TECHNOLOGY FOCUS - CHEMICAL ENGINEERING - Preferred Method: Separating the fluid mixture comprising at least first and second fluid components, additionally comprises admitting a pre-regeneration fluid into the parallel passage adsorbent contactor and desorbing at least a portion of the second fluid component co-adsorbed on the adsorbent material by heating the adsorbent material to a pre-regeneration temperature, prior to recovering the first product fluid. The adsorbent material is kinetically selective for the first fluid component and has a first mass transfer rate for the first fluid component which is greater than a second mass transfer rate for the second fluid component. Admitting the fluid mixture comprises admitting the fluid mixture into the inlet end of the parallel passage adsorbent contactor to flow towards the outlet end in the first axial direction where the fluid mixture is admitted at a space velocity greater than the second mass transfer rate for the second fluid component and less than the first mass transfer rate for the first fluid component. The method also comprises conditioning at least one the adsorbent material to a desired pre-adsorption temperature prior to admitting the fluid mixture into the parallel passage adsorbent contactor. The adsorbing further comprises adsorbing at least a portion of the first fluid component on the adsorbent material at a first adsorbent material temperature, and the desorbing further comprises desorbing at least a portion of the first fluid component adsorbed on the adsorbent material by heating the adsorbent material at a second adsorbent material temperature. The second adsorbent material temperature is higher than the first adsorbent material temperature. The pre-regeneration temperature is greater than the first adsorbent temperature, and less than the second adsorbent temperature. The pre-adsorption temperature is lower than a first adsorbent material temperature during the adsorbing of the first fluid component, or where the pre-adsorption temperature is higher than a first adsorbent material temperature during the adsorbing of the first fluid component, and lower than a second adsorbent material temperature during the desorbing of the first fluid component. The parallel passage adsorbent contactor comprises at least first and second adsorbent materials, and where the desorbing comprises desorbing at least a portion of the first fluid component adsorbed on the first adsorbent material by heating the first adsorbent material separately from the second adsorbent material. The desorbing additionally comprises supplying a purge fluid into the parallel passage adsorbent contactor, and the recovering additionally comprises recovering a desorbed product fluid comprising the first fluid component and the purge fluid. The purge fluid is condensable, and additionally comprises condensing the purge fluid out of the desorbed product fluid following recovering the desorbed product fluid. The desorbing additionally comprises heating at least one the adsorbent material by supplying at least one heat transfer fluid at an elevated temperature into the parallel passage adsorbent contactor. The desorbing additionally comprises directly heating at least one the adsorbent material by supplying thermal energy to the thermally conductive filaments to directly heat the cell walls comprising the adsorbent material. The axially continuous thermally conductive filaments additionally comprise axially continuous electrically conductive filaments, and where the desorbing additionally comprises directly heating at least one the adsorbent material by electrically heating the thermally and electrically conductive filaments to directly heat the cell walls comprising the adsorbent material. The parallel passage adsorbent contactor comprises at least first and second axial segments comprising first and second adsorbent materials, and where the desorbing comprises desorbing at least a portion of the first fluid component adsorbed on the first adsorbent material by electrically heating the conductive filaments in the first segment in contact with the first adsorbent material separately from the second adsorbent material. The parallel passage adsorbent contactor comprises at least first and second axial segments comprising first and second adsorbent materials, and where the desorbing comprises desorbing at least a portion of the first fluid component adsorbed on the first adsorbent material by electrically heating the conductive filaments in the first segment in contact with the first adsorbent material, and then sequentially desorbing at least a portion of a fluid component adsorbed on the second adsorbent material by electrically heating the conductive filaments in the second segment in contact with the second adsorbent material. The first segment is located nearest to the outlet end of the parallel passage contactor and the second segment is located towards the inlet end of the parallel passage contactor from the first segment, and where the recovering additionally comprises sequentially recovering a second desorbed product fluid enriched in a fluid component adsorbed on the second adsorbent material from at least one of the inlet and outlet ends. The conditioning additionally comprises admitting at least one heat transfer fluid into the parallel passage adsorbent contactor to condition at least one the adsorbent material to the desired pre-adsorption temperature. The conditioning further comprises providing a secondary purge of the adsorbent material prior to admitting the fluid mixture. The transferring heat along at least a portion of the thermally conductive filaments during the adsorbing step is effective to reduce a thermal profile spike in the parallel passage adsorbent contactor associated with the adsorbing of the first fluid component on the adsorbent material. The adsorbent material is selected from: