Patent Publication Number: US-8529664-B2

Title: Removal of a target gas from a mixture of gases by swing adsorption with use of a turboexpander

Description:
CROSS REFERENCE TO RELATED APPLICATION 
     This Non-Provisional Application claims the benefit of U.S. Provisional Application No. 60/930,827 filed May 18, 2007. 
    
    
     FIELD OF THE INVENTION 
     The present invention relates to the separation of a target gas from a high pressure gas mixture containing said target gas and a product gas using a swing adsorption process unit. A turboexpander is used upstream of the swing adsorber to reduce the pressure of the high pressure gas mixture. A compressor is optionally used downstream of the swing adsorber to increase the pressure of the resulting target gas-containing stream for injecting into a subterranean formation or to increase the pressure of the product gas. 
     BACKGROUND OF THE INVENTION 
     Gas separation is important in various industries and can typically be accomplished by flowing a mixture of gases over an adsorbent that preferentially adsorbs a more readily adsorbed component relative to a less readily adsorbed component of the mixture. One of the more important gas separation techniques is pressure swing adsorption (PSA). PSA processes rely on the fact that under pressure gases tend to be adsorbed within the pore structure of a microporous adsorbent material or within the free volume of a polymeric material. The higher the pressure, the more gas is adsorbed. When the pressure is reduced, the gas is released, or desorbed. PSA processes can be used to separate gases in a mixture because different gases tend to fill the micropore or free volume of the adsorbent to different extents. If a gas mixture, such as natural gas, for example, is passed under pressure through a vessel containing polymeric or microporous adsorbent that fills with more nitrogen than it does methane, part or all of the nitrogen will stay in the adsorbent bed, and the gas coming out of the vessel will be enriched in methane. When the adsorbent bed reaches the end of its capacity to adsorb nitrogen, it can be regenerated by reducing the pressure, thereby releasing the adsorbed nitrogen. It is then ready for another cycle. 
     Another important gas separation technique is temperature swing adsorption (TSA). TSA processes also rely on the fact that under pressure gases tend to be adsorbed within the pore structure of a microporous adsorbent material or within the free volume of a polymeric material. When the temperature of the adsorbent is increased, the gas is released, or desorbed. By cyclically swinging the temperature of adsorbent beds, TSA processes can be used to separate gases in a mixture when used with an adsorbent that selectively picks up one or more of the components in the gas mixture. 
     Adsorbents for PSA systems are usually very porous materials chosen because of their large surface area. Typical adsorbents are activated carbons, silica gels, aluminas and zeolites. In some cases a polymeric material can be used as the adsorbent material. Though the gas adsorbed on the interior surfaces of microporous materials may consist of a layer only one, or at most a few molecules thick, surface areas of several hundred square meters per gram enable the adsorption of a significant portion of the adsorbent&#39;s weight in gas. 
     Different molecules can have different affinities for adsorption into the pore structure or open volume of the adsorbent. This provides one mechanism for the adsorbent to discriminate between different gases. In addition to their affinity for different gases, zeolites and some types of activated carbons, called carbon molecular sieves, may utilize their characteristics to exclude or slow the diffusion of some gas molecules into their structure. This provides a mechanism for selective adsorption based on the size of the molecules and usually restricts the ability of the larger molecules to be adsorbed. Either of these mechanisms can be employed to selectively fill the micropore structure of an adsorbent with one or more species from a multi-component gas mixture. The molecular species that selectively fill the micropores or open volume of the adsorbent are typically referred to as the “heavy” components and the molecular species that do not selectively fill the micropores or open volume of the adsorbent are usually referred to as the “light” components. 
     An early teaching of a PSA process having a multi-bed system is found in U.S. Pat. No. 3,430,418 wherein a system having at least four beds is described. This &#39;418 patent describes a cyclic PSA processing sequence that includes in each bed: (1) higher pressure adsorption with release of product effluent from the product end of the bed; (2) co-current depressurization to intermediate pressure with release of void space gas from the product end thereof; (3) countercurrent depressurization to a lower pressure; (4) purge; and (5) repressurization. The void space gas released during the co-current depressurization step is commonly employed for pressure equalization purposes and to provide purge gas to a bed at its lower desorption pressure. Another conventional PSA processes using three sorbent beds is disclosed in U.S. Pat. No. 3,738,087. Conventional PSA processes are typically able to recover only one of the key components (i.e., light or heavy) at high purity and are unable to make a complete separation and separate both components with a high recovery. The light component usually has a low recovery factor. Recovery of the light component usually drops even lower when the feed gas is introduced at higher pressures (i.e., pressures above 500 psig). 
     While there are various teachings in the art with respect to new adsorbent materials, new and improved parallel channel contactors, and improved rapid cycle PSA equipment, none of these to date present a viable solution to the problem of producing good recovery of the light component and purity when the feed gas is at very high-pressure. This is a critical issue since natural gas is often produced at high pressures (500-7000 psi) and methane acts as a light component in the adsorption process. One problem in extending PSA processes to high pressures, especially with those streams containing large amounts of CO 2 , is that at the end of the adsorption step there can be more moles of gas in the flow channels and mesopores then there are in the microporous sorbent. This can lead to poor recovery of desired product and also to low purity product streams. 
     Another problem can be that at high pressures the isotherm of an adsorbent saturates. When the isotherm saturates, the amount of material adsorbed changes slowly with increasing pressure. The slope of the isotherm, as a function of pressure, can be less than 1/100 of the slope of the isotherm at low pressures. This low slope decreases the effectiveness of the adsorbent, lowering recovery and decreasing the purity of the components recovered. 
     Many gas fields also contain significant levels of H 2 O, H 2 S, CO 2 , N 2 , mercaptans and/or heavy hydrocarbons that have to be removed to various degrees before the gas can be transported to market. It is preferred that as much of the acid gases such as H 2 S and CO 2  be removed from natural gas as possible. In all natural gas separations, methane is a valuable component and acts as a light component in swing adsorption processes. Small increases in recovery of this light component can result in significant improvements in process economics and also serve to prevent unwanted resource loss. It is desirable to recover more than 80 vol %, preferably more than 90 vol % of the methane when detrimental impurities are removed. While various processes exist for removing CO 2 , H 2 S, and N 2  from natural gas, there remains a need for processes and materials that will perform this recovery more efficiently, at lower costs, and at higher hydrocarbon yields, particularly at higher methane yields. For example, purification of high CO 2  content natural gas using PSA technologies is challenging because of: 1) the large volume of gas that must be processed; 2) the fact that all conventional adsorbents preferentially adsorb CO 2 ; 3) the presence of impurities such as H 2 S, water, and higher hydrocarbons; 4) the very high pressures that makes minimization of voidage and dead spaces of the adsorbent critical; and 5) the fugacity of CO 2  that significantly affects the physics of high-pressure adsorption and transport in microporous materials. 
     Therefore, there remains a need in the art for the purification of high pressure gaseous streams, such as high-pressure natural gas streams containing significant amounts of CO 2 . 
     SUMMARY OF THE INVENTION 
     In accordance with an embodiment of the present invention there is provided a process for removing a target gas component from a gas mixture containing said target gas component and a product gas component, which process comprises: 
     a) conducting said gas mixture to a turboexpander wherein the volume of said gas mixture is expanded, thereby lowering its pressure; 
     b) conducting said lowered pressure gas mixture from said turboexpander to a swing adsorption gas separation unit wherein the gas separation unit contains an adsorbent contactor comprised of an effective microporous adsorbent material for removing at least a portion of said target gas component from said gas mixture by adsorbing at least a portion of said target gas component onto said adsorbent material; 
     c) producing a product gas stream with a lower mol % of said target gas component than said gas mixture and a higher mol % of said product gas component than said gas mixture; 
     d) collecting said the product gas stream; 
     e) desorbing at least a portion of the adsorbed target gas component from said adsorbent material, thereby resulting in a waste gas stream which has a higher mol % of said target gas component than said gas mixture; and 
     f) collecting said waste gas stream. 
     In a preferred embodiment, the product gas component is CH 4  and the gas mixture is comprised of natural gas. 
     In another preferred embodiment, the product gas component is CH 4  and greater than about 90 mol % of the CH 4  in the gas mixture is recovered in the product gas stream. 
     In another preferred embodiment, the target gas component is CO 2    
    
    
     
       BRIEF DESCRIPTION OF THE FIGURES 
         FIG. 1  hereof is a schematic diagram of an integrated process utilizing a turboexpander and a PSA process of the present invention. 
         FIG. 2  hereof is a representation of one embodiment of a parallel channel contactor of the present invention in the form of a monolith directly formed from the microporous adsorbent of the present invention and containing a plurality of parallel channels. 
         FIG. 3  hereof is a cross-sectional representation along the longitudinal axis of the monolith of  FIG. 2 . 
         FIG. 4  hereof is a representation of a magnified section of the cross-sectional view of the monolith of  FIG. 2  showing the detailed structure of the adsorbent layer along with utilizing a blocking agent for occupying some of the mesopores and macropores. 
         FIG. 5  hereof represents another embodiment of the present invention in which the parallel channel contactor is in the form of a coated monolith for TSA applications where the adsorbent layer is coated onto the channel walls of a preformed monolith. 
         FIG. 6  hereof is a representation of a parallel channel contactor of the present invention in the form of an array of hollow fibers. 
         FIG. 7  hereof is yet another representation of a parallel channel contactor of the present invention but in the form of a hollow fiber contactor for TSA applications. 
         FIG. 8  hereof is another representation of a hollow fiber contactor for TSA applications as shown in  FIG. 7  but with the outer surfaces of the housing for the contactor rendered transparent. Dotted lines are used to indicate the edges of the outer surface. 
         FIG. 9  hereof is a representation of an embodiment of the present invention wherein the parallel contactor is of the laminate type. 
         FIG. 10  hereof is a schematic diagram of a preferred five step PSA/RCPSA process for treating a stream containing about 20 vol % CO 2  and about 80 vol % CH 4 . 
         FIG. 11  hereof is a schematic diagram of a preferred five step PSA/RCPSA process for treating a stream containing about 2 vol % N 2  and about 98 vol % CH 4 . 
     
