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11 Usingtheexemplaryconditionsspeci?ed,inputgasstream 202 enters capture reactor 203 at the ?rst temperature of approximately150°C.andthe?rstCO2 pressureofapproxi mately 109 psig and contacts Zeolite sorbent 204 at the ?rst temperature. Zeolite sorbent 204 adsorbs substantially al CO2 andH20,andCO2 depletedgasstream205comprisedof H2 exitscapturereactor203 atthe?rsttemperatureandatotal pressure of 280 psig. In a particular embodiment, CO2 depletedgasstream203 exitstoanIGCC burningH2 forthe production of steam at a temperature of 550° C. Under the exemplary conditions speci?ed, When Zeolite 13X isutiliZedasZeolitesorbent204 inthecapturereactor, the Zeolite 13X sorbent has a CO2 capture capacity of approximately 3.0 mol/kg and an H2O capture capacity of approximately 1.11 mol/kg. The heat of adsorption is approximately 35 kJ/mol CO2 and 15.5 kJ/mol H2O. The exothermicheatgeneratedbyadsorptioninthecapturereac tor is removed by ?rst heat transfer Ql through an indirect heatexchangerfacilitatingheattransferfromZeolitesorbent 204 and capture reactor 203 to 25° C. cooling Water. 20 12 cooledbyheatexchanger219toathirdtemperaturelessthan thesecondtemperature.IntheparticularembodimentshoWn, output gas stream 208 is cooled to approximately 76° C. through indirect heat exchange With 25° C. cooling Water. This serves to condense moisture in output gas stream 208 for subsequent removal by moisture removing means 211, as Well as reduce compressor Work loads for any subsequent compression operations Which may exist as subsequent requirements. In a particular embodiment utiliZing Zeolite 13X, an input gasstreamof39mol% CO2,54mol% H2,and7mol% H2O, a ?rst temperature of 150° C., and a ?rst CO2 pressure of approximately 109 psig in capture reactor 203, With regen eration in regeneration reactor 206 at a second temperature of 350° C. and a second CO2 pressure of approximately 271 psig, output gas stream 208 exits regeneration reactor 206 Withacompositionof96.7mol% CO2and3.3mol% H2O. Following cooling by heat exchanger 219 and H20 removal by moisture removing means 211, output gas stream 208 has acompositionof98.0mol% CO2and2.0mol% H2O. IntheembodimentillustratedatFIG.2,folloWingmoisture removal, ?oW diverting means 213 splits output gas stream 208 into ?nal CO2 stream 210 and regeneration stream 209. FloWdivertingmeans213maybeany?oWdivertingdevice knoWn intheart,suchasaHow splittingvalveratedforthe prevailing conditions. Back pressure regulating means 220 maintains output gas stream 208 and regeneration gas stream 209 atthesecondCO2 pressure.Inaparticularembodiment, theprocessdepictedatFIG.2providesa?nalCO2stream210 havingacompositionof98.0mol% CO2and2.0mol% H2O, atatotalpressureof280psigandatemperatureof760C.The high purity, high pressure, and reduced temperature stream producedprovidessigni?cantadvantageintermsofanysub sequentcompressionrequired,andeliminatesorgreatly reducesanyfurthergasseparationoperations. In the embodiment illustrated at FIG. 2, regeneration gas stream 209 is then heated by a heat transfer O3 in heat exchanger 214 to match or approach the second temperature conditioninregenerationreactor206,andrecirculatedto regenerationreactor206tomaintaintheCO2 atmospherein regeneration reactor 206. In the embodiment shoWn, heat exchanger 214 facilitates heat transfer Q3 as an indirect heat exchange from Water at a temperature greater than the third temperaturetoregenerationgasstream209. Regeneration is conducted in regeneration vessel 206 for a ?xed period of time Which is suf?ciently long in duration to desorbsubstantiallyalCO2 andH20 andproduceunloaded