Abstract:
A method of using a catalyst body able to support gas flow therethrough and having a catalyst for promoting a catalytic reaction of a component of a first gas and being able to be regenerated by a second gas, comprising: providing at least the first gas and the second gas; and repeatedly moving successive parts of the catalyst body into communication with the first gas and then into communication with the second gas; wherein: the part of the catalyst body in communication with the first gas causes the component of the first gas to be reacted as the first gas passes though and exits the part of the catalyst body; and the part of the catalyst body in communication with the second gas has the catalyst of that part regenerated as the second gas passes through and exits the part.

Description:
CROSS-REFERENCE TO RELATED APPLICATION 
       [0001]    This application is a divisional of application Ser. No. 12/131,483, filed Jun. 2, 2008, which, in turn is a divisional of application Ser. No. 10/916,202, filed Aug. 11, 2004, now U.S. Pat. No. 7,381,488, the entire disclosures of which are hereby incorporated by reference. 
     
    
     BACKGROUND OF THE INVENTION 
       [0002]    This invention relates to oxidizer assemblies and, in particular, to oxidizer assemblies for use in proton exchange membrane (“PEM”) fuel cell applications. 
         [0003]    In copending application U.S. Ser. No. 10/894,993, filed Jul. 20, 2004, entitled OMS-2 Catalysts in PEM Fuel Cell Applications, there is disclosed an oxidizer assembly which utilizes an OMS (“octahedral molecular sieve”)- 2  catalyst to oxidize the carbon monoxide in the fuel feed to a PEM fuel cell. As described therein, OMS-containing materials, such as synthetic todorokite (Mg 2+   0.98-1.35 Mn 3+   1.89-1.94 Mn 4+   4.38-4.54 O 12  4.47-4.55H 2 O) or cryptomelane (K-hollandite, KMn 8 O 16 nH 2 O), comprise manganese oxide octahedral compounds linked by edges and vertices and forming uniform tunnels therethrough. OMS-2 catalysts are manganese oxide octahedral molecular sieves possessing the 2×2 tunnel structure (as in the aforementioned cryptomelane). 
         [0004]    The &#39;993 application specifically describes transition metal cation doped OMS-2 catalysts which can be framework-substituted and tunnel-substituted molecular sieves which are referred to by the designations [M]-OMS-2 and [M-OMS-2], respectively, where M indicates tunnel or framework-substituted metal cation(s) other than manganese. Specifically disclosed in the application as preferable catalysts are Co-OMS-2, Cu-OMS-2 and Ag-OMS-2, with Ag-OMS-2 being most preferable. 
         [0005]    The &#39;993 application also describes the operation of the OMS-2 catalyst to cause selective oxidation of the carbon monoxide in the feed to a PEM fuel-cell as occurring chemically via a sorption-chemical oxidation process aided by the unique pore structure and active sites of the catalyst. In particular, the sorption-chemical oxidation process at low temperatures is described as a two stage process, a sorption stage and a chemical oxidation stage. As stated therein, during the sorption stage, carbon monoxide is selectively adsorbed on the metal active side of the M-OMS-2 (Ag-OMS-2) catalyst as follows: 
         [0000]      Ag*+CO→CO ad   (1)
 
         [0006]    This process then proceeds to the chemical oxidation stage in which carbon monoxide is chemically oxidized with oxygen typically present in the OMS-2 tunnel or provided with the fuel feed or reformate gas. Specifically, oxygen from the OMS-2 tunnel is released in the following reaction: 
         [0000]      O-OMS-2→OMS- 2+½O   2   (2)
 
         [0000]    Subsequently, carbon monoxide is oxidized by reacting carbon monoxide with the released oxygen to produce carbon dioxide in the following reaction: 
         [0000]      CO ad +½O 2 →CO 2 +Ag*  (3)
 
         [0007]    Following the sorption-chemical oxidation reaction, the OMS-2 can be regenerated in situ by adding oxygen from a feed gas to produce an O-OMS-2 regenerative substrate. This reaction is as follows: 
         [0000]      OMS-2+½O 2 →O-OMS-2  (4)
 
         [0008]    The oxidizer assembly incorporating the OMS-2 catalyst is described in the &#39;993 application as being capable of performing the oxidation and the regeneration processes simultaneously. In particular, an oxidizer assembly is disclosed in which parallel packed bed reactors each having an M-OMS-2 catalysts are operated so that one reactor is performing carbon monoxide oxidation of the PEM fuel cell feed gas, while the other reactor is having its M-OMS-2 catalyst being regenerated. While this type of oxidizer assembly is usable, a more compact and simpler oxidizer assembly is desired. 