    
    
     DETAILED DESCRIPTION OF THE INVENTION 
     Improvements in the recovery of the light component from a gas mixture are especially important for processes used to remove impurities from natural gas streams; particularly high pressure natural gas streams. The light component is taken to be the species, or molecular component or components, that are not preferentially taken up by the adsorbent in the adsorption step of the process. These light components form the product gas stream. Similarly, a heavy component is taken to be the species, or molecular component or components, that are preferentially taken up by the adsorbent in the adsorption step of the process. These heavy components are also referred to as target components, or gases. In natural gas processing, it is desirable to separate the impurities (heavy components or target components) and recover the methane-rich product (light component) stream at as high a pressure as practical for operability in natural gas processing. The present invention is directed to swing adsorption processes for removing a target gas from a high-pressure gas mixture stream containing at least one target gas and at least one product gas. 
     Natural gas streams that must be treated or separated occur at relatively high pressures. The term “high-pressure”, as used for the gaseous mixture to be treated herein ranges from about 500 to about 7,000 psi, preferably from about 1,000 to about 5,000 psi. Preferred gaseous streams to be treated in accordance with the present invention are natural gas streams containing at least about 5 vol %, preferably at least about 30 vol %, and more preferably greater than about 50 vol % of contaminants. Non-limiting examples of contaminants that are typically found in raw natural gas streams include water, condensates (higher molecular weight organics), ethane, propane, butane, CO 2 , N 2 , He, H 2 S, Hg, and mercaptans. In a preferred embodiment of the process streams utilized in the current invention, more than about 50 vol % of the contaminants is CO 2 . In order to overcome problems associated with conventional swing adsorption processes when processing high-pressure gaseous streams, the practice of the instant invention employs a turboexpander upstream of a swing adsorption process unit. In a preferred embodiment, a compressor is also utilized in the current process to compress the target gas enriched steam for disposal/sequestration or injection into a subterranean formation. The turboexpander is used upstream of the swing adsorption step in order to expand the volume of gas which reduces its pressure of the feed mixed gaseous stream to the point where a favorable regime in the adsorption isotherm can be accessed and the density of the molecules in the gas phase does not significantly affect the performance of the swing adsorption process. A turboexpander, which is also sometimes referred to as an expansion turbine or jet expander, refers to a centrifugal or axial flow turbine through which a high-pressure gas is expanded to produce work, that is typically used to drive a compressor. The expansion of the high-pressure gas significantly lowers its pressure. The heart of a turboexpander is a composite metal shaft that has a compressor wheel attached to one end of the shaft and an expander wheel attached to the other end of the shaft. Each wheel is contained completely separate from the other. A sealing system along the common shaft is used to prevent the process fluids present at each wheel from coming in contact from leakage along the shaft. The sealing systems are usually both mechanical and hydraulic in nature although some systems use a gas (seal gas) purge. The advantage of using a gas seal system is that sealing fluids do not leak into and accumulate in downstream equipment. Turboexpanders are well known in other art and thus a more detailed description is not needed herein. 
     Various types swing adsorption can be used in the practice of the present invention. Non-limiting examples of such swing adsorption processes include thermal swing adsorption (TSA) and various types of pressure swing adsorption processes including conventional pressure swing adsorption (PSA), and partial pressure swing or displacement purge adsorption (PPSA) technologies. These swing adsorption processes can be conducted with rapid cycles, in which case they are referred to as rapid cycle thermal swing adsorption (RCTSA), rapid cycle pressure swing adsorption (RCPSA), and rapid cycle partial pressure swing or displacement purge adsorption (RCPPSA) technologies. The term swing adsorption processes shall be taken to include all of these processes (i.e. TSA, PSA, PPSA, RCTSA, RCPSA, and RCPPSA) including combinations of these processes. Such processes require efficient contact of a gas mixture with a solid adsorbent material. 
     Although any suitable adsorbent contactor can be used in the practice of the present invention, including conventional adsorbent contactors, it is preferred that structured parallel channel contactors disclosed herein be utilized. The structure of parallel channel contactors, including fixed surfaces on which the adsorbent or other active material is held, provides significant benefits over previous conventional gas separation methods, such as vessels containing adsorbent beads or extruded adsorbent particles. It is possible to significantly improve the recovery percentage of the light component, or product gas, of a gas mixture by use of the present invention. With the preferred contactors of the present invention, it has been unexpectedly discovered that total recovery of the light component achieved in the swing adsorption process can be greater than about 80 vol %, more preferably greater than about 85 vol %, even more preferably greater than about 90 vol %, and most preferably greater than about 95 vol % of the content of the light component introduced into the process. Recovery of the light component is defined as the time averaged molar flow rate of the light component in the product stream divided by the time averaged molar flow rate of the light component in the feedstream. Similarly, recovery of the heavy component (target gas) is defined as the time averaged molar flow rate of the heavy component in the product stream divided by the time averaged molar flow rate of the heavy component in the feedstream. 
     The preferred structured adsorbent contactors of the present invention contain a very low volume fraction of open mesopores and macropores. That is, the structured bed adsorbent contactors of the present invention contain less than about 20 vol %, preferably less than about 15 vol %, more preferably less than about 10 vol %, and most preferably less than about 5 vol % of their pore volume in open pores in the mesopore and macropore size range. Mesopores are defined by the IUPAC to be pores with sizes in the 20 to 500 angstrom size range. Macropores are defined herein to be pores with sizes greater than about 500 Angstroms and less than about 1 micron. Because the flow channels are larger than about 1 micron in size, they are not considered to be part of the macropore volume. By open pores we mean mesopores and macropores that are not occupied by a blocking agent and that are capable of being occupied, essentially non-selectively, by components of a gas mixture. Different test methods as described below are to be used to measure the volume fraction of open pores in a contactor depending on the structure of the contactor. 
     The preferred test for determining the volume fraction of open mesopores and macropores of the contactor is defined as follows and involving an analysis of the isotherm of a condensable vapor adsorbed by the contactor. A liquid which has a vapor pressure greater than about 0.1 torr at the temperature of the test is a material that can be used to produce a condensable vapor. At about 20° C., water, hexane, trimethlybenzene, toluene, xylenes, and isooctane have sufficiently high vapor pressures that they can be used as condensable vapors. In the adsorption branch of the isotherm, capillary condensation fills empty micropore, mesopore, and much of the empty macropore volume with liquid. During desorption, micropores, mesopores, and macropores pores filled with liquid are emptied. It is well known that there is a hysteresis between the adsorption and desorption branches of the isotherm. Detailed analysis of the adsorption isotherm relies in part on the Kelvin equation which is well known to those skilled in the art. The detailed analysis provides a measurement of the volume fraction of the mesopores and macropores in the structured adsorbent and to some extent the size distribution of open mesopores and macropores. 
     If a liquid blocking agent is not used in the contactor of the present invention then the procedure used to measure the volume of open mesopores and macropores of the contactor is the same as that disclosed in co-pending U.S. Provisional Patent Application No. 60/930,827, filed May 18, 2007, which is incorporated herein by reference. 
     Although the open pore volume for the contactor is determined by the test procedure described above, scanning electron microscopy may be used to further confirm the relative volume of mesopores and macropores in the sample. When scanning electron microscopy is used the surface as well as a cross section of the contactor should be imaged. 
     It will be understood that the term PSA, unless preceded by the term “conventional” or “rapid cycle” refers collectively to all pressure swing adsorption processes including conventional PSA, RCPSA and PPSA. In PSA processes, a gaseous mixture is conducted under pressure for a period of time over a first bed of a solid sorbent that is selective, or relatively selective, for one or more components, usually regarded as a contaminant, that is to be removed from the gaseous mixture. 
     Unless otherwise noted, the term “selectivity” as used herein is based on binary (pairwise) comparison of the molar concentration of components in the feed stream and the total number of moles of these components adsorbed by the particular adsorbent during the adsorption step of the process cycle under the specific system operating conditions and feedstream composition. For a feed containing component A, component B, as well as additional components, an adsorbent that has a greater “selectivity” for component A than component B will have at the end of the adsorption step of the swing adsorption process cycle a ratio:
 
 U   A =(total moles of  A  in the adsorbent)/(molar concentration of  A  in the feed)
 
that is greater than the ratio:
 
 U   B =(total moles of  B  in the adsorbent)/(molar concentration of  B  in the feed)
 
Where U A  is the “Adsorption Uptake of component A” and U B  is the “Adsorption Uptake of component B”.
 
     Therefore for an adsorbent having a selectivity for component A over component B that is greater than one:
 
Selectivity= U   A   /U   B (where  U   A   &gt;U   B ).
 
