TECHNOLOGY FOCUS - CHEMICAL ENGINEERING - Preferred Component: The reactor contains a first bed, an intermediate bed downstream of the first bed and a second bed downstream of the intermediate bed.The first bed contains the first adsorbent, the second bed contains a mixture of the second adsorbent and the shift catalyst, and the intermediate bed contains the shift catalyst.The second bed is packed with solid particles comprising the second adsorbent and the shift catalyst.The pressurization gas comprises the purge gas and/or the feed gas.The first adsorbent is identical to the second adsorbent.Preferred Method: The mixture of the second adsorbent and the shift catalyst in the second bed are provided by, packing the second bed with the solid particles without mixing.The first and second adsorbents are regenerated by, decreasing a gas pressure of the reactor and purging the reactor with a purge gas free of carbon dioxide.The process further comprises conveying the product gas to a methanator to reduce the carbon monoxide concentration in the product gas to less than 50 parts per million (ppm); conveying the product gas to a pressure swing adsorption unit to increase hydrogen concentration of the product gas to at least 99 vol.%; counter currently purging the reactor at feed gas pressure with purge gas before regenerating the first and second adsorbents to yield an effluent stream containing unreacted carbon monoxide and water; recycling the effluent stream to the feed gas stream to produce a carbon dioxide and carbon monoxide depleted product stream with enhanced hydrogen recovery; concurrently rinsing the reactor at feed gas pressure with carbon dioxide product before regenerating the first and second adsorbents to produce a carbon dioxide and carbon monoxide depleted product stream with enhanced hydrogen recovery and recover a carbon dioxide-rich byproduct stream during the regenerating step.The process is conducted in a series of cycles in more than one reactor.A reactor is being regenerated while another is being operated in parallel to produce the product gas.Preferred Condition: The first adsorbent is identical to the second adsorbent.The feed gas is fed into the reactor at a flow rate of 5-50 gmole/hr/cm2.The reactor temperature during the process is maintained at 175-550degreesC.A volume fraction of the mixture in the second bed varies as a function of location in the second bed such that a shift catalyst concentration gradient is provided.Preferred Function: The purge gas from the pressure swing adsorption unit is used to purge the reactor.The carbon dioxide and carbon monoxide depleted product stream is used to generate power in a gas fired turbine system.    TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Catalyst: The shift catalyst comprises cupric oxide/zinc oxide based shift catalysts, ferric oxide/chromium oxide based shift catalysts, and/or shift catalysts containing noble metals.Preferred Component: The purge gas comprises steam and/or a steam/hydrogen mixture.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Composition: The feed gas comprises hydrogen (25-75 vol.%); water (10-50 vol.%); carbon monoxide (1-20 vol.%); carbon dioxide (1-20 vol.%); nitrogen (0-50 vol.%); and methane (0.1-5 vol.%).Preferred Component: The feed gas is a syngas effluent from a steam methane reformer, partial oxidation reactor, air-blown autothermal reformer, oxygen-blown autothermal reformer upstream of the reactor, or a high temperature shift reactor.Raw syngas to the high temperature shift reactor is obtained from a steam methane reformer, partial oxidation reactor, air-blown autothermal reformer or oxygen-blown autothermal reformer upstream of the reactor.    TECHNOLOGY FOCUS - MECHANICAL ENGINEERING - Preferred Apparatus: The apparatus further comprises an adiabatic vessel in which the first bed, the intermediate bed and the second bed are packed as consecutive layers; steam methane reformer, partial oxidation reactor or autothermal reformer in fluid communication with the feed gas inlet; a high temperature shift reactor in fluid communication with the feed gas inlet and the steam methane reformer, partial oxidation reactor or autothermal reformer; a methanator in fluid communication with the product gas outlet to reduce the carbon monoxide concentration in the product gas to less than 50 ppm; a hydrogen fuel cell in fluid communication with the methanator; and a pressure swing adsorption unit adapted to increase a hydrogen concentration of the product gas to at least 99 vol.%, and to provide purge gas to the reactor.Preferred Condition: There are adiabatic vessels that operate in parallel with each other. EXAMPLE - A syn gas comprising hydrogen (49.53%); water (34.80%); carbon monoxide (9.36%); carbon dioxide (5.36%); and methane (1.44%) was fed in a shift SER reactor at 375degreesC and pressure of 2.07 MPa. During the reaction step, bulk carbon dioxide in the feed gas was removed by adsorption, the shift reaction was catalyzed to form carbon dioxide and hydrogen from carbon monoxide and steam. Carbon dioxide was continually removed from the reaction product by adsorption onto the high temperature adsorbent. The process gas leaving the first bed comprised hydrogen (52.34%; water (36.78%); carbon monoxide (9,89%); and methane (0.99%). The product mixture from the intermediate bed contained hydrogen (61.05%); water (28.06%); carbon monoxide (1.18%); carbon dioxide (8.71%), and methane (0.99%). Removal of carbon dioxide in the second bed drove the shift reaction to high conversion, giving a product containing very low levels of carbon oxides.