         [0009]    It is therefore an object of the present invention to provide an oxidizer assembly for oxidizing the carbon monoxide in a feed gas which is simple and compact in configuration. 
         [0010]    It is a further object of the present invention to provide an oxidizer assembly of the above-mentioned type which is also capable of allowing in situ catalyst regeneration without interrupting the oxidation of carbon monoxide. 
       SUMMARY OF THE INVENTION 
       [0011]    In accordance with the principles of the present invention, the above and other objectives are realized in an oxidizer assembly provided with a housing having a plurality of inlets each for receiving a different gas and a plurality of outlets. Each of the outlets corresponds to a different one of the inlets and outputs gas resulting from the gas received from its corresponding inlet. A catalyst assembly able to support gas flow therethrough is disposed within the housing and includes a catalyst able to oxidize carbon monoxide gas and to be regenerated. The catalyst assembly is further adapted to be movable such that successive parts of the assembly are able to be brought repeatedly in communication with a first inlet and its corresponding first outlet and then a second inlet and its corresponding second outlet of the housing. In the preferred form of the invention, the catalyst assembly is additionally adapted so that each section is brought in communication with a third inlet and its corresponding outlet after being in communication with the second inlet and its corresponding second outlet and prior to being brought back into communication with the first inlet and its corresponding outlet. 
         [0012]    In this way, by supplying a feed gas with carbon monoxide to be oxidized to the first inlet, an oxidant gas to the second inlet and a cooling gas to the third inlet, the following occurs with respect to each region of the catalyst assembly: when in communication with the first inlet, the region receives the feed gas and oxidizes the carbon monoxide in the feed gas as the feed gas passes therethrough to the first outlet; when in communication with the second inlet, the region receives the oxidant gas and as the oxidant gas passes therethrough to the second outlet the catalyst in the region is regenerated; and when in communication with the third inlet, the region receives the cooling gas and is cooled as the cooling gas passes to the third outlet. This process is then repeated as each region of the catalyst assembly is brought repeatedly in communication with the first, second and third inlets. 
         [0013]    In the form of the invention to be disclosed herein, the catalyst assembly comprises a porous body coated with an OMS-2 catalyst. Also, in a first embodiment of the invention to be disclosed herein, the porous catalyst body is rotatable within the housing and has first and second ends along its axis of rotation which abut and seal against, but rotate relative to, first and second sealing members, respectively. The first and second sealing members, in turn, abut first and second end walls of the housing which have the inlets and the outlets, respectively. In this case, the sealing members define at least first, second and third inlet manifolds which communicate with the first, second and third inlets, respectively, and corresponding first, second and third outlet manifolds which communicate with the first, second and third outlets, respectively, and at any given time the regions of the rotatable catalyst body in line with the respective inlet manifolds and their corresponding outlet manifolds are sealed from one another. As the catalyst body rotates, these regions change so that all parts of the catalyst body are repeatedly moved to communicate with the first, second and third inlet manifolds and thus the first, second and third inlets. 
         [0014]    In a second embodiment of the invention, the porous catalyst body is also rotatable within the housing and is configured to define regions sealed from each other and which at first and second ends along the axis of rotation of the catalyst body communicate with first and second end walls of the housing which have, respectively, the inlets and outlets of the housing. As the catalyst body rotates, the regions move so that they are brought repeatedly into communication with the first, second and third inlets, while remaining sealed from each other. 
         [0015]    In the above embodiments, the rotatable catalyst body is in the form of a honeycomb ceramic corderite structure with through passages. 
