Process for CO2 capture using zeolites from high pressure and moderate temperature gas streams

Abstract

A method for separating CO2 from a gas stream comprised of CO2 and other gaseous constituents using a zeolite sorbent in a swing-adsorption process, producing a high temperature CO2 stream at a higher CO2 pressure than the input gas stream. The method utilizes CO2 desorption in a CO2 atmosphere and effectively integrates heat transfers for optimizes overall efficiency. H2O adsorption does not preclude effective operation of the sorbent. The cycle may be incorporated in an IGCC for efficient pre-combustion CO2 capture. A particular application operates on shifted syngas at a temperature exceeding 200° C. and produces a dry CO2 stream at low temperature and high CO2 pressure, greatly reducing any compression energy requirements which may be subsequently required.

Description

TECHNICAL FIELD

A method for separating CO₂ from a gas stream comprised of CO₂ and other gaseous constituents using a zeolite sorbent in a swing-adsorption process, producing a high temperature CO₂ stream at a higher CO₂ pressure than the input gas stream. The method utilizes CO₂ desorption in a CO₂ atmosphere and effectively integrates heat transfers for optimizes overall efficiency. H₂O adsorption does not preclude effective operation of the sorbent. The cycle may be incorporated in an IGCC for efficient pre-combustion CO₂ capture. A particular application operates on shifted syngas at a temperature exceeding 200° C. and produces a dry CO₂ stream at low temperature and high CO₂ pressure, greatly reducing any compression energy requirements which may be subsequently required.

BACKGROUND OF THE INVENTION

The emission of CO₂ from power plants has been identified as a factor potentially resulting in long-term environmental problems. Consequently, separation of CO₂ from gaseous streams utilizing adsorption of gases and vapors by microporous solids has attracted attention, because of its great practical importance in the fields of gas separation and gas purification. Certain technologies based on the CO₂ adsorption/desorption by using natural and synthetic zeolites are among the most effective methods.

Generally, two methods are used for CO₂ adsorption/desorption utilizing zeolite adsorbents for CO₂ separation: Temperature Swing Adsorption (TSA) and Pressure Swing Adsorption (PSA). In each of these techniques, a bed of zeolite adsorbent is exposed to a flow of feed air under temperature and pressure conditions allowing the zeolite adsorbent to adsorb some portion of the carbon dioxide and water vapor present in the feed air. This exposure continues for a period of time, and typically ceases prior to break-through of carbon dioxide and water in the exiting treated feed air. Following this exposure, the flow of feed air is ceased and the adsorbent is regenerated. In a temperature swing adsorber, the carbon dioxide and water are driven off from the adsorbent by heating the adsorbent in the regeneration phase. In a pressure swing adsorber, the pressure of the regeneration gas is lower than that of the feed gas and the change in pressure is used to remove the carbon dioxide and water from the adsorbent.

There has been extensive research on the equilibrium of carbon dioxide on zeolite adsorbent materials at ambient temperature and atmospheric pressure. It is established that zeolites efficiently remove carbon dioxide and water vapor from air streams at low temperatures, i.e., temperatures of about 40° C. or lower, because it more strongly adsorbs these components than it adsorbs nitrogen, oxygen or argon. However, at lower pressures, the carbon dioxide adsorption capacity of zeolites generally diminish rapidly as the temperature of the gas being separated increases, and the separation process can become infeasible at temperatures above about 40° C. This temperature limitation is further complicated by the heat of adsorption associated with zeolites, generating the tendency for adsorption bed temperatures to increase considerably, and often necessitating adsorption bed cooling with external refrigeration to maintain the gas at temperatures below 40° C. This places significant limitation on the application of zeolites for adsorption of carbon dioxide at high temperature, which is becoming increasingly significant in fields such as emission control of fossil-fueled power systems, natural gas treatments, purification of hydrocarbons, and production of hydrogen gas, among others. In these applications and others, it would be advantageous to provide a cycle where zeolite adsorbents could be utilized in a manner preserving the adsorption capacity at higher temperatures, such that parasitic external refrigeration loads could be reduced or eliminated. Such a capability could have particular import for gaseous stream separation in the production of H₂ from shifted syngas using a water-gas-shift reactor, where any requirement to maintain temperature of the adsorbent bed below 20° C. levies significant refrigeration requirements. Such a capability has further advantage when separation operations occur prior to combustion of a non-adsorbed component, so that refrigeration requirements have a direct impact on the subsequent efficiency of the combustion. For example, the separation of CO₂ and H₂ from a water-gas shift (WGS) reactor in preparation for H₂ combustion in an Integrated Gasification Combined Cycle (IGCC) plant.

It is known that the adsorption of some zeolites increases as the pressure of the adsorbent bed in increased for some applications. See e.g., Siriwardane et al, “Adsorption of CO₂, N₂, and O₂ on natural zeolites,” Energy & Fuels, Vol. 17 (2003), discussing the adsorption of certain zeolites at temperatures of 25° C. and pressures up to 300 psig. See also Siriwardane et al, “Adsorption of CO₂ on Zeolites at Moderate Temperatures,” Energy & Fuels, Vol. 19 (2005), discussing the adsorption of certain zeolites at temperatures up to 120° C. and pressures up to 300 psig, and regeneration at 300° C. under an N₂ atmosphere. Generally speaking, investigations of diverse zeolites have indicated that the capacity for CO₂ adsorption is enhanced when the partial pressure of CO₂ increases. See Bonenfant et al, “Advances in principal factors influencing carbon dioxide adsorption on zeolites,” Sci. Technol. Adv. Mater. 9 (2008). A swing-adsorption cycle for CO₂ separation using zeolites that takes advantage of the propensity for increased adsorption as pressure increases would allow zeolite use at higher temperatures, further reducing or eliminating parasitic external refrigeration loads. Additionally, and significantly, such a swing-adsorption process would have great benefit if desorption could occur at the higher pressure and produce a higher pressure CO₂ product stream, reducing compression burdens which might exist in sequestration and storage operations.