     During the adsorption step, heavy components are selectively adsorbed and the weakly adsorbed components pass through the bed to form the product gas. It is possible to remove two or more contaminants simultaneously but for convenience, the component or components, that are to be removed by selective adsorption will be referred to in the singular and referred to as a contaminant or heavy component. In the PSA process, the gaseous mixture is passed over a first adsorption bed in a first vessel and a light component enriched product stream emerges from the bed depleted in the contaminant, or heavy component, which remains sorbed in the bed. After a predetermined time or, alternatively when a break-through of the contaminant or heavy component is observed, the flow of the gaseous mixture is switched to a second adsorption bed in a second vessel for the purification to continue. While the second bed is in adsorption service, the sorbed contaminant, or heavy component is removed from the first adsorption bed by a reduction in pressure. In some embodiments, the reduction in pressure is accompanied by a reverse flow of gas to assist in desorbing the heavy component. As the pressure in the vessels is reduced, the heavy component previously adsorbed in the bed is progressively desorbed to a heavy component enriched product stream. When desorption is complete, the sorbent bed may be purged with an inert gas stream, e.g., nitrogen or a purified stream of process gas. Purging may also be facilitated by the use of a purge stream that is higher in temperature than the process feedstream. 
     After breakthrough in the second bed and after the first bed has been regenerated so that it is again ready for adsorption service, the flow of the gaseous mixture is switched back to the first bed, and the second bed is regenerated. The total cycle time is the length of time from when the gaseous mixture is first conducted to the first bed in a first cycle to the time when the gaseous mixture is first conducted to the first bed in the immediately succeeding cycle, i.e., after a single regeneration of the first bed. The use of third, fourth, fifth, etc. vessels in addition to the second vessel can serve to increase cycle time when adsorption time is short but desorption time is long. 
     Conventional PSA processes suffer from several inherent disadvantages. For example, conventional PSA units are typically more costly to build and operate and are significantly larger in size for the same amount of target gas that needs to be recovered from a target-gas containing gas stream, such as natural gas, as compared to RCPSA. Also, a conventional PSA unit will generally have cycle times in excess of about one minute, typically in excess of about 2 to 4 minutes due to time limitations required to allow diffusion of the components through the larger beds utilized in conventional PSA and the equipment configuration involved. In contrast, RCPSA generally has a total cycle times of less than one minute. The total cycle times of RCPSA may be less than about 30 seconds, preferably less than about 15 seconds, more preferably less than about 10 seconds, even more preferably less than about 5 seconds, and even more preferably less than about 1 second. Further, the rapid cycle pressure swing adsorption units can make use of substantially different sorbents, such as, but not limited to, structured materials such as monoliths, laminates, and hollow fibers. 
     RCPSA can enable a significant increase in process intensification (e.g., higher operating frequencies and gas flow velocities) when compared to conventional PSA. RCPSA typically utilizes a rotary valving system to conduct the gas flow through a rotary adsorber module that contains a number of separate adsorbent bed compartments or “tubes”, each of which is successively cycled through the sorption and desorption steps as the rotary module completes the cycle of operations. The rotary sorber module is normally comprised of multiple tubes held between two seal plates on either end of the rotary sorber module wherein the seal plates are in contact with a stator comprised of separate manifolds wherein the inlet gas is conducted to the RCPSA tubes and the processed purified product gas and the tail gas exiting the RCPSA tubes are conducted away from the rotary sorber module. By suitable arrangement of the seal plates and manifolds, a number of individual compartments or tubes may pass through the characteristic steps of the complete cycle at any given time. In contrast, with conventional PSA, the flow and pressure variations, required for the RCPSA sorption/desorption cycle, changes in a number of separate increments on the order of seconds per cycle, which smoothes out the pressure and flow rate pulsations encountered by the compression and valving machinery. In this form, the RCPSA module includes valving elements angularly spaced around the circular path taken by the rotating sorption module so that each compartment is successively passed to a gas flow path in the appropriate direction and pressure to achieve one of the incremental pressure/flow direction steps in the complete RCPSA cycle. One key advantage of the RCPSA technology is a significantly more efficient use of the adsorbent material. The quantity of adsorbent required with RCPSA technology can be reduced to a fractional volume of that required for conventional PSA technology to achieve the same separation quantities and qualities. As a result, the footprint, investment, and the amount of active adsorbent required for RCPSA is typically significantly lower than that for a conventional PSA unit processing an equivalent amount of gas. 
     The present invention may be used in PPSA, RCPSA or hybrid PPSA or RCPPSA processes where a gas or liquid is purged through the bed to help desorb molecules. In a PPSA process, desorption of the adsorbed species is accomplished by passing a gas or liquid through the contactor to desorb molecules taken up during an adsorption step. An example of a gas that may be used is steam. In hybrid PPSA processes, the desorption of molecules from the contactor is accomplished by use of a thermal or pressure swing and part of the desorption is accomplished with a purge. 
     Improvements in the recovery of the light component are especially important for processes used to remove impurities from natural gas streams, particularly high pressure natural gas streams. It is desirable to recover the impurities (heavy components) and the methane-rich product (light component) streams at as high a pressure as practical for operability in natural gas processing. As previously mentioned, the present invention can be used to obtain methane recovery of greater than about 80 mol %, more preferably greater than about 85 mol %, even more preferably greater than about 90 mol %, and most preferably greater than about 95 mol %, even when the natural gas is fed at high pressures, such as at pressures in excess of about 500 psig, preferably at pressure in excess of about 1,000 psig, more preferably at pressures in excess of about 2,000 psig and most preferably in excess of about 2,500 psig. The present invention can be used even when the gas stream is at an exceptionally high pressure of up to about 7,000 psig. The composition of natural gas streams directly from an underground field (raw natural gas) will vary from field to field. Non-limiting examples of components that comprise a raw natural gas stream include water, condensates (higher molecular weight organics), methane, ethane, propane, butane, CO 2 , N 2 , He, H 2 S, Hg, and mercaptans. Water and condensates are typically removed and the condensates sent to a petroleum refinery. In order to produce a gas that can be introduced into a pipeline for sale to residential and commercial fuel markets contaminants, such as N 2 , Hg, mercaptans, and the acid gases CO 2  and H 2 S must to removed to acceptable levels. The levels and impurity types vary from gas field to gas field and in some cases can comprise the majority of molecules in the raw natural gas stream. For example, it is not uncommon for natural gas fields to contain from about 5 mol % to about 90 mol % CO 2 , more typically from about 10 mol % to about 70 mol % CO 2 . 
     The present invention also provides a method to increase recovery of the light component by conditioning the temperature and pressure of gas fed to the contactor. This method can be used with or without a contactor having a low volume fraction of mesopores and macropores. During the adsorptive step of well designed kinetically controlled swing adsorption processes, the amount of heavy component in the micropores or free volume can be approximately computed from the adsorption isotherm of the heavy component in equilibrium with its local gas phase concentration in the contactor. In well designed equilibrium controlled swing adsorption processes the amount of heavy component in the micropores or free volume can be approximately computed from the competitive adsorption isotherm of the heavy and light components in equilibrium with their local gas phase concentration in the contactor. These approximations are possible because in well designed swing adsorption processes, the contactor provides good mass transfer characteristics between the gas phase and the adsorbed phase in the micropores or free volume of the contactor. The maximum attainable loading of the heavy component in the macropores or free volume of the contactor is called q s  (units for q s  are milli-mole/m 3  of the microporous or polymeric material). At low pressures the adsorption isotherm for the heavy component usually obeys Henry&#39;s Law and the amount of heavy component adsorbed, q Heavy , in the microporous or polymeric material is
 
q Heavy =K Heavy P Heavy q s (in milli-mole/m 3 )
 
where K Heavy  is the Henry&#39;s constant and P Heavy  is the partial pressure of the heavy component. The Henry&#39;s constant, K Heavy  depends on temperature and usually varies according to the equation
 
               K   Heavy     =       K   0     ⁢       ⅇ       Δ   ⁢           ⁢   H     RT       ⁡     (     in   ⁢           ⁢     Pascals     -   1         )               
where K 0  is a pre-exponential factor and ΔH is the heat of adsorption (Joule/Mole).
 
     To improve selectivity and recovery for either a kinetically or equilibrium controlled swing adsorption processes the inlet temperature and pressure should be chosen such that at the end of the adsorption step the loading of the heavy component in the micropores or free volume near the point at which feed is introduced to the contactor should be greater than about 0.15 q s  and preferably greater than about 0.3 q s  and even more preferably greater than about 0.6 q s . This requirement places a lower bound on the inlet pressure and a maximum bound on the inlet temperature. With increasing loading of the heavy component in the micropores or free volume of the adsorbent the amount of material that is selectively adsorbed in the contactor is increased and the amount of material that can be selectively released in the desorption step is increased. These increases reduce the loss of the light component that is non-selectively adsorbed into the mesopores and macropores. Increasing the loading significantly beyond this range reduces the recovery of the light component because the slope of the adsorption isotherm tends to decrease with increasing pressure. To maximize the recovery of the light component it is also preferred that near the point at which feed is introduced to the contactor the slope of the adsorption isotherm for the heavy component be large enough so that 
                 ∂     q   Heavy         ∂     P   Heavy         &gt;     α   ⁢           ⁢     K   Heavy     ⁢           ⁢     q   s             
where α= 1/50, more preferably α= 1/25, and even more preferably α=⅛. This inequality places a maximum bound on the inlet pressure and a minimum bound on the inlet temperature. As such these requirements define a window (i.e., maxima and minima) for feed pressure and temperature in which the recovery of the light component is optimized. Usually it is preferred to operate the swing adsorption process at the lowest pressure within the operating window as is practical. As the feed pressure decreases, the concentration of molecules in the mesopores and macropores of the contactor decreases. Lower concentrations of molecules nonselectively adsorbed in the mesopores and macropores leads to lower losses of the light component in the swing adsorption process.
 