     
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         [0016]    The above and other features and aspects of the present invention will become more apparent upon reading the following detailed description in conjunction with the accompanying drawings, in which: 
           [0017]      FIG. 1  shows a PEM fuel cell system using an oxidizer assembly for oxidizing carbon monoxide in accordance with the principles of the present invention; 
           [0018]      FIG. 2  shows the oxidizer assembly of  FIG. 1  in greater detail; 
           [0019]      FIG. 3A  shows a cross-sectional view taken along the line  3 A- 3 A of  FIG. 2  of a first embodiment of the oxidizer assembly of  FIG. 2 ; 
           [0020]      FIG. 3B  shows a cross-sectional view taken along the line  3 B- 3 B of  FIG. 2  of the first embodiment of the oxidizer assembly of  FIG. 2 ; 
           [0021]      FIG. 3C  shows a cross-sectional view taken along the line  3 C- 3 C of  FIG. 2  of the first embodiment of the oxidizer assembly of  FIG. 2 ; 
           [0022]      FIG. 4A  shows a cross-sectional view taken along the line  4 A- 4 A of  FIG. 2  of a second embodiment of the oxidizer assembly of  FIG. 2 ; 
           [0023]      FIG. 4B  shows a cross-sectional view taken along the line  4 B- 4 B of  FIG. 2  of the second embodiment of the oxidizer assembly of  FIG. 2 ; 
           [0024]      FIG. 4C  shows a cross-sectional view taken along the line  4 C- 4 C of  FIG. 2  of the second embodiment of the oxidizer assembly of  FIG. 2 ; 
           [0025]      FIG. 5  shows a representation of a ceramic honeycomb corderite substrate for use in the oxidizer assembly of  FIG. 2 ; 
           [0026]      FIG. 6  shows an SEM representation of an Ag-OMS-2 catalyst coated on the substrate of  FIG. 5 ; 
           [0027]      FIG. 7  shows a graph of performance data of coated substrate samples of  FIG. 6  tested in a microreactor over a period of time; and 
           [0028]      FIG. 8  shows a diagram of the operation of the oxidizer assembly of  FIG. 2 . 
       
    
    
     DETAILED DESCRIPTION 
       [0029]      FIG. 1  shows a PEM fuel cell system in accordance with the principles of the present invention. As shown, the system  1  comprises a PEM fuel cell  2  having an anode section  2   a  and a cathode section  2   b  separated by a PEM  2   c . A fuel supply  3  provides a hydrocarbon fuel, such as, for example, natural gas, gasoline or methanol, to a reformer unit  4  which converts the hydrocarbon fuel to a PEM fuel feed or reformate which is rich in hydrogen. The fuel feed also contains substantial levels of carbon monoxide gas, typically greater than 20,000 ppm. 
         [0030]    The PEM fuel cell feed from the reformer  4  is then passed through a low temperature shift reactor  5  in which a portion of the carbon monoxide gas is converted to carbon dioxide, thereby reducing its level, typically to about 2,000 ppm. An oxidizer  6  follows the shift reactor and is adapted to oxidize a further portion of the remaining carbon monoxide in the PEM fuel cell feed so that the level of carbon monoxide is less than about 20 ppm. The resultant PEM fuel cell feed is then delivered from the oxidizer to the anode section  2   a  of the PEM fuel cell  2 , whereby the fuel undergoes electrochemical reaction with the oxidant supplied to the cathode section  2   a  of the fuel cell to thereby produce electrical energy. 
         [0031]    As is also shown, an oxidant supply assembly  7  supplies oxidant to the oxidizer  6  for regenerating the catalyst of the oxidizer. A cooling gas supply assembly  8  further supplies a cooling gas to the oxidizer for cooling the oxidizer. These operations will be further described hereinbelow. 
         [0032]    The oxidizer  6  is adapted to oxidize the carbon monoxide in the PEM fuel feed in such a manner as to readily handle transients in the level of carbon monoxide and with limited hydrogen consumption. This is realized, as discussed in the &#39;993 application by using an OMS-2 catalyst as an oxidizing catalyst in the oxidizer  6 . As previously discussed, OMS-2 catalysts are octahedral molecular sieves of, as, for example, cryptomelane (K-hollandite, KMn 8 O 16 nH 2 O). The OMS-2 catalysts thus comprise manganese oxide octahedral compounds linked by edges and vertices and forming uniform tunnels therethrough. As also previously discussed, metal cations may be incorporated in the tunnels of the OMS compounds. 