Further, in CO₂ separation for the purpose of storage and sequestration, purity of the CO₂ product stream is of paramount importance. Often, in swing-adsorption cycles using zeolites for CO₂ separation, the higher temperature or lower pressure regeneration must be assisted by the use of an inert regeneration gas to strip the adsorbed carbon dioxide and water from the adsorbent. Typical approaches utilize N₂, He, or some portion of the post-adsorption feed gas. See e.g., U.S. Pat. No. 5,968,234, issued to Midgett, issued Oct. 19, 1999; see also U.S. Pat. No. 5,855,650, issued to Kalbassi et al, issued Jan. 5, 1999, among others. The use of regeneration gas often increases the recovery of CO₂ in zeolite based swing-adsorption processes, however the practice inherently dilutes the recovered CO₂ stream. In applications where purity of the generated CO₂ stream is desired, such as in CO₂ sequestration and storage operations, the diluted stream must undergo further separation for removal of the regeneration gas, and further inefficiencies result. It would be advantageous to provide a swing-adsorption process for CO₂ separation using zeolites where sorbent regeneration could occur in an atmosphere of CO₂. The use of CO₂ as sweep gas during regeneration would result in the generation of a pure stream of the gas without the need for further gas separations.

Accordingly, it is an object of this disclosure to provide a method of CO₂ separation utilizing zeolite adsorbents in a manner that preserves adsorption capacities at higher temperatures, such that parasitic external refrigeration loads are reduced or eliminated.

Further, it is an object of this disclosure to provide a method of CO₂ separation utilizing zeolite adsorbents that takes advantage of the propensity for increased adsorption under increased CO₂ partial pressure and allows for higher pressure regeneration, such that a higher pressure CO₂ product stream is produced and compression burdens which might exist in sequestration and storage operations are reduced or eliminated.

Further, it is an object of this disclosure to provide a method of CO₂ separation utilizing zeolite adsorbents in a TSA process where sorbent regeneration occurs in an atmosphere of CO₂, such that a pure stream of the CO₂ is generated without the need for further gas separations.

These and other objects, aspects, and advantages of the present disclosure will become better understood with reference to the accompanying description and claims.

SUMMARY OF INVENTION

The disclosure provides a method for separating CO₂ from a gas stream comprised of CO₂ and other gaseous constituents using a zeolite sorbent in a swing-adsorption process that produces a relatively pure CO₂ stream during zeolite sorbent regeneration, such that further gaseous separation operations are eliminated. Additionally, the method allows for CO₂ adsorption at higher temperatures and higher pressures, reducing the energy loss associated with cooling gaseous streams when separation precedes combustion of a non-adsorbed component. Further, the method allows for CO₂ desorption in a CO₂ atmosphere, producing a high purity, high pressure CO₂ stream and reducing compression burdens which might exist in sequestration and storage operations. The method effectively lends itself to a CO₂ separation cycle whereby necessary heat transfers within the cycle are effectively integrated such that overall efficiency is optimized, and H₂O adsorption does not preclude effective operation of the sorbent.

The regeneration of the CO₂ loaded zeolite sorbent in a CO₂ atmosphere is a novel aspect of the method disclosed herein. Adsorption occurs under a first temperature and a first CO₂ pressure condition, where the first CO₂ pressure is generally the partial pressure of CO₂ in an input gas stream comprised of CO₂, H₂O, and other gaseous constituents. Desorption is provoked by heating the loaded zeolite sorbent in a CO₂ atmosphere of at least 90 wt % CO₂, so that regeneration occurs at a higher, second CO₂ pressure, and a product CO₂ stream of high purity and high CO₂ pressure results. In a particular embodiment, the method incorporates cyclic operation of the sorbent between a capture reactor and a regeneration reactor in a thermally integrated manner for optimized efficiency. In a further embodiment, the cycle is incorporated in an IGCC for efficient pre-combustion CO₂ capture.

The method generally comprises: generating an input gas stream comprised of CO₂ and other gaseous constituents at a first CO₂ pressure; contacting the input gas stream with a zeolite sorbent at a first temperature and the first CO₂ pressure, and transferring exothermic heat; regenerating the zeolite sorbent at a higher, second temperature in a CO₂ atmosphere comprised of at least 90 mol % CO₂ to attain a second, higher CO₂ pressure, and providing endothermic heat, and; generating the output gas stream comprised of desorbed CO₂ and some portion of the CO₂ atmosphere, in order to produce a high purity output gas stream having a higher CO₂ pressure than the input gas stream. In a particular embodiment, the CO₂ atmosphere is maintained by a regeneration stream comprised of some portion of the output gas stream. In another embodiment, the input gas stream is further comprised of H₂O and the second temperature provides for dehydration prior to moisture removal, producing a dry final CO₂ stream. A particular application utilizes an input gas stream of shifted syngas at a temperature exceeding 200° C., capture at approximately 150° C., and regeneration at approximately 350° C. in order to produce a final CO₂ stream having low moisture, low temperature, and high CO₂ pressure, greatly reducing any compression energy requirements which may be subsequently required.

The various features of novelty which characterize this disclosure are pointed out with particularity in the claims annexed to and forming a part of this disclosure. For a better understanding of the invention, its operating advantages and specific objects attained by its uses, reference is made to the accompanying drawings and descriptive matter in which a preferred embodiment of the disclosure is illustrated.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1A illustrates CO₂ separation for an input gas stream comprised of CO₂ and other gaseous constituents utilizing a zeolite sorbent.

FIG. 1B illustrates the generation of a CO₂ stream by regenerating the zeolite sorbent in a high CO₂ pressure environment.

FIG. 2 illustrates a cyclic process using a capture reactor and a regeneration reactor with zeolite sorbent transfer in a thermally integrated cycle.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

The following description is provided to enable any person skilled in the art to use the invention and sets forth the best mode contemplated by the inventor for carrying out the invention. Various modifications, however, will remain readily apparent to those skilled in the art, since the principles of the present invention are defined herein specifically to provide a method of separating CO₂ from a process gas stream comprised of CO₂ and other gaseous constituents in an adsorption/desorption cycle using a zeolite sorbent, where the desorption cycle is conducted under conditions of increased temperature and increased CO₂ pressure to produce a high pressure output gas stream.