     This window is especially important in natural gas separations because some natural gas is usually produced at pressures ranging from 500 to 7,000 psi. These feed pressures are usually too high to fall within the optimum recovery window for methane which acts as a light component in swing adsorption separation. It is possible to reduce the feed pressure with a simple expansion nozzle, however this technique wastes energy. Practice of the present invention makes it possible to access the optimum light component recovery window for separations of most heavy components (such as CO 2 , N 2 , H 2 S, H 2 O, heavy hydrocarbons, and mercaptans) by preconditioning the natural gas with a turboexpander that recovers the energy from the gas expansion. Energy recovered from gas expansion can then be used for power generation or to recompress separated acid gas components (such as CO 2  or H 2 S) so that they can be disposed of in underground formations. Underground formations that are suitable for disposal/sequestration of CO 2  and H 2 S include aquifers that have a top seal that prevents significant loss of injected acid gas components, oil reservoirs, gas reservoirs, depleted oil reservoirs and depleted gas reservoirs. Typically the separated CO 2  and H 2 S has to be recompressed to pressures greater than about 2,000 psi and often to pressures greater than about 5,000 psi to be injected into these types of underground formations. Thus, it is preferable to be able to reuse energy recovered from a turboexpander for recompression. The cost of a turboexpander is also less than a gas fired turbine producing the same amount of power. As such, it is economically advantageous to use a turboexpander to capture energy from gas expansion used to condition natural gas for the optimum methane recovery window. With use of a turboexpander, the energy can either be recovered with a shaft coupled electric generator or with a shaft coupled compressor. It can be advantageous to pass the gas coming out of the turboexpander through a heat exchanger before introducing it into the swing adsorption process in order to access the operating window that maximizes methane recovery. Gas coming out of a turboexpander can be too cold to be in the optimum recovery window because the work is recovered in an isentropic expansion. Typically a heat exchanger will be run so that the gas temperature is increased before entering a swing adsorption process. These considerations are especially important when the swing adsorption is a PSA or RCPSA process. 
     In applications where CO 2  is removed from natural gas in swing adsorption processes it is preferred to formulate the adsorbent with a specific class of 8-ring zeolite materials that has a kinetic selectivity. The kinetic selectivity of this class of 8-ring zeolite materials allows CO 2  to be rapidly transmitted into zeolite crystals while hindering the transport of methane so that it is possible to selectively separate CO 2  from a mixture of CO 2  and methane. For the removal of CO 2  from natural gas, this specific class of 8-ring zeolite materials has a Si/Al molar ratio from about 2 to about 1,000, more preferably a Si/Al molar ratio from about 10 to about 500, and even more a Si/Al molar ratio from about 50 to about 300. It should be noted that as used herein, the term Si/Al is defined as the molar ratio of silica to alumina of the zeolitic structure. This preferred class of 8-ring zeolites that are suitable for use herein allow CO 2  to access the internal pore structure through 8-ring windows in a manner such that the ratio of single component diffusion coefficients of CO 2  and methane (i.e., D CO2 /D CH4 ) is greater than 10, preferably greater than about 50, and more preferably greater than about 100 and even more preferably greater than 200. 
     In many instances, nitrogen also has to be removed from natural gas or gas associated with the production of oil. In some cases this is because of the high nitrogen levels (&gt;2%) in the produced gas, and in other cases nitrogen removal is needed in order to liquefy natural gas. It may also be advantageous to separate nitrogen from flash gas that occurs in LNG production so that the methane and hydrocarbon products can be used as fuel. Another application is the purification of gas from LNG boil-off so that the methane and hydrocarbon products can be recovered or used as fuel. When recovered, it may be advantageous to re-liquefy the methane and hydrocarbon and returned them back to the LNG cargo. In all of these applications it is desirable to selectively adsorb the nitrogen over the methane in order to obtain high recovery of a purified methane product from a nitrogen containing gas. There have been very few molecular sieve sorbents with significant equilibrium or kinetic selectivity for nitrogen separation from methane. For N 2  separation from natural gas it is also preferred to formulate the adsorbent with a class of 8-ring zeolite materials that has a high kinetic selectivity. The kinetic selectivity of this class of 8-ring materials allows N 2  to be rapidly transmitted into zeolite crystals while hindering the transport of methane so that it is possible to selectively separate N 2  from a mixture of N 2  and methane. For the removal of N 2 , from natural gas, this specific class of 8-ring zeolite materials also has a Si/Al molar ratio from about 2 to about 1,000, preferably a Si/Al molar ratio from about 10 to about 500, and even more preferably a Si/Al molar ratio from about 50 to about 300. This preferred class of 8-ring zeolites that are suitable for use herein allow N 2  to access the internal pore structure through 8-ring windows in a manner such that the ratio of single component diffusion coefficients of N 2  and methane (i.e., D N2 /D CH4 ) is greater than 5, preferably greater than about 20, and more preferably greater than about 50 and even more preferably greater than 100. Resistance to fouling in swing adsorption processes during the remove N 2  from natural gas is another advantage offered by this class of 8-ring zeolite materials. 
     In other instances, it is also desirable to remove H 2 S from natural gas which can contain from about 0.001 mol % H 2 S to about 70 mol % H 2 S. In this case, it can be advantageous to formulate the adsorbent with stannosilicates as well as the aforementioned class of 8-ring zeolites that has kinetic selectivity. The kinetic selectivity of this class of 8-ring materials allows H 2 S to be rapidly transmitted into zeolite crystals while hindering the transport of methane so that it is possible to selectively separate H 2 S from a mixture of H 2 S and methane. For the removal of H 2 S, from natural gas, this specific class of 8-ring zeolite materials has a Si/Al molar ratio from about 2 to about 1,000, preferably a Si/Al molar ratio from about 10 to about 500, and more preferably a Si/Al molar ratio from about 50 to about 300. This preferred class of 8-ring zeolites that are suitable for use herein allow H 2 S to access the internal pore structure through 8-ring windows in a manner such that the ratio of single component diffusion coefficients of H 2 S and methane (i.e., D H2S /D CH4 ) is greater than about 5, preferably greater than about 20, and more preferably greater than about 50 and even more preferably greater than about 100. DDR, Sigma-1, and ZSM-58 are also suitable for the removal of H 2 S from natural gas. In some applications the H 2 S has to be removed to the ppm or sub ppm levels. To achieve such extensive removal of H 2 S it can be advantageous to use a PPSA or RCPPSA process. 
     It is sometimes necessary to remove heavy hydrocarbons, as previously defined, from natural gas or gas associated with the production of oil. Heavy hydrocarbon removal may be necessary for dew point conditioning before the natural gas is shipped via pipeline or to condition natural gas before it is liquefied. In other instances it may be advantageous to recover heavy hydrocarbons from produced gas in enhanced oil recovery (EOR) floods that employ CO 2  and nitrogen. In still other instances it may be advantageous to recover heavy hydrocarbons from associated gas that is cycled back into an oil reservoir during some types of oil production. In many instances where it is desirable to recover heavy hydrocarbons, the gas can be at pressures in excess of about 1,000 psi and in some instances the gas pressure can be in excess of about 5,000 psig, even sometimes in excess of about 7,000 psig. It is advantageous in these applications to use an adsorbent formulated with a zeolite having a pore size between about 5 and about 20 angstroms. Non-limiting examples of zeolites having pores in this size range are MFI, faujasite, MCM-41 and Beta. It is preferred that the Si/Al molar ratio of zeolites utilized in an embodiment of a process of the present invention for heavy hydrocarbon removal be from about 20 to about 1,000, more preferably a Si/Al molar ratio from about 200 to about 1000 in order to prevent excessive fouling of the adsorbent. 
     In some instances, natural gas is produced with mercaptans present and it is advantageous to use adsorption processes to aid in their separation. Streams containing mercaptans and components found in natural gas are present in several processes that have been developed to purify natural gas. It is possible to more selectively separate mercaptans from natural gas or natural gas components and increase the recovery of the valuable components (such as methane) using the contactors of the present invention. It is advantageous in these applications to also use an adsorbent formulated with a zeolite having a pore size between about 5 and about 20 angstroms. Non-limiting examples of zeolites having pores in this size range are MFI, faujasite, MCM-41 and Beta. In these applications the Si/Al molar ratio of the zeolite can be from about 1 to about 1000. 
     The low mesoporous and macroporous adsorbent is an integral component of the preferred contactors of the present invention that can be used in both equilibrium and kinetically controlled swing adsorption processes to improve light component product recovery. Conventional adsorbent contactors contain significant levels of mesopores and macropores. At the end of the adsorption step, the mesopores and macropores, which are non-selective, will contain significant amounts of light components because transport into the mesopores and macropores is nonselective. This is an especially important problem in high pressure RCPSA, PSA, TSA and PPSA processes because at the end of the adsorption step the number of molecules in the mesopore and macropore spaces can be comparable to the number of molecules selectively adsorbed in the micropores of the adsorbent. In the desorption step most of the light components contained in the mesopores and macropores are undesirably lost to the heavy component product stream. As such, these light molecules are not recovered as desired with the light product. This can result in significant loss of valuable light product. The preferred adsorbent contactors of the present invention can significantly improve this recovery of light products by reducing the volume fraction of the open mesopore and macropore spaces. 
     In one embodiment of the present invention, the walls of the open flow parallel channels are comprised of the adsorbent. The adsorbent is preferably a microporous adsorbent or polymer that selectively adsorbs the heavy components. Non-limiting examples of microporous adsorbents include 8-ring zeolites, titanosilicates, ferrosilicates, stannosilicates, aluminophosphates (AlPOs), silicaaluminophosphates (SAPOs) and carbon molecular sieves. Preferred are zeolites for the removal of CO 2 , N 2 , and H 2 S with the stannosilicates being more preferred for the removal of H 2 S. When zeolites are used, it is preferred to use high Si/Al molar ratio zeolites to form at least part of the adsorbent because they are more tolerant of strongly adsorbed foulants. Non-limiting examples of polymers that can be used as selective adsorbents include polyimides, polysulfones, and functionalized polymers such as amine functionalized polymers. 
     The preferred adsorbent contactors of the present invention may optionally contain a thermal mass (heat transfer) material to help control heating and cooling of the adsorbent of the contactor during both the adsorption step and desorption step of a pressure swing adsorption process. Heating during adsorption is caused by the heat of adsorption of molecules entering the adsorbent. The optional thermal mass material also helps control cooling of the contactor during the desorption step. The thermal mass can be incorporated into the flow channels of the contactor, incorporated into the adsorbent itself, or incorporated as part of the wall of the flow channels. When it is incorporated into the adsorbent, it can be a solid material distributed throughout the adsorbent layer or it can be included as a layer within the adsorbent. When it is incorporated as part of the wall of the flow channel, the adsorbent is deposited or formed onto the wall. Any suitable material can be used as the thermal mass material in the practice of the present invention. Non-limiting examples of such materials include metals, ceramics, and polymers. Non-limiting examples of preferred metals include steel alloys, copper, and aluminum. Non-limiting examples of preferred ceramics include silica, alumina, and zirconia. An example of a preferred polymer that can be used in the practice of the present invention is polyimide. Depending upon the degree to which the temperature rise is to be limited during the adsorption step, the amount of thermal mass material used can range from about 0 to about 25 times the mass of the microporous adsorbent of the contactor. A preferred range for the amount of thermal mass in the contactor is from about 0 to 5 times the mass of the microporous adsorbent of the contactor. A more preferred range for the amount of thermal mass material will be from about 0 to 2 times the mass of the microporous adsorbent material, most preferably from about 0 to 1 times the mass of the microporous material of the contactor. 
     Open mesopore and macropore volume includes the volume fraction of all mesopores and macropores that are not filled with a blocking agent, and that are non-selective and thus are capable of being occupied essentially by all components of the gas mixture. Non-limiting examples of blocking agents that can be used in the practice of the present invention include polymers, microporous materials, solid hydrocarbons, and liquids that can fill the open mesoporous and macroporous spaces but still allow molecules to transport into the micropores in the selective adsorbent. When the blocking agent is a polymer or liquid, it is preferred that the molecular size of the blocking agent be large enough so that is does not significantly invade micropores of the adsorbent, but not so large that it does not fill the mesopores and macropores. When solid blocking agents are used the particle size of the solid is greater than any selective micropores in the adsorbent but smaller than the meso and macropores. As such the blocking agent can fit into the meso and macropores without significantly occluding or filling micropores which may be present in the adsorbent. 
     The blocking agent fills the open meso and macropores of the adsorbent to an extent that the volume fraction of the open meso and macropores of the adsorbent meets the aforementioned requirements. Non-limiting examples of polymers that can be used as blocking agents include polyimides, polysulfones, and silicone rubbers. Non-limiting examples of liquids that can be used as blocking agents include amines, aromatics such as 1,3,5 trimethylbenzene and branched saturated hydrocarbons such a heptamethylnonane as well as liquid hydrocarbons having carbon numbers in the about 5 to about 60 range. When a liquid blocking agent is used it is advantageous to saturate, or nearly saturate, the feed gas with the liquid blocking agent. Non-limiting examples of solid blocking agents include hydrocarbons such as waxes and those having carbon numbers in the 10-1000 range. Non-limiting examples of microporous materials that can be used in the practice of the present invention include microporous carbons and zeolites having pore sizes larger than those of the selective structured adsorbent of this invention. An example of an adsorbent formulated with a blocking agent is a silica or alumina bound zeolite layer having about 30% mesoporous and macroporous volume in the interstices between the zeolite particles that is filled in with a liquid so that substantially all voids are filled with liquid (i.e., the total resulting macro and mesoporosity in the layer is less than about 20%). In some cases, the blocking agent forms a continuous network and the adsorbent is a composite structure with the microporous material embedded within the blocking agent. A non-limiting example of such a structure is a zeolite/polymer composite where the polymer is continuous and the composite has less than about 20 vol % in open mesopores and macropores. 
     It is also possible to formulate the adsorbent using a mesoporous material that fills the macropores to reduce the overall void, or open, volume. An example of such a structure would be an adsorbent having about 30 vol % of macropores that are filled in with a mesoporous sol gel so that the resulting mesopore and macropore volume is less than about 20 vol %. 
     The channels, also sometimes referred to as “flow channels” or “gas flow channels” are paths in the contactor that allow gas flow through. Generally, flow channels provide for relatively low fluid resistance coupled with relatively high surface area. Flow channel length should be sufficient to provide the mass transfer zone which is at least, a function of the fluid velocity, and the surface area to channel volume ratio. The channels are preferably configured to minimize pressure drop in the channels. In many embodiments, a fluid flow fraction entering a channel at the first end of the contactor does not communicate with any other fluid fraction entering another channel at the first end until the fractions recombine after exiting at the second end. It is important that there be channel uniformity to ensure that substantially all of the channels are being fully utilized, and that the mass transfer zone is substantially equally contained. Both productivity and gas purity will suffer if there is excessive channel inconsistency. If one flow channel is larger than an adjacent flow channel, premature product break through may occur, which leads to a reduction in the purity of the product gas to unacceptable purity levels. Moreover, devices operating at cycle frequencies greater than about 50 cycles per minute (cpm) require greater flow channel uniformity and less pressure drop than those operating at lower cycles per minute. Further, if too much pressure drop occurs across the bed, then higher cycle frequencies, such as on the order of greater than 100 cpm, are not readily achieved. 
     The dimensions and geometric shapes of the parallel channel contactors of the present invention can be any dimension or geometric shape that is suitable for use in swing adsorption process equipment. Non-limiting examples of geometric shapes include various shaped monoliths having a plurality of substantially parallel channels extending from one end of the monolith to the other; a plurality of tubular members; stacked layers of adsorbent sheets with and without spacers between each sheet; multi-layered spiral rolls, bundles of hollow fibers, as well as bundles of substantially parallel solid fibers. The adsorbent can be coated onto these geometric shapes or the shapes can, in many instances, be formed directly from the adsorbent material plus suitable binder. An example of a geometric shape formed directly from the adsorbent/binder would be the extrusion of a zeolite/polymer composite into a monolith. Another example of a geometric shape formed directly from the adsorbent would be extruded or spun hollow fibers made from a zeolite/polymer composite. An example of a geometric shape that is coated with the adsorbent would be a thin flat steel sheet that is coated with a microporous, low mesopore, adsorbent film, such as a zeolite film. The directly formed or coated adsorbent layer can be itself structured into multiple layers or the same or different adsorbent materials. Multi-layered adsorbent sheet structures are taught in United States Patent Application Publication No. 2006/0169142, which is incorporated herein by reference. 
     The dimensions of the flow channels can be computed from considerations of pressure drop along the flow channel. It is preferred that the flow channels have a channel gap from about 5 to about 1,000 microns, preferably from about 50 to about 250 microns. In some RCPSA applications, the flow channels are formed when adsorbent sheets are laminated together. Typically, adsorbent laminates for RCPSA applications have flow channel lengths from about 0.5 centimeter to about 10 meter, more typically from about 10 cm to about 1 meter and a channel gap of about 50 to about 250 microns. The channels may contain a spacer or mesh that acts as a spacer. For laminated adsorbents, spacers can be used which are structures or material, that define a separation between adsorbent laminates. Non-limiting examples of the type of spacers that can be used in the present invention are those comprised of dimensionally accurate: plastic, metal, glass, or carbon mesh; plastic film or metal foil; plastic, metal, glass, ceramic, or carbon fibers and threads; ceramic pillars; plastic, glass, ceramic, or metal spheres, or disks; or combinations thereof. Adsorbent laminates have been used in devices operating at PSA cycle frequencies up to at least about 150 cpm. The flow channel length may be correlated with cycle speed. At lower cycle speeds, such as from about 20 to about 40 cpm, the flow channel length can be as long as or longer than one meter, even up to about 10 meters. For cycle speeds greater than about 40 cpm, the flow channel length typically is decreased, and may vary from about 10 cm to about 1 meter. Longer flow channel lengths can be used for slower cycle PSA processes. Rapid cycle TSA processes tend to be slower than rapid cycle PSA processes and as such longer flow channel lengths can also be used with TSA processes. 
     The overall adsorption rate of the swing adsorption processes is characterized by the mass transfer rate from the flow channel into the adsorbent. It is desirable to have the mass transfer rate of the species being removed (i.e., the heavy component) high enough so that most of the volume of the adsorbent is utilized in the process. Since the adsorbent selectively removes the heavy component from the gas stream, inefficient use of the adsorbent layer can lower recovery of the light component and/or decrease the purity of the light product stream. With use of the present invention, it is possible to formulate an adsorbent with a low volume fraction of meso and macroporous such that most of the volume of the adsorbent, which will be in the microporous range, is efficiently used in the adsorption and desorption of the heavy component. One way of doing this is to have an adsorbent of substantially uniform thickness where the thickness of the adsorbent layer is set by the mass transfer coefficients of the heavy component and the time of the adsorption and desorption steps of the process. The thickness uniformity can be assessed from measurements of the thickness of the adsorbent or from the way in which it is fabricated. It is preferred that the uniformity of the adsorbent be such that the standard deviation of its thickness is less than about 25% of the average thickness. More preferably, the standard deviation of the thickness of the adsorbent is less than about 15% of the average thickness. It is even more preferred that the standard deviation of the adsorbent thickness be less than about 5% of the average thickness. 
     Calculation of these mass transfer rate constants is well known to those having ordinary skill in the art and may also be derived by those having ordinary skill in the art from standard testing data. D. M. Ruthven &amp; C. Thaeron,  Performance of a Parallel Passage Absorbent Contactor , Separation and Purification Technology 12 (1997) 43-60, which is incorporated herein by reference, clarifies many aspects of how the mass transfer is affected by the thickness of the adsorbent, channel gap and the cycle time of the process. Also, U.S. Pat. No. 6,607,584 to Moreau et al., which is also incorporated by reference, describes the details for calculating these transfer rates and associated coefficients for a given adsorbent and the test standard compositions used for conventional PSA. 
     A figure of merit for the mass transfer through the adsorbent layer is a time constant, τ a , for transport of the heavy component computed at each point in the adsorbent. For a planar adsorbent sheet with thickness in the x direction, and the y and z directions being in the plane of the sheet, the time constant τ a  of the heavy component is
 