         [0033]    As stated in the &#39;993 application, the preferable OMS-2 catalysts for the oxidizer  6  are metal cation doped OMS-2 catalysts, i.e., M-OMS-2 catalysts. Preferable M-OMS-2 catalysts are Co-OMS-2, Cu-OMS-2 and Ag-OMS-2, with Ag-OMS-2 being most preferable. 
         [0034]      FIG. 2  illustrates a form of the oxidizer assembly  6  in accordance with the principles of the present invention. As shown in  FIG. 2 , the oxidizer assembly  6  includes a catalyst assembly  104  having a catalyst body  104   a  which is enclosed within a housing  102 . The housing  102 , shown as cylindrical, has a first end wall  106   a  and a second end wall  106   b . The first end wall  106   a  has a plurality of inlets  108   a ,  110   a  and  112   a  and the second end wall  106   b  a plurality of corresponding outlets  108   b ,  110   b  and  112   b.    
         [0035]    The inlets  108   a ,  110   a  and  112   a  are adapted to receive, respectively, the reformed fuel feed containing carbon monoxide from the shift reactor  5 , the oxidant gas from the oxidant supply  7  for regeneration of the catalyst of the catalyst body  104   a , and a cooling gas from the supply  8  for cooling the regions of the catalyst assembly which have had their catalyst regenerated. The outlets  108   b ,  110   b  and  112   b , in turn, convey from the housing the gases received in the corresponding inlets  108   a ,  110   a  and  112   a  after the gasses have passed through the catalyst assembly  104 . 
         [0036]    As also shown, the oxidizer assembly  6  includes a drive shaft  114  for rotating the catalyst body  104   a . This rotation brings each region of the catalyst body repeatedly into communication with the inlets  108   a ,  110   a  and  112   a  and their corresponding outlets  108   b ,  110   b  and  112   b.    
         [0037]    As can be appreciated, therefore, at any given time, the catalyst body  104   a  is simultaneously oxidizing carbon monoxide gas in the fuel feed in a first region of the body communicating with the inlet  108   a  and its corresponding outlet  108   b , is having its catalyst regenerated by oxidant gas received in a second region of the body communicating with the inlet  110   a  and its corresponding outlet  110   b , and is being cooled by a cooling gas in a third region of the body communicating with the inlet  112   a  and its corresponding outlet  112   b . Moreover, as will be discussed in greater detail hereinbelow, the catalyst assembly  104  is further adapted such that the aforementioned first, second and third regions of the catalyst body are sealed from one another so that the gases delivered to and exiting from these regions do not mix with each other. Additionally, as the catalyst body rotates, the regions change so that all parts of the catalyst body come into communication with the first, second and third inlets and this process is continuously repeated. 
         [0038]      FIGS. 3A-3C  illustrate detailed cross-sectional views of a first embodiment of the oxidizer assembly  6  of  FIG. 2 . These cross-sections are taken along the lines  3 A- 3 A,  3 B- 3 B and  3 C- 3 C of  FIG. 2 . As shown in  FIGS. 3A and 3B , the catalyst body  104   a  of the catalyst assembly is a one-piece substantially cylindrical porous structure with a circular cross-section. In the present case, the catalyst body is made porous via apertures  104   ac  extending therethrough between a first end  104   aa  and an opposing second end  104   ab  of the body. The catalyst body is also attached to the shaft  114  so as to be rotatable within the cylindrical housing  102 . Typically, the housing  102  can be formed as a stainless steel canister and the catalyst body  104   a  as a ceramic honeycomb corderite monolith or structure having a catalyst coating, as described in more detail below. 
         [0039]    The first and second end walls  106   a  and  106   b  of the housing  102  are formed as separate covers which fit into the respective open opposite ends of the housing  102  so as to close the housing and cover the catalyst body  104   a  and other components of the assembly  6  contained within the housing. In the particular case shown, each end wall  106   a ,  106   b  extends a short distance into the housing along the housing inner wall so as to fully cover the respective opening. Each end wall can typically be formed from a glass filled Teflon® material, although other high-temperature polymer materials, such as Viton® or PVA-based rubber, can also be used. 