desiccant, activated carbon, carbon molecular sieve, carbon adsorbent, graphite, activated alumina, molecular sieve, aluminophosphate, silicoaluminophosphate, zeolite adsorbent, ion exchanged zeolite, hydrophilic zeolite, hydrophobic zeolite, modified zeolite, natural zeolites, faujasite, clinoptilolite, mordenite, metal-exchanged silico-aluminophosphate, uni-polar resin, bi-polar resin, aromatic cross-linked polystyrenic matrix, brominated aromatic matrix, methacrylic ester copolymer, graphitic adsorbent, carbon fiber, carbon nanotube, nano-materials, metal salt adsorbent, perchlorate, oxalate, alkaline earth metal particle, ETS, CTS, metal oxide, chemisorbent, amine, organometallic reactant, and metal organic framework adsorbent materials, and combinations. The admitting, adsorbing, recovering a first product fluid, desorbing and recovering the desorbed second product fluid steps are substantially isobaric and are conducted at one of substantially atmospheric and elevated supra-atmospheric pressures. The admitting, adsorbing, and recovering a first product fluid are conducted at substantially atmospheric pressure, and where the desorbing and recovering a desorbed second product fluid steps are conducted at an elevated super-atmospheric pressure. Preferred Process: The temperature swing adsorption method additionally comprises admitting a pre-regeneration fluid into the parallel passage adsorbent contactor and desorbing at least a portion of the nitrogen component co-adsorbed on the carbon dioxide adsorbent material by heating the carbon dioxide adsorbent material to a pre-regeneration temperature, prior to recovering the first product fluid. The carbon dioxide adsorbent material is kinetically selective for the carbon dioxide component and has a first mass transfer rate for the carbon dioxide component which is greater than a second mass transfer rate for the nitrogen component. Admitting the flue gas comprises admitting the flue gas into the inlet end of the parallel passage adsorbent contactor to flow towards the outlet end in the first axial direction where the flue gas is admitted at a space velocity greater than the second mass transfer rate for the nitrogen component and less than the first mass transfer rate for the carbon dioxide component. The temperature swing adsorption process also comprises conditioning at least one the adsorbent material to a desired pre-adsorption temperature prior to admitting the flue gas feed mixture into the parallel passage adsorbent contactor. The adsorbing further comprises adsorbing at least a portion of the carbon dioxide on the carbon dioxide adsorbent material at a first adsorbent material temperature, and the desorbing further comprises desorbing at least a portion of the carbon dioxide adsorbed on the adsorbent material by heating the adsorbent material at a second adsorbent material temperature higher than the first adsorbent material temperature. The pre-regeneration temperature is greater than the first adsorbent temperature, and less than the second adsorbent temperature. The pre-adsorption temperature is lower than at least one of: a first adsorbent material temperature during the adsorbing of the carbon dioxide and a second adsorbent material temperature during the desorbing of the carbon dioxide. The parallel passage adsorbent contactor comprises at least a first carbon dioxide adsorbent material and a second adsorbent material, and where the desorbing comprises desorbing at least a portion of the carbon dioxide adsorbed on the first adsorbent material by heating the first adsorbent material separately from the second adsorbent material. The desorbing additionally comprises supplying a purge gas into the parallel passage adsorbent contactor, and the recovering additionally comprises recovering a carbon dioxide enriched product fluid comprising carbon dioxide and the purge gas. The purge gas is condensable, and additionally comprises condensing the purge gas out of the desorbed product fluid following recovering the desorbed product fluid. The purge gas comprises at least one of: ambient air, steam, and a flue gas product stream depleted of carbon dioxide. The desorbing additionally comprises heating at least one the adsorbent material by supplying at least one heat transfer fluid at an elevated temperature into the parallel passage adsorbent contactor and desorbing the carbon dioxide into the heat transfer fluid. The heat transfer fluid comprises at least one of: ambient air, steam, a carbon dioxide enriched product gas, and a flue gas product stream depleted of carbon dioxide. The desorbing additionally comprises directly heating at least one the carbon dioxide adsorbent material by supplying thermal energy to the thermally conductive filaments to directly heat the cell walls comprising the adsorbent material. The axially continuous thermally conductive filaments additionally comprise axially continuous electrically conductive filaments, and where the desorbing additionally comprises directly heating at least one the carbon dioxide adsorbent material by electrically heating the thermally and electrically conductive filaments to directly heat the cell walls comprising the adsorbent material. The parallel passage adsorbent contactor comprises at least first and second axial segments comprising a first carbon dioxide adsorbent material and a second adsorbent material, respectively, and where the desorbing comprises desorbing at least a portion of the carbon dioxide adsorbed on the first adsorbent material by electrically heating the conductive filaments in the first segment in contact with the first adsorbent material separately from the second adsorbent material. The parallel passage adsorbent contactor comprises at least first and second axial segments comprising a first carbon dioxide adsorbent material and a second adsorbent material respectively, and where the desorbing comprises desorbing at least