The disclosure herein provides a method for separating CO₂ from a gas stream comprised of CO₂ and other gaseous constituents using a zeolite sorbent in a swing-adsorption process that produces a relatively pure CO₂ stream during zeolite sorbent regeneration, such that further gaseous separation operations are eliminated. Additionally, the method allows for CO₂ adsorption at higher temperatures and higher pressures, reducing the energy loss associated with cooling gaseous streams when separation precedes combustion of a non-adsorbed component. Further, the method allows for CO₂ desorption in a CO₂ atmosphere, producing a high purity, high pressure CO₂ stream and reducing compression burdens which might exist in sequestration and storage operations. The method effectively lends itself to a CO₂ separation cycle whereby necessary heat transfers within the cycle are effectively integrated such that overall efficiency is optimized, and H₂O adsorption does not preclude effective operation of the sorbent.

The regeneration of the CO₂ loaded zeolite sorbent in a CO₂ atmosphere is a novel aspect of the method disclosed herein. Adsorption occurs under a first temperature and a first CO₂ pressure condition, where the first CO₂ pressure is generally the partial pressure of CO₂ in an input gas stream comprised of CO₂, H₂O, and other gaseous constituents. Desorption is provoked by heating the loaded zeolite sorbent in a CO₂ atmosphere of at least 90 wt % CO₂, so that regeneration occurs at a higher, second CO₂ pressure, so that a product CO₂ stream of high purity and high pressure results. This is in marked contrast to standard temperature-swing adsorption processes, which often produce a diluted product stream through the use of an inert regeneration gas in order to provide a high temperature, low CO₂ pressure environment favorable to desorption. Similarly, this is in marked contrast to typical pressure-swing adsorption processes, which by necessity result in a product stream having a lower CO₂ pressure than the input gas stream. Within the novel method disclosed here, regeneration in an environment of increased CO₂ pressure allows for the production of a high pressure, high purity CO₂ stream without the necessity for further separation operations or subsequent compression, greatly aiding subsequent storage and sequestration operations. In a particular embodiment, the CO₂ atmosphere is provided by recirculation of the CO₂ product stream. In another particular embodiment, the input gas stream is further comprised of H₂O and regeneration is conducted at a temperature at least 275° C., in order to desorb both CO₂ and H₂O from the loaded zeolite sorbent, such that the zeolite sorbent may be used in a cyclic manner.

The method disclosed herein may be particularly advantageous in IGCC applications that encompass pre-combustion separation of CO₂ from shifted syngas. In a particular embodiment, the zeolite sorbent adsorbs CO₂ in a capture reactor maintained at approximately 150° C. and 280 psig, and the zeolite sorbent is regenerated and CO₂ desorbed in a >90 mol % CO₂ atmosphere in a regeneration reactor, maintained at approximately 350° C. and 280 psig. The temperature and pressure range of this novel method reduces the negative impact on IGCC efficiency associated with cooling the input shifted syngas stream to ambient, and produces a higher pressure, high purity CO₂ stream aiding subsequent CO₂ storage and sequestration operations. Additionally, and significantly, the method retains effectiveness when H₂O is present in the input gas stream, eliminating the pre-emptive drying requirement associated with typical CO₂ removal cycles.

As used here, “zeolite” means crystalline aluminosillicates of alkali or alkali earth elements such as sodium, potassium, and calcium, represented by the stochiometry M_x/n[(AlO₂)_x(SiO₂)_y], where x and y are integers with y/x equal to or greater than 1 and n is the valence of cation M.

As used here, “CO₂ pressure” means the partial pressure of CO₂ in a gaseous mixture having a total pressure and comprised of CO₂ and which may be comprised of additional constituents. Further, when the method specifies “first CO₂ pressure” or “second CO₂ pressure,” in application these are considered as mean values around which variation may be expected to occur as a result of operational constraints.

As used here, “adsorption isotherm”, means the relationship between a CO₂ pressure and the mass of CO₂ gas or vapor taken up per mass of zeolite sorbent at a constant temperature.

As used here, the terms “indirect” or “indirectly” when applied to heat exchange means a process of heat transfer from a heat containing medium to a heat absorbing medium without direct contact between the two media involved. For example, heat transfer from steam to a zeolite sorbent through a heat exchanger tube separating the steam and the zeolite sorbent, or heat transfer from a zeolite sorbent to a water coolant through a heat exchanger tube separating the zeolite sorbent and the water coolant, and other similar arrangements.

As used here, the term “shifted syngas” means a composition produced by a process which converts water and carbon monoxide to hydrogen and carbon dioxide. For example, a composition produced by a water gas shift process or steam reforming.

The method disclosed herein is generally practiced as a cyclical process of TSA, with the novel distinction that CO₂ pressure is increased during the regeneration process through utilization of concentrated CO₂, as opposed to typical TSA cycles. The method may be illustrated with reference to FIGS. 1A and 1B. At FIG. 1A, a process gas stream 101 comprises an input gas stream 102 from which CO₂ is to be separated. The input gas stream 102 is introduced into a capture vessel 103 containing a bed of the zeolite sorbent 104. The input gas stream 102 and the zeolite sorbent 104 are contacted in the capture vessel 103 at a first temperature and a first CO₂ pressure, where the first temperature and first CO₂ pressure are representative of an adsorption condition defined by an adsorption isotherm of zeolite sorbent 104 reflecting adsorption of gaseous CO₂.

The first temperature and the first CO₂ pressure may be mean values around which slight variation occurs as a result of operational constraints. The acceptable magnitude of variation of the first temperature and the first CO₂ pressure depends on the subsequent regeneration conditions utilized, as will be explained infra. Thus, when the method specifies maintaining a first temperature or a first CO₂ pressure, it is understood that this is intended to indicate maintaining these parameters within the acceptable magnitude of variation about the mean value.

Zeolite sorbent 104 may be any zeolite sorbent which adsorbs gaseous CO₂ in accordance with an adsorption isotherm as defined herein. Exemplary zeolite sorbents for use with this method include zeolite 4A (e.g., Na₂O—Al₂O₃-2SiO₂), zeolite 5A (e.g., 0.7CaO-0.3Na2O—Al₂O₃-2SiO₂-4.5H₂O), and zeolite 13X (e.g., 5Na₂O-5Al₂O₃-14SiO₂, Na_x[(AlO₂)_x—(SiO₂)_y]). The first temperature and first CO₂ pressure may be any magnitude, provided that the first temperature and the first CO₂ pressure are representative of an adsorption condition defined by the adsorption isotherm of zeolite sorbent 104 reflecting adsorption of gaseous CO₂. In a particular embodiment, the first CO₂ pressure exceeds 70 psig and the first temperature exceeds 100° C. In another particular embodiment, zeolite sorbent 104 is zeolite 13X and the input gas stream 102 is shifted syngas comprised CO₂ and H₂O at a temperature of 120° C.-180° C. and a total pressure of 230-330 psig, and the input gas stream 102 and the zeolite sorbent 104 are contacted in the capture vessel 103 at a first temperature of 120° C.-180° C. and a first CO₂ pressure in accordance with the total pressure and CO₂ mol % in input gas stream 102.