         [0040]    As is also shown, the drive shaft  114  passes through the length of oxidizer assembly  6  from the outer surface of the second end wall  106   b  to above the outer surface of the end wall  106   a . The shaft is rotatably held and the catalyst body  104   a  is attached to the shaft so as to rotate therewith. Accordingly as the shaft is rotated by an actuator assembly (not shown) engaging the end of the shaft extending beyond the first end wall  106   a , the catalyst body  104   a  also rotates within the housing  102 . 
         [0041]    In the present case, the catalyst assembly  104  further comprises a first sealing member  116   a  followed by a first gasket member  118   a  positioned between the first end  104   aa  of the catalyst body  104   a  and the first end wall  106   a , and a second sealing member  116   b  followed by a second gasket member  118   b  positioned between the second end  104   ab  of the catalyst body  104   a  and the second end wall  106   b . The sealing member  116   a , the gasket member  118   a  and the end wall  106   a  are held together by a plurality of fastening members  120   a . Like fastening members  120   b  hold the sealing member  116   b , the gasket member  118   b  and the top plate  106   b  together. As can be appreciated, the combined unit of each end wall, gasket member and sealing member is fixed in place with respect to the container unit  102  and is not driven by the driving shaft  114 . 
         [0042]    Each gasket member  118   a ,  118   b  is disc shaped and includes three through openings aligned with the inlets or outlets in the adjacent end wall. In particular, as shown in  FIG. 3C , the gasket member  118   a  includes through openings  126   a ,  128   a  and  130   a  aligned with the openings  108   a ,  110   a ,  112   a  in the first end wall  106   a . The gasket member  118   b  similarly is disc shaped and includes three through openings  126   b ,  128   b  and  130   b  (not visible) aligned with the openings  108   b ,  110   b  and  112   b  in the second end wall  106   b.    
         [0043]    In the case shown, the inlets  108   a ,  110   a  and  112   a  are circular and of the same size. Likewise, the outlets  108   b ,  110   b  and  112   b  are circular and of the same size as each other and as the inlets. Additionally, each of the through openings  126   a ,  126   b ,  128   a ,  128   b ,  130   a  and  130   b  is circular and of the same size as the adjacent inlet or outlet. It should be noted, however, that the inlets, outlets and openings need not all be of the same size and shape and that these parameters can be varied depending upon the particular application and circumstances. 
         [0044]    The sealing members  116   a  and  116   b  define first, second and third inlet manifolds and corresponding first, second and third outlet manifolds which are sealed from each other and which communicate with the respective through openings and inlets and outlets in the adjoining gasket members and end walls. At any given time, the three inlet manifolds and corresponding three outlet manifolds encompass three adjacent regions of the catalyst body  104   a  so that the gases passing into, through and out of each region are sealed form each other and do not mix. 
         [0045]    As shown in  FIG. 3C , the sealing member  116   a  defines three inlet manifolds  122   a ,  124   a  and  132   a  which are sealed from each other and align with the through openings  126   a ,  128   a  and  130   a  in the gasket  118   a  and the inlets  108   a ,  110   a  and  112   a  in the end wall  106   a . The sealing member  116   b  is similar and defines three outlet manifolds  122   b ,  124   b  and  132   b  (not visible) which are sealed from each other and align with the through openings  126   b ,  128   b  and  130   b  in the gasket  118   b  and the outlets  108   b ,  110   b  and  112   b  in the end wall  106   b.    
         [0046]    In the illustrated case, the sealing member  116   a  comprises a circular outer part in the form of a ring  116   aa  which abuts the portion of the end wall  106   a  adjacent the inner wall of the housing  102 . An inner part  116   ab  of the sealing member is Y-shaped and has three segments or arms  116   ac ,  116   ad  and  116   ae  which extend radially inward from the ring  116   aa  to a central hub part  116   af  through which the shaft  114  passes. As can be appreciated, the open regions between the arms  116   ac - 116   ae  define the inlet manifolds  122   a ,  124   a  and  132   a . The sealing member  116   b  is similarly constructed thus defining the corresponding outlet manifolds  122   b ,  124   b  and  132   b.    