τ a   [x,y,z ]=Minimum[ L   path   2   /D   path ](in seconds)
 
where D path  is the average transport diffusion coefficient of the heavy component along a path from the feed channel to the point (x,y,z) and L path  is the distance along the path. There are many possible trajectories or paths from the feed channel to each point (x,y,z) in the adsorbent. The time constant is the minimum of the possible time constants (L path   2 /D path ) along all possible paths from the feed channel to the (x,y,z) point in the adsorbent. This includes paths through meso and macropores. If there is a solid material in the adsorbent (such as that which may be included for heat management) there will be no transport within it and (x,y,z) points within it are not included in the computation. The transport diffusion coefficient of each species is taken to be the single component Stefan-Maxwell diffusion coefficient for each species. The average transport diffusion coefficient along the path, D path , is the linearly averaged diffusion coefficient along the path. A linear averaging is sufficient to provide a diffusion coefficient characterizing the path. When the heavy component has many species the diffusion coefficient, D path , is also compositionally averaged. The diffusion coefficient depends on temperature and it may depend on pressure as well. To the extent that the diffusion coefficient changes, it must be averaged for the temperature and pressure changes occurring during a cycle. For an adsorbent to be efficient, the averaged thickness of the adsorbent layer preferably is chosen such that the time constant for at least half the points (or volume) in the adsorbent that is not a dense solid is less than the cycle time of the process. More preferably, the average thickness of the adsorbent layer is chosen such that the time constant for at least about 75% of the points (or volume) in the adsorbent that is not a dense solid is less than the cycle time of the process. Even more preferably the average thickness of the adsorbent layer is chosen such that the time constant for at least about 75% of the points (or volume) in the adsorbent that is not a dense solid is less than about 25% of the cycle time of the process.
 
     The present invention can be applied to improve the separation of molecular species from synthesis gas. Synthesis gas can be produced by a wide variety of methods, including steam reforming of hydrocarbons, thermal and catalytic partial oxidation of hydrocarbons, and many other processes and combinations known in the art. Many of the processes used to produce synthesis gas (for example coal gasification) produce the gas at pressures in excess of about 1,000 psi and often in excess of about 1,500 psi. Synthesis gas is used in a large number of fuel and chemical applications, as well as power applications such as Integrated Gasification Combined Cycle (IGCC). All of these applications have a specification of the exact composition of the syngas required for the process. As produced, synthesis gas contains at least CO and H 2 . Other molecular components in the gas can be CH 4 , CO 2 , H 2 S, H 2 O, and N 2 . Minority (or trace) components in the gas can include hydrocarbons, NH 3  and NOx. In almost all applications most of the H 2 S has to be removed from the syngas before it can be used and in many applications it is desirable to remove much of the CO 2 . In applications where the syngas is used as a feedstock for a chemical synthesis process, it is generally desirable to adjust the H 2 /CO ratio to a value that is optimum for the process. In certain fuel applications, a water-gas shift reaction may be employed to shift the syngas almost entirely to H 2  and CO 2 , and in many such applications it is desirable to remove the CO 2 . 
     The present invention provides a method for increasing the recovery of the valuable molecular components from synthesis gas. In most applications valuable components are CO and H 2 . When multiple species are removed from the synthesis gas, individual contactors, each optimized for the removal of a particular component, can be used. Multiple contactors can be used because the invention provides a means of rapidly changing the pressure in the contactor allowing for rapid cycle operation and consequentially small equipment size. Alternatively several different adsorbents can be incorporated into a single contactor. This provides a means of selectively removing several species with a single contactor. 
     The contactors of the present invention can better be understood with reference to the Figures hereof.  FIG. 2  hereof is a representation of a parallel channel contactor of the present invention in the form of a monolith formed directly from a microporous adsorbent plus binder and containing a plurality of parallel flow channels. A wide variety of monolith shapes can be formed directly by extrusion processes. The cylindrical monolith  1  contains a plurality of parallel flow channels  3 . These flow channels  3  can have channel gaps from about 5 to about 1,000 microns, preferably from about 50 to about 250 microns, as long as all channels of a given contactor have substantially the same size channel gap. The channels can be formed having a variety of shapes including, but not limited to, round, square, triangular, and hexagonal. The space between the channels is occupied by the adsorbent  5 . As shown the channels  3  occupy about 25% of the volume of the monolith and the adsorbent  5  occupies about 75% of the volume of the monolith. The adsorbent  5  can occupy from about 50% to about 98% of the volume of the monolith. The effective thickness of the adsorbent can be defined from the volume fractions occupied by the adsorbent  5  and channel structure as: 
     
       
         
           
             