As the input gas stream 102 passes through the bed of zeolite sorbent 104, CO₂ is adsorbed and a CO₂ front forms in the zeolite sorbent bed and travels through the bed, generating loaded zeolite sorbent containing at least adsorbed CO₂. Exothermic heat generated by CO₂ adsorption on the zeolite bed is removed from the capture vessel with a first heat transfer O₁ to substantially maintain conditions at the first 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 H₂O, such that the zeolite sorbent further adsorbs H₂O and the CO₂-depleted gas stream 105 is further depleted of H₂O. In another particular embodiment, the CO₂-depleted gas stream 105 powers an Integrated Gasification Combined Cycle.

First heat transfer Q₁ may be accomplished using a variety of heat sink means known in the art. For example, the heat sink could be a coolant fluid in a heat exchanger, another process technology requiring heat at about or less than the temperature of adsorption, or simply the atmosphere. Non-sorbed components of the gas that contacts the adsorbing media may also remove some exothermic heat during adsorption. In a particular embodiment, first heat transfer Q₁ is accomplished with a heat exchanger using water as a coolant fluid.

In a further embodiment, process gas stream 101 has a temperature exceeding the first temperature, and is cooled by heat transfer Q₄, so that input gas stream 102 enters capture vessel 103 at a temperature below that of process gas stream 101. In an exemplary application, process gas stream 101 is a shifted syngas stream produced in a WGS reactor at an approximate temperature of 250° C. and the first temperature in capture vessel 103 is 120-150° C., and heat transfer Q₄ is utilized to remove heat such that input gas stream 104 enters capture vessel 103 within the approximate temperature range 120-150° C. Heat transfer Q₄ may be accomplished using a variety of heat sink means known in the art, such as a coolant fluid 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, heat transfer Q₄ is accomplished with a heat exchanger using a medium in communication with other heat exchangers utilized in the method, so that at least some portion of heat transfer Q₄ may be utilized elsewhere in the process, as discussed infra.

The input gas stream 102 and the zeolite sorbent 104 are contacted in the capture vessel 103 at the first temperature and the first CO₂ pressure for a fixed period of time which is sufficiently short in duration so as to prevent the break-through of carbon dioxide in CO₂-depleted gas stream 105. The quantity of CO₂ in CO₂-depleted gas stream 105 which designates break-through is not specified within this method and may be determined by an operator.

Following break-through, the zeolite sorbent is referred to as loaded zeolite sorbent within this method. Regeneration of the loaded zeolite sorbent is discussed with reference to FIG. 1B. At FIG. 1B, regeneration vessel 106 holds loaded zeolite sorbent 107. Within regeneration vessel 106, loaded zeolite sorbent 107 is surrounded by a CO₂ atmosphere comprised of at least 90 mol % CO₂ at a second CO₂ pressure, where the second CO₂ pressure is greater than the first CO₂ pressure. A second heat transfer Q₂ increases the temperature of loaded zeolite sorbent 107 to a second temperature, where the second temperature is greater than the first temperature. As a result of the increase in temperature, loaded zeolite sorbent 107 desorbs some portion of the CO₂ adsorbed at the first temperature. The desorbed CO₂ enters the CO₂ atmosphere in regeneration vessel 106 at the second CO₂ pressure, and output gas stream 108 is generated by drawing some portion of the CO₂ atmosphere and the desorbed CO₂ from regeneration vessel 106. Output gas stream 108 thereby maintains a high purity of CO₂ and is produced at a CO₂ pressure exceeding the first CO₂ pressure of input gas stream 102.

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 for output gas stream 108. This is in marked contrast to standard temperature-swing adsorption processes, which often produce a diluted product stream through the use of a hot, inert regeneration gas in order to provide a high temperature, low CO₂ pressure environment for desorption. Similarly, this is in marked contrast to typical pressure-swing adsorption processes, which by necessity result in a product stream having a lower CO₂ pressure than the input gas stream. Within the novel method disclosed here, regeneration in an environment of increased CO₂ pressure allows for the production of a high pressure, high purity CO₂ stream without the necessity for further separation operations or subsequent compression, greatly aiding subsequent storage and sequestration operations.

The second temperature and the second CO₂ pressure are representative of an adsorption condition defined by an adsorption isotherm of zeolite sorbent 107 reflecting adsorption of gaseous CO₂ and, as specified supra, exceed the first temperature and the first CO₂ pressure respectively. Similar to the first temperature and the first CO₂ pressure discussed supra, the second temperature and the second CO₂ pressure may be mean values around which slight variation occurs as a result of operational constraints. The acceptable magnitude of variation of the second temperature and the second CO₂ pressure is not a limiting value, except that the magnitude of variation should be controlled such that the lowest magnitude of the second temperature exceeds the highest value of the first temperature, and such that the lowest value of the second CO₂ pressure exceeds the highest value of the first CO₂ pressure, so that adsorption in capture vessel 103 and desorption in regeneration vessel 106 can be expected to occur within the potential ranges of the first temperature and the second temperature, and an output gas stream can be produced at a second CO₂ pressure exceeding the first CO₂ pressure. Thus, when the method specifies maintaining a second temperature or a second CO₂ pressure, it is understood that this is intended to indicate maintaining these parameters within the acceptable magnitude of variation about the mean value.