Zeolitesorbent.HavingsubstantiallydesorbedalCO2 and H20,theunloadedZeolitesorbentistransferredfromregen erationreactor206viatransportpath215.Intheembodiment illustrated at FIG. 2, the unloaded Zeolite sorbent is cooled With heat transfer O5 to match or approach the ?rst tempera ture condition in capture reactor 206, so that the cooled unloadedZeolitesorbentmayentercapturereactor203via transport path 217 to serve as the Zeolite sorbent in capture reactor 203. In the embodiment shoWn, heat exchanger 216 facilitatesheattransferQ5byindirectheatexchangebetWeen the loaded Zeolite sorbent and 25° C. cooling Water. Transport of the unloaded Zeolite sorbent via transport paths 215 and 217 may be accomplished similarly to the means employed for transport path 212. Inaparticularembodiment,heatexchangers221,216,and 214 are in thermal communication so that heat transfer Q5 maybecomprisedofheatfromheattransfersQ4andQ3.This servestoreducetheoverallheatinputrequiredbytheprocess. In the particular embodiment shoWn at FIG. 2, heat exchang The input gas stream 202 and the Zeolite sorbent 204 are contacted in capture reactor 203 at the ?rst temperature and the ?rst CO2 pressure for a ?xed period of time Which is suf?ciently short in duration so as to prevent the break throughofcarbondioxideinCO2-depletedgasstream205. 25 Followingthe?xedperiodoftime,loadedZeolitesorbentat the?rsttemperatureand?rstCO2 pressureistransferredto regeneration reactor 206 via transport path 212. Transport may be accomplished in a variety of Ways knoWn to those skilledintheart.Forexample,Zeolitesorbent204maybe arrangedincapturereactor203 inapluralityofseparatebeds to from a moving bed arrangement for transfer from capture reactor 203 to regeneration reactor 206, Where the moving bedarrangementiscycledsuchthatagivenbedistransferred afterremainingintheadsorptionconditionsincapturereactor35 203 for the ?xed period of time. Other arrangements include ?uidized transfer of sorbent pellets from capture reactor 203 toregenerationreactor206folloWingthe?xedperiodoftime. Withinthediscussionoftheparticularembodimentdepicted atFIG.2,itisonlynecessarythatloadedZeolitesorbentbe 40 transferred from capture reactor 203 to regeneration reactor 206 under temperature and pressure conditions that maintain asubstantialmajorityofadsorbedCO2 andH20 adsorbedon the loaded Zeolite sorbent, so that the substantial majority of adsorbedCO2andH20maybedesorbedinregeneration45 reactor206. Regeneration reactor 206 is maintained at a second tem perature and second CO2 pressure. In a particular embodi ment, regeneration reactor 206 is maintained at approxi mately3500C.andcontainsaCO2atmospherecomprisedof50 greater than 90 mol % gaseous CO2 at a total pressure of approximately280psig.Undertheseexemplaryconditions, When Zeolite13X isthesorbentutiliZed,thisresultsinaCO2 capturecapacityofapproximately0.01mol/kgandsubstan tiallycompletedehydration.AsecondheattransferQ2trans 55 fers heat to the loaded Zeolite sorbent through indirect heat exchange in order to raise and maintain the loaded Zeolite sorbentatthesecondtemperatureasCO2 andH20 aredes orbed.Inaparticularembodiment, secondheattransferO2 is providedbyindirectheattransferfromaportionofthe550° 60 C.steamgeneratedbytheIGCC fueledbyCO2-depletedgas stream 205. Output gas stream 208 comprised of CO2 and H20 exits regeneration reactor 206 at the second temperature and a secondCO2pressureofapproximately252psig,re?ecting65 the CO2 atmosphere total pressure of 280 psig at a CO2 content of at least 90 mol %. Output gas stream 208 is then US 8,128,735B1 30PDF Image | PROCESS FOR CO2 CAPTURE USING ZEOLITES
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