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     For the monolith of  FIGS. 2 and 3  hereof the effective thickness of the adsorbent will be about 1.5 times the feed channel gap. When the channel gap is in a range from about 50 to about 250 microns it is preferred that the thickness of the adsorbent layer, in the case wherein the entire contactor is not comprised of the adsorbent, be in a range from about 25 to about 2,500 microns. For a 50 micron channel gap, the preferred range of thickness for the adsorbent layer is from about 25 to about 300 microns, more preferred range from about 50 to about 250 microns. As utilized herein, the “channel gap” of a flow channel is defined as the length of a line across the minimum dimension of the flow channel as viewed orthogonal to the flow path. For instance, if the flow channel is circular in cross-section, then the channel gap is the internal diameter of the circle. However, if the channel gap is rectangular in cross-section, the flow gap is the distance of a line perpendicular to and connecting the two longest sides of the rectangular (i.e., the length of the smallest side of the rectangle). It should also be noted that the flow channels can be of any cross-sectional configuration. Preferred embodiments are wherein the flow channel cross-sectional configuration is either circular, rectangular or square. However, any geometric cross-sectional configuration may be used, such as but not limited to, ellipses, ovals, triangles, or various polygonal shapes. In other preferred embodiments, the ratio of the adsorbent volume to flow channel volume in the adsorbent contactor is from about 0.5:1 to about 100:1, and more preferably from about 1:1 to about 50:1. 
       FIG. 3  is a cross-sectional view along the longitudinal axis showing feed channels  3  extending through the length of the monolith with the walls of the flow channels formed entirely from adsorbent  5  plus binder. A schematic diagram enlarging a small cross section of adsorbent layer  5  is shown in  FIG. 4  hereof. The adsorbent layer  5  is comprised of a microporous adsorbent, or polymeric, particles  7 ; solid particles (thermal mass)  9 ; that act as heat sinks, a blocking agent  13  and open mesopores and micropores  11 . As shown, the microporous adsorbent or polymeric particles  7  occupy about 60% of the volume of the adsorbent layer and the particles of thermal mass  9  occupy about 5% of the volume. With this composition, the voidage (flow channels) is about 55% of the volume occupied by the microporous adsorbent or polymeric particles. The volume of the microporous adsorbent  5  or polymeric particles  7  can range from about 25% of the volume of the adsorbent layer to about 98% of the volume of the adsorbent layer. In practice, the volume fraction of solid particles  9  used to control heat will range from about 0% to about 75%, preferably about 5% to about 75%, and more preferably from about 10% to about 60% of the volume of the adsorbent layer. A blocking agent  13  fills the desired amount of space or voids left between particles so that the volume fraction of open mesopores and macropores  11  in the adsorbent layer  5  is less than about 10%. 
     When the monolith is used in a gas separation process that relies on a kinetic separation (predominantly diffusion controlled) it is advantageous for the microporous adsorbent or polymeric particles  7  to be substantially the same size. It is preferred that the standard deviation of the volume of the individual microporous adsorbent or polymeric particles  7  be less than 100% of the average particle volume for kinetically controlled processes. In a more preferred embodiment the standard deviation of the volume of the individual microporous adsorbent or polymeric particles  7  is less than about 50% of the average particle volume. The particle size distribution for zeolite adsorbents can be controlled by the method used to synthesize the particles. It is also possible to separate pre-synthesized microporous adsorbent particles by size using methods such as a gravitational settling column. It may also be advantageous to use uniformly sized microporous adsorbent or polymeric particles in equilibrium controlled separations. 
     Several ways that monoliths can be formed directly from a structured microporous adsorbent are disclosed in co-pending U.S. Provisional Patent Application No. 60/930,827, filed May 18, 2007, which is incorporated herein by reference. 
     For example, when the microporous adsorbent is a zeolite, the monolith can be prepared by extruding an aqueous mixture containing effective amounts of a solid binder, zeolite and adsorbent, solid heat control particles, and polymer. Another method by which a monolith can be formed directly from a microporous adsorbent is by extruding a polymer and microporous adsorbent mixture. 
     Also disclosed in co-pending U.S. Provisional Patent Application No. 60/930,827, filed May 18, 2007, which is incorporated herein by reference are parallel channel contactors in the form of coated monoliths wherein an adsorbent layer is coated onto the walls of the flow channels of a preformed monolith. 
       FIG. 5  hereof is a representation of a parallel channel contactor of the present invention in the form of a coated monolith  201  for TSA applications where the adsorbent layer is coated onto the channel of a preformed monolith comprised of non-adsorbent material. When TSA or RCTSA processes are performed the contactor will preferably have paths, or separate channels, that can be used to heat and cool the adsorbent. For TSA or RCTSA processes, the parallel channel contactor can be configured in a configuration similar to a shell and tube heat exchanger with the adsorbent coated on the tube walls of the heat exchanger. In this Figure, an extrusion process is used to form a monolith from a suitable non-adsorbent material including a metal such as steel, or a ceramic such as cordierite, zeolite, or a carbon. A ceramic or metallic glaze or sol gel coating  219  is applied to seal the channel walls of the monolith. As previously mentioned, such glazes can be applied by slurry coating the channel walls followed by curing by firing. A sol gel can also be applied to the channel walls and then fired under conditions that densify the coating. As previously mentioned, it is also possible to use vacuum and pressure impregnation techniques to apply the glaze or sol gel. In this case the glaze or sol gel will penetrate into the pore structure of the monolith  201 . In all cases the glaze seals the wall of the channel such that gas flowing thorough the channel is not readily transmitted into the body of the monolith. It may also be desirable to impregnate the pore structure of the monolith with a solid material before the channel walls are sealed. Alternate rows of channels are sealed at their ends  215  in order to provide for TSA operation. At the opposite end of the monolith these same rows of channels are also sealed. Slots ( 223  and  225 ) are cut through the monolith at both ends to provide flow access to the sealed rows of channels  215 . Sealing surfaces  219  are provided at both ends of the monolith as well as in the middle of the monolith  221 . In operation, the monolith will be mounted in a module in a manner that seals the ends of the channels as well as the middle of the monolith. Any suitable technology can be used to seal the ends of the channels including metallic welds, gasketing with materials such as rubbers or carbons, and the use of adhesives such as inorganic cements and epoxies. The module is configured so that a heating or cooling fluid can be flowed through the channels sealed at the ends  215  by introducing it through the slots  223  and removing it through slots  225 . The heating and cooling fluid will undergo heat exchange with fluid flowing through the channels that are open at the end of the module. These modifications to the monolith convert it into a heat exchanger. It will be understood that there are various other ways in which heat exchangers can be produced or configured. Non-limiting examples of such other ways include shell and tube heat exchangers, fiber film heat exchangers and printed circuit heat exchangers, all of which are well known in the art. By coating an adsorbent layer with a low volume fraction of meso and macropores on one side of a heat exchanger it can be used in accordance with the present invention. As such, this example illustrates how heat exchangers can be converted into modules suitable for TSA with an adsorbent layer having a low volume fraction of meso and macropores. 
     Feed channels  203  can have channel gaps from about 5 to about 1,000 microns, preferably from about 50 to about 250 microns. When the feed channel gap  203  is in a range from 50 to about 250 microns it is preferred that the thickness of the adsorbent layer  205  be in a range form about 25 to about 2,500 microns. For a 50 micron channel gap  203  the preferred range of thickness for the adsorbent layer is from about 25 to about 300 microns and a more preferred range is from about 50 to about 250 microns. The techniques previously discussed above can be used to coat the adsorbent layer into the monolith. 
       FIG. 6  hereof is a schematic of a parallel channel contactor  331  of the present invention in the form of a substantially parallel array of hollow fibers embedded in a matrix material  325 . A wide variety of hollow fibers can be formed directly using conventional spinning and extrusion processes. The contactor of this  FIG. 6  is formed from an array of hollow fibers  301 . The bores  303  of the fibers are used as flow channels. These flow channels  303  can also have channel gaps from about 5 to about 1,000 microns, preferably from about 50 to about 250 microns as previously mentioned. Also as previously mentioned, the walls of the fibers contain an adsorbent layer  305 . When the flow channel diameter  303  is in a range from about 50 to about 250 microns it is preferred that the thickness of the adsorbent layer  305  be in a range form about 25 to about 2,500 microns. 
     Various different methods known in the art can be used to produce the adsorbent layer  305  in the fiber. Some of these methods are described in co-pending U.S. Provisional Patent Application No. 60/930,827, filed May 18, 2007, which is incorporated herein by reference. 
     The fibers can be formed into a substantially parallel array to form a contactor of the present invention. One method to do this is with an embedding or potting process that surrounds the entire length of the fibers with a matrix material  325 . To visualize the array in  FIG. 6  the end of the matrix material  351  has been rendered transparent along with the face  321  of the embedded hollow fiber bundle. In many instances, it can be advantageous to coat the exterior of the fiber with a material that acts as a diffusion barrier  315 . Non-limiting examples of materials that can act as diffusion barriers include sputter deposited metal and ceramic films, evaporated metal and ceramic films, metal and ceramic films formed by chemical vapor deposition, coated composites of polymers and solids (such as clays) and coatings of polymers that have low diffusion coefficients. To act as a diffusion barrier, the effective diffusion coefficient of the coating should be less than about 1/10 the average diffusion coefficient in the adsorbent layer and preferably less than about 1/1000 the average diffusion coefficient in the adsorbent layer. When a diffusion barrier is used, the gas in the feed channel is effectively contained in the feed channel and adsorbent layer. This can eliminate the need for a supporting matrix around the fibers, thus lowering the mass of the contactor, and in some cases allowing for the cycle time in the process to be decreased (i.e., rapid cycle operation). 
     Another fabrication method suitable for use herein is to coat the adsorbent inside the prefabricated fiber such as a hollow glass fiber, hollow silica fiber or hollow polymer fiber. Coating methods previously described can be used to form an adsorbent layer inside of a prefabricated fiber. When the prefabricated fiber is made from glass, or silica, the final product has a built in diffusion barrier  315 . 
     When there is no diffusion barrier on the fiber it is advantageous for, the matrix material to contain an adsorbent having a low volume fraction of mesopores and macropores. In this case, it is advantageous to space the fibers closely together with the distance between adjacent fibers less than about 5 fiber diameters, preferably less than about 1.5 fiber diameters. When there is a diffusion barrier on the outer surface of the fibers, it can be advantageous to embed only the ends  351  and  353  of the fiber bundle in the matrix material. In this case, the matrix material only has to support the fibers and not have substantial gas flow through the material. It can be composed of polymer, metal or ceramic or combinations thereof. It is preferred that the matrix be nonporous and requirements for having an adsorbent in the matrix material can be minimized or eliminated. Requirements for spacing between fibers can be less critical than when the entire length of the fiber is potted or embedded. The matrix material can be applied selectively to the ends of the fiber bundles by any suitable method known in the art. Non-limiting examples of such methods include potting, embedding, casting, electroplating, or electroless plating processes. To avoid plugging the end of the fibers the end of the fibers can be filled with a material that can be readily removed after the matrix is applied. Non-limiting examples of materials that can be readily removed include polymers, metals, salts and inorganics that can be selectively dissolved or etched away after the matrix material has been applied. Grinding, machining and polishing methods can also be used to open the ends of the fibers. Other methods to pot or embed the ends of the fibers are similar to those used to form hollow fiber membrane modules. When the ends of the fiber bundle are potted with a matrix material it is advantageous to place the contactor into an operational RCPSA, PSA or PSA module in a manner such that most of the feed gas flows through the bore of the fiber. One way to ensure that the flow goes through the bore of the fiber is to place a fibrous packing, or inram, between the matrix material at the ends  351  and  353  and the interior of the PSA, RCPSA, RCPPSA or PPSA module. Another way is to bond the ends of the contactor to the interior of the pressure swing adsorption module. 
       FIGS. 7 and 8  hereof are representations of a parallel channel contactor of the present invention in the form of a hollow fiber contactor for a TSA process where the adsorbent layer  405  comprises part of the wall of the fiber wherein the fiber have a hollow core  403 . In  FIG. 8 , the outer surfaces of the housing for the contactor  401  are rendered transparent with only dotted lines indicating the edges of the outer surface. The hollow fibers used in this example have a diffusion barrier  415  on their exterior surface. The ends of the fiber bundle are potted or embedded in a matrix material  417 . This potted array is then sealed into a tubular housing  401 . Sealing surfaces  419  are provided at the ends of the tubular housing  401 . A sealing surface  421  is also provided in the middle of the housing. Slots  423  and  425  are cut through the wall near the ends of the tubular housing to allow for the flow of heating and cooling fluids. 
     In operation, the tubular housing is mounted in a TSA or RCTSA module in a manner that seals the ends of the channels as well as the middle of the monolith. Any suitable sealing technology can be used. Non-limiting examples of sealing technologies that can be used in the practice of the present invention include metallic welds, gasketing with materials such as rubbers or carbons, and the use of adhesives such as inorganic cements or epoxies. The module is configured so that a heating or cooling fluid can be flowed inside the hollow tubular housing  401  by introducing it through slots  423  and removing it through slots  425 . The heating and cooling fluid will undergo heat exchange with fluid flowing through the hollow fibers which are open at the end of the module. With these sealing arrangements, the tubular housing  401  containing the parallel array of hollow fibers becomes a heat exchanger suitable for use in TSA processes. The fibers have an adsorbent layer  405  with a low volume fraction of meso and macropores. 
       FIG. 9  hereof is a representation of a parallel channel contactor of the present invention in which the parallel channels are formed from laminated sheets containing adsorbent material. Laminates, laminates of sheets, or laminates of corrugated sheets can be used in PSA RCPSA, PPSA or RCPPSA processes. Laminates of sheets are known in the art and are disclosed in U.S. Patent Publication US2006/0169142 A1 and U.S. Pat. No. 7,094,275 B2 which are incorporated herein by reference. When the adsorbent is coated onto a geometric structure or components of a geometric structure that are laminated together, the adsorbent can be applied using any suitable liquid phase coating techniques. Non-limiting examples of liquid phase coating techniques that can be used in the practice of the present invention include slurry coating, dip coating, slip coating, spin-coating, hydrothermal film formation and hydrothermal growth. When the geometric structure is formed from a laminate, the laminate can be formed from any material to which the adsorbent of the present invention can be coated. The coating can be done before or after the material is laminated. In all these cases the adsorbent is coated onto a material that is used for the geometric shape of the contactor. Non-limiting examples of such materials include glass fibers, milled glass fiber, glass fiber cloth, fiber glass, fiber glass scrim, ceramic fibers, metallic woven wire mesh, expanded metal, embossed metal, surface-treated materials, including surface-treated metals, metal foil, metal mesh, carbon-fiber, cellulosic materials, polymeric materials, hollow fibers, metal foils, heat exchange surfaces, and combinations of these materials. Coated supports typically have two major opposing surfaces, and one or both of these surfaces can be coated with the adsorbent material. When the coated support is comprised of hollow fibers, the coating extends around the circumference of the fiber. Further support sheets may be individual, pre-sized sheets, or they may be made of a continuous sheet of material. The thickness of the substrate, plus applied adsorbent or other materials (such as desiccant, catalyst, etc.), typically ranges from about 10 micrometers to about 2000 micrometers, more typically from about 150 micrometers to about 300 micrometers. 
     Metallic mesh supports can provide desirable thermal properties of high heat capacity and conductivity which “isothermalize” a PSA, RCPSA, PPSA or RCPPSA cycle to reduce temperature variations that degrade the process when conducted under more adiabatic conditions. Also, metal foils are manufactured with highly accurate thickness dimensional control. The metal foil may be composed of, without limitation, aluminum, steel, nickel, stainless steel or alloys thereof. Hence there is a need for a method to coat metal foils with a thin adsorbent layer of accurately controlled thickness, with necessary good adhesion. One method for doing this is by hydrothermal synthesis. Coating procedures used can be very similar to the way in which zeolite membranes are prepared as discussed above. Zeolite layers grown by hydrothermal synthesis on supports often have cracks which are meso and micropores. Examples of these cracks and ways of preparing zeolite films containing a controlled density of cracks are disclosed in co-pending U.S. Provisional Patent Application No. 60/930,827, filed May 18, 2007, which is incorporated herein by reference. 
     The volume of these pores is often less than about 10 vol % of the film thickness and there is often a characteristic distance between cracks. Another method of coating a metal foil is with thick film coating is slip casting, or doctor blading. An aqueous slurry of prefabricated zeolite particles, binder (for example colloidal silica or alumina), viscosifying agent such as a polymer like polyvinyl alcohol is cast for example onto a metal foil and fired to remove the polymer and cure the binder and zeolite. The product, after firing, is then a bound zeolite film on a metal foil typically containing about 30 to about 40 vol % voids. To make a suitable adsorbent layer, the voids are filled in a subsequent step by coating the bound zeolite film with a polymer or by introducing a liquid into the voids of the bound zeolite film. The final product, after filling the voids with a polymer or liquid, will be an adsorbent layer having the low meso and macroporosity requirements of the present invention. 
     Another method for coating metal foils with prefabricated zeolite crystals, or microporous particles, is electrophoretic deposition (EPD). EPD is a technique for applying high quality coatings of uniform thickness to metal substrates. The method can be used to apply organic and inorganic particulate coatings on electrically conductive substrates. Slurry compositions containing prefabricated zeolites, or microporous particles, may be electrophoretically applied to a rigid support material, such as by using the method described in Bowie Keefer et al.&#39;s prior Canadian Patent Application No. 2,306,311, entitled “Adsorbent Laminate Structure,” which is incorporated herein by reference. 
     Some contactor geometric shapes will require that the adsorbent be applied to the channel surface in a layer using a colloidal binder material or that an entire geometric shape be comprised of the adsorbent plus colloidal binder and containing a plurality of parallel channels. When a colloidal binder is used, the selection of the colloidal material depends on the particular adsorbent used. Colloidal materials capable of functioning as a binder and/or which form a gel are preferred. Such colloidal materials include, without limitation, colloidal silica-based binders, colloidal alumina, colloidal zirconia, and mixtures of colloidal materials. “Colloidal silica” refers to a stable dispersion of discrete amorphous silicon dioxide particles having a particle size ranging from about 1 to about 100 nanometers. Suitable colloidal silica materials also can be surface modified, such as by surface modification with alumina. Another type of colloidal binder suitable for use herein include clay materials, such as palygorskite (also known as attapulgite), which are hydrated magnesium aluminum silicates. Also, inorganic binders may be inert; however, certain inorganic binders, such as clays, used with zeolite adsorbents may be converted in-situ from kaolin binders to zeolite so that the zeolite is self-bound with minimal inert material. In these bound structures, the voids between the colloidal particles form mesopores and the voids between the adsorbent particles form meso and/or macropores. A blocking agent can be applied to fill the majority of the meso and macroporosity in these bound layers so that the adsorbent meets the open pore volume requirement of this invention. Organic binders used to bind activated carbon particulates in laminated structures may be pyrolyzed to form a useful carbonaceous adsorbent. 
       FIG. 9  hereof illustrates an embodiment of the present invention wherein a microporous adsorbent, preferably DDR, film  505  is hydrothermally grown on each of both faces of flat metal foils  509  (which is preferably stainless steel). The metal foils  509  with the adsorbent films  505  are laminated together  501  to form a parallel channel contactor. Spacers of appropriate size are placed between the metal foils during lamination so that the channel gap  503  is of a predetermined size. Approximately half the volume of the feed channels  503  are filled with a spacer that keeps the sheets substantially evenly spaced apart. 
     The heat capacity of the metal foils  509  limits the thermal excursions in the process. When a target component, such as CO 2 , is adsorbed in the adsorbent, heat is released in the amount of the heat of adsorption. This warms the adsorbent films and as the film warms, its temperature rises above that of the metal foils and heat diffuses into the metal foil where it is stored. Desorption of a target component, such as CO 2 , from the adsorbent is an endothermic process and heat must be supplied in an amount equal to the heat of adsorption. When the target component desorbs, the temperature of the films falls below that of the metal foils and heat stored in the metal foils flows into the films. The thermal excursion of the adsorbent film is less than +/−10° C. with the contactor dimensions and the process described in this example. 
     The adsorbent film is composed of individual adsorbent crystals, mesopores (including grain boundaries) and macropores. In this example, the crystals in the film are substantially of the same size. Most of the open volume in the film is comprised of mesoporous cracks with characteristic widths of about 200 angstroms. These mesoporous cracks are substantially evenly distributed throughout the film. The total volume of the mesopores and macropores is about 5 vol % of the total volume of the adsorbent film. 
     The present invention can better be understood with reference to the following examples that are presented for illustrative purposes and not to be taken as limiting the invention. 
     Example 1 
     This example illustrates the use of a turboexpander to condition acid gas (i.e., natural gas containing H 2 S and CO 2 ) so that PSA can operate in the window that optimizes methane recovery.  FIG. 1  hereof shows a process scheme in which a turboexpander is used to set the pressure and temperature of an acid gas that is separated in a PSA. An acid gas stream  811  with a temperature of 100° C. and pressure of 1,500 psi is produced from a gas field and fed to the process. The CO 2  content of the stream is about 66 mol % and the H 2 S concentration is 2 mol %. Water is present at its saturated vapor pressure and the concentration of the heavy hydrocarbons is about 2 mol %. The heavy hydrocarbons contain a small fraction of waxy species with carbon numbers as large as 36. For this stream  811 , CO 2  comprises the majority of the heavy component that will be removed by a kinetically controlled PSA process. If DDR zeolite is used as the adsorbent in the kinetically controlled PSA, the loading in the DDR zeolite from CO 2  partial pressure in stream  811  would be in excess of 0.6 q s  and the slope of the CO 2  isotherm would be: 
                 ∂     q     CO   ⁢           ⁢   2           ∂     P     CO   ⁢           ⁢   2           ≅     .02   ⁢           ⁢     K     CO   ⁢           ⁢   2       ⁢     q   s             
where the K CO2  is the Henry&#39;s constant for CO 2  and q s  is the saturated loading for CO 2  in DDR.
 