a portion of the carbon dioxide adsorbed on the first adsorbent material by electrically heating the conductive filaments in the first segment in contact with the first adsorbent material, and then sequentially desorbing at least a portion of a flue gas stream component adsorbed on the second adsorbent material by electrically heating the conductive filaments in the second segment in contact with the second adsorbent material. The first segment is located nearest to the outlet end of the parallel passage contactor and the second segment is located towards the inlet end of the parallel passage contactor from the first segment, and where the recovering additionally comprises sequentially recovering a second desorbed product fluid enriched in a flue gas component adsorbed on the second adsorbent material from at least one of the inlet and outlet ends. The conditioning additionally comprises admitting at least one heat transfer fluid into the parallel passage adsorbent contactor to condition at least one the adsorbent material to the desired pre-adsorption temperature. The conditioning further comprises providing a secondary purge of the carbon dioxide adsorbent material prior to admitting the flue gas feed mixture. The transferring heat along at least a portion of the thermally conductive filaments during the adsorbing step is effective to reduce a thermal profile spike in the parallel passage adsorbent contactor associated with the adsorbing of carbon dioxide on the carbon dioxide adsorbent material. The carbon dioxide adsorbent material is selected from: activated carbon adsorbent, carbon molecular sieve, amine impregnated adsorbent supports (comprising silica, activated carbon, alumina, zeolite, polymer and ceramic supports), metal salt, metal hydroxide, metal oxide, zeolite, hydrotalcite, silicalite, metal organic framework and zeolitic imadazolate framework adsorbent materials, and combinations. The admitting, adsorbing, recovering a flue gas product stream, desorbing and recovering a desorbed carbon dioxide product steps are substantially isobaric and are conducted at one of substantially atmospheric and one or more elevated super-atmospheric pressures. The admitting, adsorbing, and recovering a flue gas product stream are conducted at substantially atmospheric pressure, and where the desorbing and recovering a desorbed carbon dioxide product steps are conducted at an elevated super-atmospheric pressure. The transferring heat along at least a portion of the thermally conductive filaments during the adsorbing step is effective to substantially retain a thermal wave front resulting from the adsorbing step within the parallel passage adsorbent contactor at the end of the adsorbing step. The parallel passage adsorbent contactor comprises at least first and second axial segments comprising a first adsorbent material selective for carbon dioxide over nitrogen, and a second adsorbent material selective for at least one of water, nitrogen oxides, sulfur oxides and heavy metals over carbon dioxide, respectively, and where the second axial segment is located upstream of the first axial segment nearer to the inlet end of the contactor. The parallel passage adsorbent contactor further comprises at least a third axial segment comprising a third adsorbent material selective for at least one of water, nitrogen oxides, sulfur oxides and heavy metals over carbon dioxide, and where the third axial segment is located upstream of the first axial segment and downstream of the second axial segment. Alternatively, the temperature swing adsorption process for separating at least one of carbon dioxide and hydrogen sulfide from a natural gas feed mixture comprising at least one of carbon dioxide and hydrogen sulfide and methane components comprises: admitting the natural gas feed mixture into an adsorptive separation system comprising at least one parallel passage adsorbent contactor, the parallel passage adsorbent contactor comprising a set of substantially parallel fluid flow passages oriented in a first axial direction between an inlet and an outlet end; cell walls situated between the fluid flow passages comprising at least one adsorbent material selective for at least one of carbon dioxide and hydrogen sulfide over methane; and a set of axially continuous thermally conductive filaments oriented in the axial direction and in direct contact with the adsorbent material; admitting the natural gas feed mixture into the inlet end of the parallel passage adsorbent contactor to flow towards the outlet end in the first axial direction; adsorbing at least a portion of at least one of the carbon dioxide and hydrogen sulfide components on the adsorbent material; transferring heat from a heat of adsorption on the adsorbent material along the at least a portion of thermally conductive filaments in a second axial direction towards the inlet end and opposite to the first axial direction during the adsorbing step; recovering a natural gas product stream depleted in at least one of carbon dioxide and hydrogen sulfide relative to the natural gas feed mixture from the outlet end; desorbing at least a portion of at least one of the carbon dioxide and hydrogen sulfide adsorbed on at least one the adsorbent material by heating the adsorbent material; transferring heat along at least a portion of the thermally conductive filaments in either of the first or second axial directions to provide at least a portion of the heat of desorption of the carbon dioxide or hydrogen sulfide during the desorbing step; and recovering a desorbed product enriched in at least one of carbon dioxide and hydrogen sulfide from at least one of the inlet and the outlet ends. The admitting, adsorbing, recovering a natural gas product stream, desorbing and recovering a desorbed product steps are substantially isobaric and are conducted at elevated super-atmospheric pressures. EXAMPLE - No suitable example given.