In a particular embodiment, loaded zeolite sorbent 107 is zeolite 13X with adsorbed CO₂ and H₂O, and the second temperature is at least 275° C., so that loaded zeolite sorbent 107 desorbs both CO₂ and substantially all H₂O in regeneration vessel 106. In another embodiment, where the loaded zeolite sorbent 107 is zeolite 13X and the input gas stream 102 is shifted syngas comprised of CO₂ and H₂O, a second temperature of 275° C.-380° C. and a second CO₂ pressure of approximately 209-297 psig is utilized for desorption in regeneration vessel 106, following adsorption in capture vessel 103 under a first temperature of 120° C.-180° C. and a first CO₂ pressure in accordance with a total pressure between 230-330 psig and the CO₂ mol % in input gas stream 102. In the latter embodiment, the zeolite 13X CO₂ capture capacities are approximately 3.0 mol/kg sorbent in the capture vessel and 0.01 mol/kg in the regeneration vessel. The low CO₂ capture capacity under the second temperature and in an atmosphere of 90 mol % gaseous CO₂ allows regeneration at a high second CO₂ pressure.

Second heat transfer Q₂ is applied indirectly to the adsorbent material through a heating coil, electrical heat source, a heat exchanger in intimate association with the adsorbent material, or other heat source means known in the art. In a particular embodiment, second heat transfer O₂ is accomplished with a heat exchanger using some portion the steam generated by an IGCC plant powered by at least a portion of 002-depleted gas stream 105.

In a particular embodiment, output gas stream 108 is indirectly cooled to a third temperature below the second temperature by heat exchanger 119, and a total pressure of at least the second CO₂ pressure is maintained by back pressure regulating means 120, in order to produce final CO₂ stream 110. 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 pressure maintained by back pressure regulating means 120 is the second CO₂ pressure. The reduction in temperature to the third temperature is particularly advantageous when further compression of final CO₂ stream 110 outside the method disclosed herein is desired, and the lower third temperature of the final CO₂ stream serves to reduce subsequent compressor work required. In such applications, output gas stream 108 may be indirectly cooled to the third temperature using a variety of heat sink means known in the art. For example, the heat sink could be a coolant fluid 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 cooled with a heat exchanger using water as a coolant fluid. Similarly, back pressure regulating means 120 may be variety of pressure regulating devices known in the art. For example, back pressure regulating means 120 may be a back pressure regulator valve.

In a particular embodiment, where input gas stream 102 is further comprised of H₂O and output gas stream 108 contains H₂O, moisture removing means 111 may be employed following heat exchanger 119 in order to remove some portion of the H₂O at the third temperature, such that final CO₂ stream 110 has a reduced moisture content as compared to output gas stream 108. In a particular embodiment, the third temperature is below the saturation temperature for H₂O in output gas stream 108, and the H₂O is removed as a condensate using screens or other tortuous flow paths in moisture removing means 111 as is known in the art.

In a further embodiment, the CO₂ atmosphere in regeneration vessel 106 is provided by regeneration stream 109, comprised of a portion of output gas stream 108 as indicated at FIG. 1B. When the CO₂ atmosphere is provided by regeneration stream 109, back pressure regulating means 120 serves to maintain regeneration stream 109 at the total pressure of output gas stream 108, and regeneration stream 109 is heated by a heat transfer Q₃ to match or approach the second temperature condition in regeneration vessel 106. In a particular embodiment, the heat transfer Q₃ is accomplished with a heat exchanger using a medium in communication with other heat exchangers utilized in the method, so that at least some portion of heat transfer Q₃ may be comprised of heat removed elsewhere in the process, as discussed infra. Additionally, when input gas stream 102 is further comprised of H₂O and output gas stream 108 contains H₂O, regeneration stream 109 follows moisture removing means 111 to reduce the moisture content of regeneration stream 109.

Regeneration is generally conducted in regeneration vessel 106 for a fixed period of time which is sufficiently long in duration to desorb substantially all CO₂ and H₂O when applicable from the loaded zeolite sorbent, however the fixed period of time for regeneration is not specified within this method and may be determined by an operator using various indications known to those skilled in the art. For example, comparison of flow rates between output gas stream 108 or final CO₂ stream 110 and regeneration stream 109 may be utilized as an indication of regeneration completion, or the fixed period of time may be specified based on past experience with the system, or using other methodologies known to those skilled in the art. Following regeneration, the zeolite sorbent is referred to as unloaded zeolite sorbent within this method.

Regeneration in the manner provided thus provides a high purity product stream of CO₂ having a higher CO₂ pressure than input gas stream 102 and having a total pressure commiserate with or greater than the first CO₂ pressure of input gas stream 102. Additionally, in a particular embodiment, final CO₂ stream 110 may be produced at a third temperature below the first temperature, greatly reducing subsequent compression burdens if desired. In an exemplary embodiment where input gas stream 102 is shifted syngas comprised of CO₂ and H₂O and adsorption occurs under a first temperature of 150° C. and a first CO₂ pressure of approximately 109 psig (reflecting a total pressure of 280 psig and CO₂ content of 39 mol %), followed by regeneration at a second temperature of 350° C. and a second CO₂ pressure of approximately 252 psig (reflecting a CO₂ atmosphere total pressure of 280 psig at a CO₂ content of at least 90 mol %), a final CO₂ stream 110 with a purity of 98 mol % CO₂ and having a total pressure of 280 psig at a temperature of 76° C. may be produced. The production of this high pressure, high purity CO₂ stream without the necessity for further separation operations or subsequent compression is based on regeneration in a CO₂ atmosphere of at least 90 mol % CO₂, and is a novel aspect of this disclosure.

It is understood that while capture vessel 103 at FIG. 1A and regeneration vessel 106 at FIG. 1B have been discussed as separate and distinct entities in the foregoing explanation, capture vessel 103 and regeneration vessel 106 may be a single vessel capable of providing both the adsorption and regeneration conditions discussed. Additionally, it is understood that when capture vessel 103 and regeneration vessel 106 are separate vessels, the sorbent may be transferred between capture vessel 103 and regeneration vessel 106, 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 vessel 103.

FIG. 2 illustrates a process flow diagram demonstrating the method operated in a substantially continuous mode utilizing separate capture and regeneration reactors and thermally integrated operation. In a particular embodiment, process gas stream 201 is a shifted syngas stream exiting a WGS at a composition of approximately 39 mol % CO₂, 54 mol % H₂, and 7 mol % H₂O, at a temperature of approximately 250° C. and a total pressure of 280 psig. Process gas stream 201 undergoes heat transfer Q₄ in heat exchanger 221, and input gas stream 202 exits heat exchanger 221 with a composition of approximately 39 mol % CO₂, 54 mol % H₂, and 7 mol % H₂O, at a first temperature of approximately 150° C. and a total pressure of 280 psig, representing a first CO₂ pressure of approximately 109 psig. Heat exchanger 221 is an indirect heat exchanger such as a shell-and-tube heat exchanger facilitating heat transfer from process gas stream 201 to 25° C. cooling water.