     To bring the stream into a more preferred window of operation the stream is passed through a turboexpander  821  that reduces the stream pressure to about 500 psi. In a preferred embodiment, the turboexpander  821  is designed to have a radial inflow. Radial inflow turbine designs suitable for use in this process can be found in Perry&#39;s Chemical Engineers&#39; Handbook (7th Edition. © 1997 McGraw-Hill edited by R. H Perry and D. W. Green). During the approximately isentropic expansion the gas temperature falls significantly and liquids fall out of the gas stream due to a change in the dew point. Radial inflow turbine designs can be operated so that liquids falling out of the gas stream will not impede the operation of the turboexpander. In this example, the power generated by the turboexpander is coupled through a shaft  831  to and an electric generator  823 . In an alternative embodiment, the power from the turboexpander is shaft coupled to a compressor instead of an electric generator. 
     Before the stream is passed through turboexpander  821  it may optionally be sent through a process  813  to remove any particles, or a portion of the wax, or optionally some of the heavy hydrocarbons, H 2 S and/or water. The absolute temperature of the stream  837  coming out of the turboexpander is approximately 30% less than feedstream  811  and contains a mixture of gas and liquid droplets. Stream  837  is then sent to a process block  839  that at least removes the liquid droplets from the stream. Liquid droplet removal can be accomplished through a variety of methods including coalescing filters, settling drums, static centrifugation, and electrostatic precipitation. The process block  839  also contains equipment to increase the temperature of stream  837 . Means of heating the stream within process block  839  include heat exchangers such as shell and tube heat exchangers as well as other types of heat exchangers including the many varieties discussed in Perry&#39;s Chemical Engineers&#39; Handbook (7th Edition. © 1997 McGraw-Hill edited by R. H Perry and D. W. Green) and packed bed heat exchangers as well as mixing the stream with an optional separately formed hot gas stream  835 . When heat exchangers are used in process block  839  it is preferred that they extract heat from either streams  881 ,  891  or  895 . Optionally, the heat exchanger used in process block  839  can extract heat from optional stream  835 . In one embodiment stream  835  is produced by combusting hydrocarbon and air or oxygen enriched air. In another embodiment, stream  835  is produced by heat exchanging a working fluid or gas with high temperature combustion products. Besides increasing the temperature of stream  837  and removing liquid droplets, process block  839  can optionally be configured to remove heavy hydrocarbons, water vapor, or H 2 S from the gas phase. In this example, process block  839  is configured to remove liquid droplets, and to heat stream  837  to a temperature of about 90° C. 
     The physical composition of stream  871  coming from process block  839  is such that if DDR zeolite is used as the adsorbent in a kinetically controlled PSA, the loading in the DDR zeolite from CO 2  partial pressure in stream  871  would be in excess of 0.5 q s  and the slope of the CO 2  isotherm would be: 
                 ∂     q     CO   ⁢           ⁢   2           ∂     P     CO   ⁢           ⁢   2           ≅     .02   ⁢           ⁢     K     CO   ⁢           ⁢   2       ⁢     q   s             
where K CO2  is the Henry&#39;s constant for CO 2  at 90° C. and q s  is the saturated loading for CO 2  in DDR.
 