         [0047]    With this design for the sealing members, at any given time, three regions of maximum area of the catalyst body  104   a  are exposed, respectively, to the three inlets  108   a ,  110   a  ad  112   a  and their corresponding outlets  108   b ,  110   b  and  112   b  of the oxidizer assembly and these three regions are sealed from each other by the sealing members  116   a  and  116   b . As a result, the catalyst body is simultaneously oxidizing the fuel feed from the shift reactor  5  in a first region in communication with the inlet manifold  122   a , having its catalyst regenerated by the oxidant gas from the oxidant supply  7  in a second region in communication with the inlet manifold  124   a , and being cooled by the cooling gas from the supply  8  in third region in communication with the inlet manifold  132   a . Moreover, as the catalyst body is rotated, the areas of the catalyst body  104   a  forming the three sealed regions change so that all the areas of the body perform oxidation, are regenerated, and then are cooled in sequence and the process is then repeated. 
         [0048]    A typical material for the gasket members  118   a ,  118   b  is Teflon®. The sealing members  116   a ,  116   b , in turn, can be formed from Viton®. 
         [0049]      FIGS. 4A-4C  illustrate detailed cross-sectional views of a second embodiment of the oxidizer assembly  6  of  FIG. 2 . These cross-sections are taken along the lines  4 A- 4 A,  4 B- 4 B and  4 C- 4 C of  FIG. 2 . This embodiment uses a similar housing, end walls, gaskets and rotating shaft as in the embodiment of  FIGS. 3A-3C  and these components have been similarly numbered. In this case, however, the sealing members  116   a  and  116   b  are not used and the sealing function is realized with catalyst body  104   a  itself. 
         [0050]    More particularly, as can be seen the catalyst body is segmented into three separate regions  104   ac ,  104   ad , and  104   ae . These regions are carried by a Y-shaped sealing frame  115  which, typically, can be formed from, for example, Teflon® and/or Viton®. The frame  115  has a central hub  115   a  which is attached to the shaft  114  so that the frame and, therefore, the catalyst regions, can be rotated relative to the housing  102 . Extending from the central hub are three arms  115   b ,  115   c  and  115   d  which extend radially outwardly from the hub to the end wall adjacent the inner wall of the housing  102 . The arms  115   b - 115   d  additionally extend along the length of the housing from the gasket member  118   a  to the gasket member  118   b , which as shown are thicker in this embodiment than in the embodiment of  FIGS. 3A-3C . With this configuration for the arms, the catalyst regions  104   ac - 104   ae  are wedge shaped to fit the wedge shaped areas defined by the regions between successive arms. 
         [0051]    The arms  115   b - 115   d  of the Y-shaped frame  115  in this embodiment act as seals to prevent gas being introduced into or exiting from the catalyst regions  104   ac - 104   ae  from mixing with each other. At any given time, therefore, each of the sealed regions  104   ac - 104   ae  is in communication with a different one of the inlets  108   a ,  110   a ,  112   a  and their corresponding outlets  108   b ,  110   b  and  112   b  of the oxidizer assembly. As a result, like the embodiment of the oxidizer assembly of  FIGS. 3A-3C , the assembly of  FIGS. 4A-4C  is simultaneously oxidizing fuel feed from the reactor  5  in a first region in communication with the inlet  108   a , is being regenerated by the oxidant gas from the supply  7  in a second region in communication with the inlet  110   a , and is being cooled by the cooling gas from the cooling gas supply  8  in a third region in communication with the inlet  112   a . Also, as the catalyst body  104   a  is rotated, the three regions are moved so that each communicates with the different inlet and outlet pairs sequentially. Continued rotation of the body  104   a  then repeats this process. 
         [0052]    In the embodiment of the oxidizer assembly of  FIGS. 4A-4C , the catalyst body is divided or segmented into three equal sections. However, the number as well as the dimensions of each section can be varied. Changing the number and/or dimensions of the catalyst body sections will of course require a corresponding change in the number and/or the angular spacing of the arms of the sealing member  115 . 