Using the exemplary conditions specified, input gas stream 202 enters capture reactor 203 at the first temperature of approximately 150° C. and the first CO₂ pressure of approximately 109 psig and contacts zeolite sorbent 204 at the first temperature. Zeolite sorbent 204 adsorbs substantially all CO₂ and H₂O, and CO₂ depleted gas stream 205 comprised of H₂ exits capture reactor 203 at the first temperature and a total pressure of 280 psig. In a particular embodiment, CO₂ depleted gas stream 203 exits to an IGCC burning H₂ for the production of steam at a temperature of 550° C.

Under the exemplary conditions specified, when zeolite 13X is utilized as zeolite sorbent 204 in the capture reactor, 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 exothermic heat generated by adsorption in the capture reactor is removed by first heat transfer Q₁ through an indirect heat exchanger facilitating heat transfer from zeolite sorbent 204 and capture reactor 203 to 25° C. cooling water.

The input gas stream 202 and the zeolite sorbent 204 are contacted in capture reactor 203 at the first temperature and the first CO₂ pressure for a fixed period of time which is sufficiently short in duration so as to prevent the break-through of carbon dioxide in CO₂-depleted gas stream 205. Following the fixed period of time, loaded zeolite sorbent at the first temperature and first CO₂ pressure is transferred to regeneration reactor 206 via transport path 212. Transport may be accomplished in a variety of ways known to those skilled in the art. For example, zeolite sorbent 204 may be arranged in capture reactor 203 in a plurality of separate beds to from a moving bed arrangement for transfer from capture reactor 203 to regeneration reactor 206, where the moving bed arrangement is cycled such that a given bed is transferred after remaining in the adsorption conditions in capture reactor 203 for the fixed period of time. Other arrangements include fluidized transfer of sorbent pellets from capture reactor 203 to regeneration reactor 206 following the fixed period of time. Within the discussion of the particular embodiment depicted at FIG. 2, it is only necessary that loaded zeolite sorbent be transferred from capture reactor 203 to regeneration reactor 206 under temperature and pressure conditions that maintain a substantial majority of adsorbed CO₂ and H₂O adsorbed on the loaded zeolite sorbent, so that the substantial majority of adsorbed CO₂ and H₂O may be desorbed in regeneration reactor 206.

Regeneration reactor 206 is maintained at a second temperature and second CO₂ pressure. In a particular embodiment, regeneration reactor 206 is maintained at approximately 350° C. and contains a CO₂ atmosphere comprised of greater than 90 mol % gaseous CO₂ at a total pressure of approximately 280 psig. Under these exemplary conditions, when zeolite 13X is the sorbent utilized, this results in a CO₂ capture capacity of approximately 0.01 mol/kg and substantially complete dehydration. A second heat transfer Q₂ transfers heat to the loaded zeolite sorbent through indirect heat exchange in order to raise and maintain the loaded zeolite sorbent at the second temperature as CO₂ and H₂O are desorbed. In a particular embodiment, second heat transfer Q₂ is provided by indirect heat transfer from a portion of the 550° C. steam generated by the IGCC fueled by CO₂-depleted gas stream 205.

Output gas stream 208 comprised of CO₂ and H₂O exits regeneration reactor 206 at the second temperature and a second CO₂ pressure of approximately 252 psig, reflecting the CO₂ atmosphere total pressure of 280 psig at a CO₂ content of at least 90 mol %. Output gas stream 208 is then cooled by heat exchanger 219 to a third temperature less than the second temperature. In the particular embodiment shown, 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 gas stream of 39 mol % CO₂, 54 mol % H₂, and 7 mol % H₂O, a first temperature of 150° C., and a first CO₂ pressure of approximately 109 psig in capture reactor 203, with regeneration 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 with a composition of 96.7 mol % CO₂ and 3.3 mol % H₂O. Following cooling by heat exchanger 219 and H₂O removal by moisture removing means 211, output gas stream 208 has a composition of 98.0 mol % CO₂ and 2.0 mol % H₂O.

In the embodiment illustrated at FIG. 2, following moisture removal, flow diverting means 213 splits output gas stream 208 into final CO₂ stream 210 and regeneration stream 209. Flow diverting means 213 may be any flow diverting device known in the art, such as a flow splitting valve rated for the prevailing conditions. Back pressure regulating means 220 maintains output gas stream 208 and regeneration gas stream 209 at the second CO₂ pressure. In a particular embodiment, the process depicted at FIG. 2 provides a final CO₂ stream 210 having a composition of 98.0 mol % CO₂ and 2.0 mol % H₂O, at a total pressure of 280 psig and a temperature of 76° C. The high purity, high pressure, and reduced temperature stream produced provides significant advantage in terms of any subsequent compression required, and eliminates or greatly reduces any further gas separation operations.

In the embodiment illustrated at FIG. 2, regeneration gas stream 209 is then heated by a heat transfer Q₃ in heat exchanger 214 to match or approach the second temperature condition in regeneration reactor 206, and recirculated to regeneration reactor 206 to maintain the CO₂ atmosphere in 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 temperature to regeneration gas stream 209.

Regeneration is conducted in regeneration vessel 206 for a fixed period of time which is sufficiently long in duration to desorb substantially all CO₂ and H₂O and produce unloaded zeolite sorbent. Having substantially desorbed all CO₂ and H₂O, the unloaded zeolite sorbent is transferred from regeneration reactor 206 via transport path 215. In the embodiment illustrated at FIG. 2, the unloaded zeolite sorbent is cooled with heat transfer Q₅ to match or approach the first temperature condition in capture reactor 206, so that the cooled unloaded zeolite sorbent may enter capture reactor 203 via transport path 217 to serve as the zeolite sorbent in capture reactor 203. In the embodiment shown, heat exchanger 216 facilitates heat transfer Q₅ by indirect heat exchange between 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.

