B have been discussed asseparateanddistinctentitiesintheforegoingexplanation, capture vessel 103 and regeneration vessel 106 may be a singlevesselcapableofprovidingboththeadsorptionand regenerationconditionsdiscussed.Additionally,itisunder stood that When capture vessel 103 and regeneration vessel 106 are separate vessels, the sorbent may be transferred betWeencapturevessel103andregenerationvessel106,such that loaded Zeolite sorbent is transferred from capture vessel 103 to regeneration vessel 106, and unloaded Zeolite sorbent is transferred from regeneration vessel 106 to capture vessel 103. The unloaded Zeolite sorbent may be cooled during the transfer from regeneration vessel 106 such that the unloaded Zeolite sorbent may serve as Zeolite sorbent 104 in capture vessel103. FIG.2illustratesaprocess?oW diagramdemonstratingthe methodoperatedinasubstantiallycontinuousmodeutiliZing separatecaptureandregenerationreactorsandthermallyinte grated operation. In a particular embodiment, process gas stream201isashiftedsyngasstreamexitingaWGS ata compositionofapproximately39mol% CO2,54mol% H2, and7mol% H2O,atatemperatureofapproximately250°C. and a total pressure of 280 psig. Process gas stream 201 undergoes heat transfer Q4 in heat exchanger 221, and input gasstream202exitsheatexchanger221Withacomposition ofapproximately39mol% CO2,54mol% H2,and7mol% H2O, at a ?rst temperature of approximately 150° C. and a totalpressureof280psig,representinga?rstCO2 pressureof approximately 109 psig. Heat exchanger 221 is an indirect heatexchangersuchasashell-and-tubeheatexchangerfacili tating heat transfer from process gas stream 201 to 25° C. coolingWater. 45PDF Image | PROCESS FOR CO2 CAPTURE USING ZEOLITES
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