         [0053]    As discussed above, the catalyst body  104   a  can be formed from a ceramic honeycomb corderite substrate coated with a catalyst, preferably an M-OMS-2 catalyst.  FIG. 5 . shows an example of a ceramic honeycomb monolith or substrate of corderite material manufactured by Emprise Corporation which is suitable for use as the body  104   a . As can be seen in  FIG. 5 , the substrate  501  has a substantially cylindrical shape and a plurality of pores or cells  501   a  extending through the length of the substrate. The pores  501   a  form a plurality of channels through the length of the substrate  501  so as to allow gas or liquid to pass from one end to the other. 
         [0054]    An example of a substrate  501   a  for use in the oxidizer of  FIGS. 3A-3C , is a substrate which is approximately 0.750 inches in diameter and 3 inches in length, and having a cross-section with approximately 300 to 500 pores or cells per square inch. The cylindrical substrate  501  may also be divided into several wedge-shaped segments and used in the embodiment of the oxidizer  6  in  FIGS. 4A-4C . 
         [0055]    As also mentioned above, the corderite substrate is coated with an M-OMS-2 catalyst to provide the desired catalyst body  104   a . This may be accomplished by applying the M-OMS-2 catalyst to the ceramic honeycomb corderite substrate using a catalyst binder solution. A typical binder solution comprises the M-OMS-2 catalyst powder dispersed in a commercially available wetting agent, such as TFE Teflon®. A commercially available inking agent, such as Polyox™ WSR-301 manufactured by Union Carbide Corporation, may be added to increase the viscosity of the binder solution. 
         [0056]    Prior to the application of the catalyst binder solution to the substrate, it is desirable to pre-wet the corderite material with deionized water to allow for better flow of the catalyst suspension through the corderite and to delay the absorption of liquid in the binder solution by the corderite. Additionally, pre-wetting the corderite substrate before applying the catalyst allows for larger amounts of catalyst to be held by the substrate than if the catalyst binder solution was applied to the substrate when dry. The binder solution is applied to the corderite substrate by a dipping method or a spraying method so as to coat the inner and outer surfaces of the corderite substrate. 
         [0057]      FIG. 6  shows an SEM representation of an Ag-OMS-2 catalyst coated onto a honeycomb corderite substrate. As can be seen, the catalyst coating is uniformly distributed on the surface of the substrate. 
         [0058]    Catalyst coated honeycomb corderite substrate samples for the catalyst body  104   a  have been prepared with approximately 0.44 to 0.51 grams of M-OMS-2 catalyst. In addition, it is further desirable that the resulting M-OMS-2 catalyst coating on the substrate comprise approximately 4% binder by weight, and that the capacity of the catalyst is approximately 0.125% by weight of carbon monoxide per gram of catalyst. 
         [0059]    Catalyst coated honeycomb corderite samples prepared as above set forth were tested in a micro-reactor bed.  FIG. 7  shows a graph of performance data of the coated substrate samples tested using a simulated reformate fuel gas. The simulated reformate gas comprised 2235 ppm of carbon monoxide, 75% hydrogen, 25% carbon dioxide and 2000 ppm oxygen gas. During the testing, the simulated reformate gas was passed through the samples at 100° Celsius with a space velocity of 500 h −1 . As shown in  FIG. 7 , the samples tested were capable of converting approximately 85% of carbon monoxide to carbon dioxide, and after approximately 250 minutes of operation, the samples were converting over 50% of carbon monoxide in the simulated reformate. 
         [0060]    After being exposed to the simulated reformate gas, these coated samples had their catalyst regenerated by passing through the samples a regeneration gas comprising oxygen at 150° Celsius for 30 minutes. After each regeneration cycle, approximately 85% carbon monoxide conversion was maintained, demonstrating that the catalyst of the coated substrate was able to be fully regenerated after being exposed to the regeneration gas. 