In a particular embodiment, heat exchangers 221, 216, and 214 are in thermal communication so that heat transfer Q₅ may be comprised of heat from heat transfers Q₄ and Q₃. This serves to reduce the overall heat input required by the process. In the particular embodiment shown at FIG. 2, heat exchangers 221, 216, and 214 utilize water as a working fluid to transport heat from heat exchanger 221 and 216 to heat exchanger 214.

Further, while capture and regeneration are shown with a counter-current geometry in capture reactor 203 and regeneration reactor 206, it is understood that capture reactor 203 and regeneration reactor 206 could be operated in a co-current geometry.

Thus, this disclosure provides a method of CO₂ separation utilizing zeolite adsorbents that allows for higher pressure regeneration, such that a higher pressure CO₂ product stream is produced and compression burdens which might exist in sequestration and storage operations are reduced or eliminated. Further, the method provides for CO₂ separation utilizing zeolite adsorbents in a manner that preserves adsorption capacities at higher temperatures, such that parasitic external refrigeration loads are reduced or eliminated. Further, the method provides for CO₂ separation utilizing zeolite adsorbents in a TSA process where sorbent regeneration occurs in an atmosphere of CO₂, such that a pure stream of the CO₂ is generated without the need for further gas separations.

It is understood that while specific temperatures and pressures have been utilized for illustrative purposes, the specific temperature and pressures are exemplary only. Within this method, it is only necessary that the second temperature exceeds the first temperature and that the second CO₂ pressure exceeds the first CO₂ pressure, so that so that adsorption at the first temperature and desorption at the second temperature can be expected to occur, and an output gas stream can be produced at a second CO₂ pressure exceeding the first CO₂ pressure. Similarly, it is understood that while specific zeolites have been utilized for illustrative purpose, the specific zeolites are exemplary only. Within this method, the zeolite utilized may be any zeolite sorbent which adsorbs gaseous CO₂ in accordance with an adsorption isotherm as defined herein. Further, it is understood that the term “capture reactor” and “regeneration reactor” may specify single reactors or may refer to a plurality of reactors each providing the conditions specified within this disclosure.

Having described the basic concept of the invention, it will 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 modifications are intended to be suggested and are within the scope and spirit of the present invention. Additionally, the recited order of elements or sequences, or the use of numbers, letters, or other designations therefore, is not intended to limit the claimed processes to any order except as may be specified in the claims. Accordingly, the invention is limited only by the following claims and equivalents thereto.

All publications and patent documents cited in this application are incorporated by reference in their entirety for purposes to the same extent as if each individual publication or patent document were so individually denoted.

Claims

1. A method of separating CO2 from a process gas stream comprised of CO2 and other gaseous constituents in an adsorption/desorption cycle using a zeolite sorbent, where the desorption cycle is conducted under conditions of increased temperature and increased CO2 pressure to produce a high pressure output gas stream, comprising: Generating an input gas stream comprised of the process gas stream, such that the input gas stream is comprised of CO2 and other gaseous constituents, and such that the input gas stream has a first CO2 pressure;Contacting the input gas stream with the zeolite sorbent at a first temperature and the first CO2 pressure, such that the zeolite sorbent adsorbs some portion of the CO2 from the input gas stream, and transferring heat from the zeolite sorbent with a first heat transfer to maintain the zeolite sorbent at the first temperature, thereby producing a loaded zeolite sorbent;Surrounding the loaded zeolite sorbent with a CO2 atmosphere comprised of at least 90 mol % CO2 to attain a second CO2 pressure, where the second CO2 pressure is greater than the first 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 producing an unloaded zeolite sorbent; andGenerating the output gas stream, where the output gas stream is comprised of some portion of the CO2 atmosphere and some portion of the desorbed CO2,

2. The method of claim 1 where the input gas stream is further comprised of H2O and the second temperature is at least 275 degrees Celsius.

3. The method of claim 1 where the CO2 atmosphere surrounding the loaded zeolite is provided by a regeneration 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 capture reactor to a regeneration reactor, and where the loaded zeolite sorbent is surrounded with a CO2 atmosphere in the regeneration reactor, and the output gas stream is generated from the regeneration reactor.

5. The method of claim 4 including transferring the unloaded zeolite sorbent from the regeneration reactor to the capture reactor and cooling the unloaded zeolite during the transfer, such that the unloaded zeolite sorbent serves as the zeolite sorbent at the first temperature and the initial pressure.

6. The method of claim 5 where the CO2 atmosphere surrounding the loaded zeolite in the regeneration reactor is provided by a regeneration stream comprised of a portion of the output gas stream.

7. The method of claim 6 including cooling the output gas stream to a third temperature then splitting the output gas stream into the regeneration stream and a final CO2 stream, 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 H2O, and including removing some portion of the H2O from the output gas stream at the third temperature.

9. The method of claim 7 where the process gas stream has a temperature exceeding the first temperature, and including cooling the process gas stream to the first temperature with a fourth heat transfer and transferring heat from the fourth heat transfer to the regeneration stream, such that the third heat transfer is comprised of heat from the fourth heat transfer.

10. The method of claim 9 where the process gas stream is a shifted syngas stream from a water-gas-shift reactor.

11. The method of claim 7 where the unloaded zeolite sorbent is cooled during transfer with a fifth heat transfer, and including transferring heat from the fifth heat transfer to the regeneration stream, such that the third heat transfer is comprised of heat from the fifth heat transfer.

12. The method of claim 4 including generating a CO2-depleted gas stream from the capture reactor, generating steam using an Integrated Gasification Combined Cycle powered by at least a portion of the CO2-depleted gas stream, and indirectly transferring heat from a portion of the generated steam to the regeneration reactor, such that the second heat transfer is comprised of heat from the portion of the generated steam.

13. The method of claim 1 where the zeolite sorbent is one of zeolite 4A, zeolite 5A, or zeolite 13X.

14. The method of claim 1 where the first CO2 pressure exceeds 70 psig and the first temperature exceeds 100 degrees Celsius.

