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13 ers 221, 216, and 214 utilize Water as a Working ?uid to transport heat from heat exchanger 221 and 216 to heat exchanger214. Further, While capture and regeneration are shown With a counter-current geometry in capture reactor 203 and regen eration reactor 206, it is understood that capture reactor 203 andregenerationreactor206couldbeoperatedinaco-current geometry. Thus,thisdisclosureprovidesamethodofCO2separation utiliZing Zeolite adsorbents that alloWs for higher pressure regeneration,suchthatahigherpressureCO2 productstream is produced and compression burdens Which might exist in sequestration and storage operations are reduced or elimi nated.Further,themethodprovidesforCO2 separationuti liZing Zeolite adsorbents in a manner that preserves adsorp tion capacities at higher temperatures, such that parasitic external refrigeration loads are reduced or eliminated. Fur ther,themethodprovidesforCO2 separationutiliZingZeolite adsorbents in a TSA process Where sorbent regeneration occursinanatmosphereofCO2,suchthatapurestreamofthe 20 CO2isgeneratedWithouttheneedforfurthergasseparations. 14 Contacting the input gas stream With the Zeolite sorbent at a?rsttemperatureandthe?rstCO2 pressure,suchthat theZeolitesorbentadsorbssomeportionoftheCO2 from the input gas stream, and transferring heat from the Zeolite sorbent With a ?rst heat transfer to maintain the Zeolite sorbent at the ?rst temperature, thereby produc ingaloadedZeolitesorbent; SurroundingtheloadedZeolitesorbentWithaC02 atmo spherecomprisedofatleast90mol% CO2toattaina second CO2 pressure, Where the second CO2 pressure is greater than the ?rst CO2 pressure, and increasing the temperature of the loaded Zeolite sorbent to a second temperature by transferring heat to the loaded Zeolite sorbent With a second heat transfer, thereby producing desorbed CO2 from the loaded Zeolite sorbent and pro ducing an unloaded Zeolite sorbent; and Generating the output gas stream, Where the output gas streamiscomprisedofsomeportionoftheCO2 atmo sphere and some portion ofthe desorbed CO2, therebyseparatingCO2fromaprocessgasstreamcomprised ofCO2 andothergaseousconstituentsinanadsorption/des orption cycle using a Zeolite sorbent, Where the desorption temperature and pressures are exemplary only. Within this method,itisonlynecessarythatthesecondtemperature25 exceedsthe?rsttemperatureandthatthesecondCO2 pres sureexceedsthe?rstCO2 pressure,sothatsothatadsorption at the ?rst temperature and desorption at the second tempera turecanbeexpectedtooccur,andanoutputgasstreamcanbe producedatasecondCO2pressureexceedingthe?rstCO2 30 pressure. Similarly, it is understood that While speci?c Zeo lites have been utilized for illustrative purpose, the speci?c Zeolites are exemplary only. Within this method, the Zeolite utiliZed may be any Zeolite sorbent Which adsorbs gaseous CO2inaccordanceWithanadsorptionisothermasde?ned35 herein. Further, it is understood that the term “capture reac tor”and“regenerationreactor”may specifysinglereactorsor may refertoapluralityofreactorseachprovidingthecondi tionsspeci?edWithinthisdisclosure. andincreasedCO2 pressuretoproduceahighpressureoutput gasstream. 2. The method of claim 1 Where the input gas stream is furthercomprisedofH20 andthesecondtemperatureisat least 275 degrees Celsius. 3.Themethodofclaim1WheretheCO2 atmospheresur roundingtheloadedZeoliteisprovidedbyaregeneration stream comprised of a portion of the output gas stream. 4. The method of claim 1 Where the input gas stream is contacted With a Zeolite sorbent in a capture reactor, and including transferring the loaded Zeolite sorbent from the capturereactortoaregenerationreactor,andWherethe loadedZeolitesorbentissurroundedWithaC02 atmosphere intheregenerationreactor,andtheoutputgasstreamisgen eratedfromtheregenerationreactor. 5. The method of claim 4 including transferring the unloadedZeolitesorbentfromtheregenerationreactortothe capture reactor and cooling the unloaded Zeolite during the transfer, such that the unloaded Zeolite sorbent serves as the Zeolitesorbentatthe?rsttemperatureandtheinitialpressure. US 8,128,735B1 It is understood that While speci?c temperatures and pres sureshavebeenutiliZedforillustrativepurposes,thespeci?c cycleisconductedunderconditionsofincreasedtemperature Havingdescribedthebasicconceptoftheinvention,itWill40 be apparent to those skilled in the art that the foregoing detailed disclosure is intended to be presented by Way of example only, and is not limiting. Various alterations, improvements, and modi?cations are intended to be sug gestedandareWithinthescopeandspiritofthepresent45 invention. Additionally, the recited order of elements or sequences, or the use of numbers, letters, or other designa tionstherefore,isnotintendedtolimittheclaimedprocesses 7.Themethodofclaim6includingcoolingtheoutputgas toanyorderexceptasmay bespeci?edintheclaims.Accord ingly,theinventionislimitedonlybythefolloWingclaims50 andequivalentsthereto. All publications and patent documents cited in this appli cation are incorporated by reference in their entirety for pur poses to the same extent as ifeach individual publication or patentdocumentWeresoindividuallydenoted. 55 The invention claimed is: 1.A methodofseparatingCO2 fromaprocessgasstream comprised of CO2 and other gaseous constituents in an adsorption/desorptioncycleusingaZeolitesorbent,Wherethe60 desorptioncycleisconductedunderconditionsofincreased temperature and increased CO2 pressure to produce a high pressureoutputgasstream,comprising: stream to a third temperature then splitting the output gas streamintotheregenerationstreamanda?nalCO2stream, and including heating the regeneration stream With a third heat transfer. 8. The method of claim 7 Where the input gas stream is further comprised of H20, and including removing some portionoftheH20fromtheoutputgasstreamatthethird temperature. 9. The method of claim 7 Where the process gas stream has atemperatureexceedingthe?rsttemperature,andincluding cooling the process gas stream to the ?rst temperature With a fourthheattransferandtransferringheatfromthefourthheat transfer to the regeneration stream, such that the third heat transferiscomprisedofheatfromthefourthheattransfer. 10. The method of claim 9 Where the process gas stream is a shifted syngas stream from a Water-gas-shift reactor. 11.Themethodofclaim7WheretheunloadedZeolite sorbentiscooledduringtransferWitha?fthheattransfer,and includingtransferringheatfromthe?fthheattransfertothe Generating an input gas stream comprised of the process gasstream,suchthattheinputgasstreamiscomprised ofCO2 andothergaseousconstituents,andsuchthatthe inputgasstreamhasa?rstCO2 pressure; 65 6.Themethodofclaim5WheretheCO2 atmospheresur roundingtheloadedZeoliteintheregenerationreactoris provided by a regeneration stream comprised of a portion of the output gas stream.PDF Image | PROCESS FOR CO2 CAPTURE USING ZEOLITES
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