         [0061]      FIG. 8  illustrates schematically a typical operating sequence for the oxidizer assembly  6  of  FIGS. 2 ,  3 A- 3 C and  4 A- 4 C where the catalyst used is an M-OMS-2 catalyst. As shown, the oxidizer assembly  6  is characterized as having a reactor zone  136  (defined by the inlet  108   a  of the assembly  6  and the corresponding outlet  108   b  of the assembly  6  and the region of the catalyst body  104   a  communicating therewith), a regenerator zone  138  (defined by the inlet  110   a  and the corresponding outlet  110   b  of the assembly  6  and the region of the catalyst body  104   a  communicating therewith) and a heat management or cooling zone  140  (defined by the inlet  112   a  and the corresponding outlet  112   b  of the assembly  6  and the region of the catalyst body  104   a  communicating therewith). 
         [0062]    In operation, a reformate or fuel feed comprising more than 2000 ppm of carbon monoxide from the reactor  5  is passed through the reactor zone  136 , where the carbon monoxide in the reformate gas is converted to carbon dioxide. Particularly, conversion of the carbon monoxide occurs via a sorption-chemical oxidation process which is carried out in two stages, a sorption stage and a chemical oxidation stage. During the sorption stage, carbon monoxide is selectively adsorbed on the metal active side of the M-OMS-2 catalyst as follows: 
         [0000]      M*+CO→CO ad   (5)
 
         [0063]    The chemical oxidation stage follows the sorption stage, and during this stage carbon monoxide is chemically oxidized with oxygen present in the OMS tunnels of the catalyst coating and/or provided in the reformate gas. Specifically, oxygen is released from the OMS tunnel and carbon monoxide is oxidized by reacting carbon monoxide with the released oxygen to produce carbon dioxide, as follows: 
         [0000]      O-OMS-2→OMS-2+½O 2   (6)
 
         [0000]      CO ad +½O 2 →CO 2 +Ag*  (7).
 
         [0064]    In the operation illustrated in  FIG. 8 , the above-described sorption-chemical oxidation reaction is carried out at 100° Celsius. Oxidized reformate gas leaving the reactor zone of the oxidizer assembly  6  comprises hydrogen rich gas with less than 10 ppm carbon monoxide and is suitable for use in the anode  2   a  of the PEM fuel cell  2 . 
         [0065]    As the region of the oxidizing assembly  6  oxidizes the carbon monoxide in the fuel feed, the catalyst in the region becomes exhausted or depleted. Rotation of the catalyst body  104   a  brings the region to the regenerator zone  138 . In the regenerator zone, oxidant from the oxidant supply  7  is passed through the region, whereby the spent oxygen in the catalyst coating of that region is replaced. More particularly, oxygen supply in the M-OMS-2 tunnels of the catalyst coating is replenished through the following reaction: 
         [0000]      OMS-2+½O 2 O-OMS-2  (8).
 
         [0066]    As shown, this regeneration process is carried out at 150-200° Celsius for approximately 15 to 30 minutes. 
         [0067]    Before the regenerated region in the catalyst body  104   a  may be used again in the reactor zone  136 , the temperature of the region has to be adjusted to correspond to the temperature of the zone. Accordingly, after undergoing regeneration in the regenerator zone  138 , the rotation of the catalyst body  104   a  brings the regenerated region to the heat management zone  140 . 
         [0068]    In the heat management zone  140 , the regenerated region of the catalyst body  104   a  is exposed to the cooling gas from the cooling gas supply  8  to reduce the temperature of the region to that of the reactor zone, i.e., to about 100° Celsius in the illustrated case of  FIG. 8 . In this case also, air at 100° Celsius may be used as the cooling gas. When the region is cooled to approximately 100° Celsius, it is ready to process additional reformate or fuel feed gas from the reactor  5  and continued rotation of the catalyst body  104   a  brings the cooled region back into the reaction zone  136 . 
         [0069]    As can be appreciated, the rotation of the catalyst body  104   a  can be continuous or intermittent depending upon the application. Also, in the case of the second embodiment shown in  FIGS. 4A-4C , the sizing of the inlets and the outlets and the sizing of the sealed regions has to be such that at any given time each region communicates with only one inlet and its corresponding outlet. This prevents two gases from being supplied to a given region and a mixing of the gases. 
         [0070]    In all cases it is understood that the above-described arrangements are merely illustrative of the many possible specific embodiments which represent applications of the present invention. Numerous and varied other arrangements can be readily devised in accordance with the principles of the present invention without departing from the spirit and scope of the invention.