     This operating condition is in a more desirable range for high methane recovery with a kinetically controlled PSA process than that for stream  811 . PSA unit  841  is used to separate most of the CO 2  and a fraction of the H 2 S out of stream  871 . In a preferred embodiment, PSA unit  841  contains a parallel channel contactor with an adsorbent having less than an open volume fraction of mesopores and macropores that is less than 10 vol %. In a preferred embodiment, the microporous adsorbent in the contactor is an 8-ring zeolite and PSA unit  841  is a RCPSA unit that is operated in a kinetically controlled mode. In a preferred embodiment more than about 90 mol % of the methane and heavy hydrocarbon fed to PSA unit  841  is recovered in the methane enriched stream  815 . In a an even more preferred embodiment more than about 95 mol % of the methane and heavy hydrocarbon fed to PSA unit  841  is recovered in the methane enriched stream  815 . In this example the molar ratio of methane to CO 2  in the methane enriched stream  815  is greater than 9:1. Depending upon final use the methane enriched stream  815  may be further processed or purified in other processes. The CO 2  enriched stream  881  coming from the PSA  841  can be sent through an optional process block  851  to remove water vapor. The optional process block  851  can also contain one side of a heat exchanger that is used to provide heat to the heat exchanger in process block  839 . The CO 2  in the stream  881  is ultimately sent to a compressor  829 . The compressor  829  is driven by the energy recovered from the turboexpander  821 . In this example, energy produced by the electric generator  823  is sent through a power transmission line  825  to power a motor  827  that is shaft coupled  833  to the compressor  829 . As was previously mentioned in an alternative embodiment, the compressor  829  can be shaft coupled to the turboexpander  821 . Because of the work of compression the temperature of the stream  891  coming out of the compressor  829  is greater than that of stream  881 . It can be advantageous to cool stream  891  before further compression to temperatures required for CO 2  disposal/sequestration. Cooling can be accomplished with an optional process block  883  that contains one side of a heat exchanger that is used to provide heat to the heat exchanger in process block  839 . If needed, process block  883  can contain equipment such as a glycol dehydration unit to reduce the corrosivity of the gas mixture. To raise the pressure of the CO 2  rich gas stream  893  to the level needed for CO 2  disposal/sequestration a final compressor  897  is provided. The compressed CO 2  rich gas stream  895  can then be sequestered at high pressures into a suitable sequestration structure such as a suitable oil or gas reservoir or available aquifer. 
     Example 2 
     With a laminated sheet parallel channel contactor described for  FIG. 10  hereof, a PSA/RCPSA cycle with five steps is operated to produce a product stream containing about 20 vol % CO 2  and about 80 vol % CH 4 . Overall methane recovery for the PSA/RCPSA cycle is computed to be about 95 vol %.  FIG. 10  hereof is a schematic diagram of five different steps in a preferred PSA/RCPSA cycle suitable for use in this invention. In the first step  611   a  parallel channel contactor PSA/RCPSA cycle is pressurized with high pressure product gas  687 . This pressurization raises the pressure in the parallel channel contactor and fills the contactor with the purified product containing about 20 vol % CO 2  and about 80 vol % CH 4 . In a second step  621   a  high pressure, 51 atmosphere (atm) feed gas  671  is conducted through the parallel channel contactor. During this step  621  the DDR adsorbent layer adsorbs CO 2  from the flowing feed gas  671 . A purified product  625  flows out of the end of the contactor. The feed gas  671  is flowed at a rate such that as the product  625  emerges from the parallel channel contactor as a concentration front moves through the contactor. Ahead of the front the gas has a composition near that of the product  625 . Behind the front the gas has a composition near that of the feed  671 . The second step  621  is stopped before this front completely breaks-through the end of the contactor. The amount of feed which emerges from the contactor before this step is halted determines in part the product purity. 
     At this point, a third step of the cycle  631  is initiated which serves to purge the contactor of feed gas trapped in the contactor channels. The third step  631  also acts, in part, as a partial pressure displacement purge of the contactor. Valves are opened at the top and bottom of the contactor. A pressurized CO 2  rich stream  633  flows into the top of the module and gas originally contained in the flow channels of the structured parallel channel contactor flows out  639 . The gas fed into the top of the module  633  is a CO 2 -rich gas produced in later steps 4 and 5 that has been compressed  675  to a pressure slightly greater than the feed pressure (51 atm.). The composition of the gas fed through the top of the contactor is substantially equal to that of the CO 2  reject stream  681 , containing about 97.5 vol % CO 2  and about 2.5 vol % CH 4 . The gas exiting out the bottom of the contactor  639  has a composition nearer to that of the feed gas  671  (about 70 vol % CO 2  and about 30 vol % CH 4 ). 
     As the gas stream entering the module  633  displaces the gas in the flow channels, a compositional front moves from top to bottom of the module. The third step  631  is stopped and a fourth step  641  is begun before, or shortly after, this front breaks through the bottom of the module. The fourth step  641  lets the pressure of the contactor down to an intermediate pressure and recovers some of the CO 2  for recompression. In the design discussed in this example, the intermediate pressure is about 22 atmospheres (atm). In the fourth step, a CO 2 -rich stream  649  exits the module at a pressure of about 22 atm. This stream is split into two streams  679  and  681 . Stream  679  is fed to compressor  675  and stream  681  is rejected from the process at a pressure of about 22 atm. Stream  633 , that was used to rinse the contactor in the third step of the process  631 , is comprised of the gas stream  679  that emerges from compressor  675 . As the pressure in the contactor drops towards the outlet pressure of about 22 atm., the flow in streams  679  and  681  decreases. When the flow in these streams has fallen to approximately ¼ of the initial value step  4  is stopped and a step  5  is begun. In the fifth step of the process  651 , the module pressure is dropped to about 5 atm. and a CO 2 -rich stream is recovered  685 . This stream  685  can optionally be fed through a compressor  677  that raises the stream pressure to about 22 atm. The stream is then combined with stream  681  and a CO 2 -rich stream  683  is rejected from the process at a pressure of about 22 atmospheres. 
     To improve the operation of the process, as well as the pressure at which CO 2  is recovered, gas may be recovered in the fifth step  651  using a multi-step process in which the contactor pressure is decreased in a series of pressure equalization steps. Gas from these pressure equalization steps can be recovered as individual gas streams and recompressed. In an example with two pressure, equalization steps, one portion of the CO 2 -rich gas is recovered at a pressure of about 12 atm while the rest is recovered at about 5 atm. It is also possible to decrease the module pressure in step four  641  using a series of pressure equalization steps. Again, each pressure equalization step can be used to form a gas stream that can either be rejected from the process in stream  683  or recompressed to form stream  633 . If pressure equalization steps are employed, it is advantageous to design them to maximize the pressure at which the CO 2  reject streams are captured. 
     Optionally when the CO 2  reject stream  683  is sequestered it is preferred to capture the CO 2  at a pressure that is more than 1/10th of the partial CO 2  pressure in the feed. In a more preferred embodiment the pressure at which the CO 2  is captured is more than ¼th of the CO 2  partial pressure in the feed. 
     Example 3 
     Using this parallel channel contactor, a PSA/RCPSA cycle with five different steps is operated to produce product stream containing about 2 vol % N 2  and about 98 vol % CH 4 . Overall methane recovery for the PSA/RCPSA cycle is computed to be about 91 vol %.  FIG. 11  hereof shows a schematic diagram of the five different steps in the PSA/RCPSA cycle. In the first step  711   a  parallel channel contactor PSA/RCPSA cycle is pressurized with high pressure product gas  787 . This pressurization raises the pressure in the parallel channel contactor and fills the contactor with the purified product containing about 2 vol % N 2  and about 98 vol % CH 4 . In a second step  721   a  high pressure 100 atm feed gas  771  is flowed through the contactor. During this step  721  the DDR adsorbent layer removes N 2  from the flowing feed gas  771 . A purified product  725  flows out of the end of the contactor. The feed gas  771  is flowed at a rate such that as the product  725  emerges from the contactor a concentration front moves through the contactor. Ahead of the front the gas has a composition near that of the product  725 . Behind the front the gas has a composition near that of the feed  771 . Before this front completely breaks through the end of the contactor the second step  721  is stopped. The amount of feed which emerges from the contactor before this step is halted determines in part the product purity. 
     At this point, a third step of the cycle  731  is initiated which serves to purge the contactor of feed gas trapped in the contactor channels. The third step  731  also acts in part as a partial pressure displacement purge of the contactor. Valves are opened at the top and bottom of the contactor. A pressurized N 2  rich stream  733  flows into the top of the module and gas originally contained in the flow channels of the structured parallel channel contactor flows out  739 . The gas fed into the top of the module  733  is a N 2  rich gas produced in later steps (4 and 5) that has been compressed  775  to a pressure slightly greater than the feed pressure (about 100 atm.). Composition of the gas fed in through the top of the contactor is nearly that of the N 2  reject stream  781 . The gas exiting out the bottom of the contactor has a composition nearer to that of the feed gas  771  (about 30 vol % N 2  and about 70 vol % CH 4 ). 
     As the gas stream entering the module  733  displaces the gas in the feed channel a compositional front moves from top to bottom of the module. Before or shortly after this front breaks through the bottom of the module the third step  731  is stopped and a fourth step  741  is begun. The fourth step  741  lets the pressure of the contactor down to an intermediate pressure and recovers some of the N 2  for recompression. In the design discussed in this example the intermediate pressure is 30 atm. In the fourth step a N 2  rich stream  749  exits the module at a pressure of about 30 atm. This stream is split into two streams  779  and  781 . Gas in stream  779  is fed to a compressor  775  and gas in stream  781  is rejected from the process at a pressure of about 30 atm. In an optimization of this process a pressure in step  741  is chosen that minimizes the amount of gas flowing in stream  781 . Stream  733  that was used to rinse the contactor in the third step of the process  731  is comprised of the gas stream  779  that emerged from the compressor  775 . As the pressure in the contactor drops towards the outlet pressure of about 30 atm, the flow in streams  779  and  781  decrease. When the flow in these streams has fallen to approximately ¼ of the initial value the fourth step is stopped and a fifth step is begun. In the fifth step of the process  751  the module pressure is dropped to about 1.2 atm and a N 2  rich stream is recovered  785 . 
     To improve the operation of the process, as well as the pressure at which N 2  is recovered, gas may be recovered in the fifth step  751  using a multi-step process in which the contactor pressure is decreased in a series of pressure equalization steps. In an example with two pressure equalization steps, one portion of the N 2  rich gas is recovered at a pressure of 12 atmospheres while the rest is recovered at about 1.2 atmospheres. 
     It is also possible to decrease the module pressure in step four  741  with a series of pressure equalization steps. Again each pressure equalization step can be used to form a gas stream that can either be rejected from the process in stream  783  or recompressed to form stream  733 . If pressure equalization steps are employed is it advantageous to design them to maximize the pressure at which the N 2  reject streams are captured.