15. A method of separating CO2 from a process gas stream comprised of CO2, H2O and other gaseous constituents in an adsorption/desorption cycle using a zeolite sorbent, where the desorption cycle is conducted under conditions of increased temperature and increased CO2 pressure to produce a final CO2 stream at high pressure, comprising: generating an input gas stream comprised of the process gas stream, such that the input gas stream is comprised of CO2, H2O and other gaseous constituents, and such that the input gas stream has a first CO2 pressure;Contacting the input gas stream with the zeolite sorbent at a first temperature and the first CO2 pressure in a capture reactor, such that the zeolite sorbent adsorbs some portion of the CO2 and some portion of the H2O from the input gas stream, and transferring heat from the zeolite sorbent with a first heat transfer to maintain the zeolite sorbent at the first temperature, thereby producing a loaded zeolite sorbent, and generating a CO2-depleted gas stream from the capture reactor;transferring the loaded zeolite sorbent from the capture reactor to a regeneration reactor, where the regeneration reactor contains a CO2 atmosphere, where the CO2 atmosphere is comprised of at least 90 mol % CO2 and where the CO2 atmosphere has a second CO2 pressure greater than the first CO2 pressure;increasing and maintaining the temperature of the loaded zeolite sorbent in the regeneration reactor at a second temperature by transferring heat to the loaded zeolite sorbent with a second heat transfer, where the second temperature exceeds the first temperature and the second temperature is at least 275 degrees Celsius, thereby producing desorbed CO2 and H2O from the loaded zeolite sorbent and producing an unloaded zeolite sorbent;Generating an output gas stream from the regeneration reactor, where the output gas stream is comprised of some portion of the CO2 atmosphere and some portion of the desorbed CO2 and H2O, and cooling the output gas stream to a third temperature below the first temperature and removing some portion of the H2O in the output gas stream;Splitting the output gas stream at the third temperature into a regeneration gas stream and the final CO2 stream, and directing the regeneration gas stream to the regeneration reactor, such that the CO2 atmosphere is comprised of CO2 from the regeneration stream; andtransferring the unloaded zeolite sorbent from the regeneration reactor to the capture reactor and cooling the unloaded zeolite sorbent during the transfer, such that the unloaded zeolite sorbent serves as the zeolite sorbent at the first temperature and the initial pressure, thereby separating CO2 from a process gas stream comprised of CO2, H2O and other gaseous constituents in an adsorption/desorption cycle using a zeolite sorbent, where the desorption cycle is conducted under conditions of increased temperature and increased CO2 pressure to produce the final CO2 stream at high pressure.

16. The method of claim 15 where the first temperature exceeds 120 degrees Celsius and the second temperature further exceeds 330 degrees Celsius.

17. The method of claim 15 where the regeneration stream is heated with a third heat transfer, and where the process gas stream has a temperature exceeding the first temperature and including cooling the process gas stream to the first temperature with a fourth heat transfer, and where the unloaded zeolite sorbent is cooled during transfer with a fifth heat transfer, and transferring heat from the fourth heat transfer and the fifth heat transfer to the regeneration stream, such that the third heat transfer is comprised of heat from the fourth heat transfer and the fifth heat transfer.

18. The method of claim 16 where the process gas stream is a shifted syngas stream from a water-gas-shift reactor, and an Integrated Gasification Combined Cycle powered by at least a portion of the CO2-depleted gas stream produces generated steam, and including indirectly transferring heat from a portion of the generated steam to the capture reactor, such that the second heat transfer is comprised of heat from the portion of the generated steam.

19. A method of separating CO2 from a shifted syngas stream comprised of CO2, H2O and H2 in an adsorption/desorption cycle using a zeolite sorbent, where the desorption cycle is conducted under conditions of increased temperature and increased CO2 pressure to produce a final CO2 stream at high pressure, comprising: Generating the shifted syngas stream at a shifted syngas temperature greater than 120 degrees Celsius in a WGS reactor;Cooling the shifted syngas stream to a first temperature, where the first temperature is less than the shifted syngas temperature and at least 120 degrees Celsius, by transferring heat from the shifted syngas stream, such that the shifted syngas stream has a first CO2 pressure at the first temperature;Contacting the shifted syngas stream with the zeolite sorbent at the first temperature and the first CO2 pressure in a capture reactor, such that the zeolite sorbent adsorbs some portion of the CO2 and some portion of the H2O from the shifted syngas stream, and transferring heat from the zeolite sorbent with a first heat transfer to maintain the zeolite sorbent at the first temperature, thereby producing a loaded zeolite sorbent, and generating an H2 gas stream from the capture reactor, where the H2 gas stream is comprised of the shifted syngas stream less the some portion of the CO2 and the some portion of the H2O adsorbed by the zeolite sorbent;generating steam having a steam temperature greater than 275 degrees Celsius using an Integrated Gasification Combined Cycle powered by at least a portion of the H2 gas stream;transferring the loaded zeolite sorbent from the capture reactor to a regeneration reactor, where the regeneration reactor contains a CO2 atmosphere, where the CO2 atmosphere is comprised of at least 90 mol % CO2 and where the CO2 atmosphere has a second CO2 pressure greater than the first CO2 pressure, and where the second CO2 pressure is at least 225 psig;increasing and maintaining the temperature of the loaded zeolite sorbent in the regeneration reactor at a second temperature, where the second temperature exceeds the first temperature and the second temperature is at least 275 degrees Celsius and the second temperature is less than the steam temperature, by transferring heat indirectly to the loaded zeolite sorbent from the steam with a second heat transfer, thereby producing desorbed CO2 and H2O from the loaded zeolite sorbent and producing an unloaded zeolite sorbent;transferring the unloaded zeolite sorbent from the regeneration reactor to the capture reactor, and cooling the unloaded zeolite sorbent to the first temperature by transferring heat from the unloaded zeolite sorbent;Generating an output gas stream from the regeneration reactor, where the output gas stream is comprised of some portion of the CO2 atmosphere and some portion of the desorbed CO2 and H2O, and cooling the output gas stream to a third temperature below the first temperature and removing some portion of the H2O in the output gas stream;Splitting the output gas stream at the third temperature into a regeneration gas stream and a final CO2 stream; andHeating the regeneration stream with a third heat transfer, where the third heat transfer is comprised of heat from the transferring heat from the shifted syngas stream and heat from the transferring heat from the unloaded zeolite sorbent, and directing the regeneration gas stream to the regeneration reactor, such that the CO2 atmosphere is comprised of CO2 from the regeneration stream,

20. The method of claim 19 where the shifted syngas temperature further exceeds 200 degrees Celsius and the second temperature further exceeds 330 degrees Celsius.