Abstract:
A simplified PEM fuel cell system is integrated with a fuel processor and an exhaust gas oxidizer to ensure clean emissions. The fuel cell can have an operating temperature of 120-200° C. Cathode exhaust of a PEM fuel cell is used to provide steam and oxygen to a fuel processing reactor to convert a hydrocarbon fuel to hydrogen, wherein the hydrogen is provided to a fuel cell.

Description:
CROSS REFERENCE TO RELATED APPLICATIONS  
       [0001]    This application claims priority under 35 USC 119(e) from U.S. Provisional Application No. 60/287,207, filed Apr. 27, 2001, naming Cutright, et al. as inventors, and titled “INTEGRATED HIGH TEMPERATURE PEM FUEL CELL SYSTEM.” That application is incorporated herein by reference in its entirety and for all purposes. 
     
    
     GOVERNMENT INTEREST  
       [0002] The Government of the United States of America has rights in this invention pursuant to Contract No. NIST-70NAN8H4039 awarded by the U.S. Department of Commerce, National Institute of Standards and Technology. 
     
    
     
       BACKGROUND  
         [0003]    The invention generally relates to an integrated high temperature PEM fuel cell system.  
           [0004]    A fuel cell is an electrochemical device that converts chemical energy produced by a reaction directly into electrical energy. For example, one type of fuel cell includes a polymer electrolyte membrane (PEM), often called a proton exchange membrane, that permits only protons to pass between an anode and a cathode of the fuel cell. At the anode, diatomic hydrogen (a fuel) is reacted to produce protons that pass through the PEM. The electrons produced by this reaction travel through circuitry that is external to the fuel cell to form an electrical current. At the cathode, oxygen is reduced and reacts with the protons to form water. The anodic and cathodic reactions are described by the following equations: 
           H 2 →2H + +2 e   −  at the anode of the cell, 
           [0005]    and 
           O 2 +4H + +4 e   − →2H 2 O at the cathode of the cell. 
           [0006]    A typical fuel cell has a terminal voltage of up to one volt DC. For purposes of producing much larger voltages, several fuel cells may be assembled together to form an arrangement called a fuel cell stack, an arrangement in which the fuel cells are electrically coupled together in series to form a larger DC voltage (a voltage near 100 volts DC, for example) and to provide more power.  
           [0007]    The fuel cell stack may include flow plates (graphite composite or metal plates, as examples) that are stacked one on top of the other. The plates may include various surface flow channels and orifices to, as examples, route the reactants and products through the fuel cell stack. Several PEMs (each one being associated with a particular fuel cell) may be dispersed throughout the stack between the anodes and cathodes of the different fuel cells. Electrically conductive gas diffusion layers (GDLs) may be located on each side of each PEM to act as a gas diffusion media and in some cases to provide a support for the fuel cell catalysts. In this manner, reactant gases from each side of the PEM may pass along the flow channels and diffuse through the GDLs to reach the PEM. The PEM and its adjacent pair are often assembled together in an arrangement called a membrane electrode assembly (MEA).  
           [0008]    A fuel cell system may include a fuel processor that converts a hydrocarbon (natural gas or propane, as examples) into a fuel flow for the fuel cell stack. Exemplary fuel processor systems are described in U.S. Pat. Nos. 6,207,122, 6,190,623, 6,132,689, which are hereby incorporated by reference.  
           [0009]    The two reactions which are generally used to convert a hydrocarbon fuel into hydrogen are shown in equations (3) and (4). 
           1/2O 2 +CH 4 --&gt;2H 2 +CO  (3) 
           H 2 O+CH 4 --&gt;3H 2 +CO  (4) 
           [0010]    The reaction shown in equation (3) is sometimes referred to as catalytic partial oxidation (CPO). The reaction shown in equation (4) is generally referred to as steam reforming. Both reactions may be conducted at a temperature from about 600-1,100° C. in the presence of a catalyst such as platinum. A fuel processor may use either of these reactions separately, or both in combination. While the CPO reaction is exothermic, the steam reforming reaction is endothermic. Reactors utilizing both reactions to maintain a relative heat balance are sometimes referred to as autothermal (ATR) reactors. It should be noted that fuel processors are sometimes generically referred to as reformers, and the fuel processor output gas is sometimes generically referred to as reformate, without respect to which reaction is employed.  
           [0011]    As evident from equations (3) and (4), both reactions produce carbon monoxide (CO). Such CO is generally present in amounts greater than 10,000 parts per million (ppm). Because of the high temperature at which the fuel processor is operated, this CO generally does not affect the catalysts in the fuel processor. However, if this reformate is passed to a prior art fuel cell system operating at a lower temperature (e.g., less than 100° C.), the CO may poison the catalysts in the fuel cell by binding to catalyst sites, inhibiting the hydrogen in the cell from reacting. In such systems it is typically necessary to reduce CO levels to less than 100 ppm to avoid damaging the fuel cell catalyst. For this reason the fuel processor may employ additional reactions and processes to reduce the CO that is produced. For example, two additional reactions that may be used to accomplish this objective are shown in equations (5) and (6). The reaction shown in equation (5) is generally referred to as the shift reaction, and the reaction shown in equation (6) is generally referred to as preferential oxidation (PROX). 
           CO+H 2 O--&gt;H 2 +CO 2   (5) 
           CO+1/2O 2 --&gt;CO 2   (6) 
           [0012]    Various catalysts and operating conditions are known for accomplishing the shift reaction. For example, the reaction may be conducted at a temperature from about 300-600° C. in the presence of supported platinum. Other catalysts and operating conditions are also known. Such systems operating in this temperature range are typically referred to as high temperature shift (HTS) systems. The shift reaction may also be conducted at lower temperatures such as 100-300° C. in the presence of other catalysts such as copper supported on transition metal oxides. Such systems operating in this temperature range are typically referred to as low temperature shift (LTS) systems. Other catalysts and operating conditions are also known. In a practical sense, typically the shift reaction may be used to lower CO levels to about 1,000-10,000 ppm, although as an equilibrium reaction it may be theoretically possible to drive CO levels even lower.  
           [0013]    The PROX reaction may also be used to further reduce CO. The PROX reaction is generally conducted at lower temperatures than the shift reaction, such as 100-200° C. Like the CPO reaction, the PROX reaction can also be conducted in the presence of an oxidation catalyst such as platinum. The PROX reaction can typically achieve CO levels less than 100 ppm (e.g., less than 50 ppm).  
           [0014]    In general, fuel cell power output is increased by raising fuel and air flow to the fuel cell in proportion to the stoichiometric ratios dictated by the equations listed above. Thus, a controller of the fuel cell system may monitor the output power of the stack and based on the monitored output power, estimate the fuel and air flows required to satisfy the power demand. In this manner, the controller regulates the fuel processor to produce this flow, and in response to the controller detecting a change in the output power, the controller estimates a new rate of fuel flow and controls the fuel processor accordingly.  
           [0015]    The ratio of fuel or air provided to a fuel cell over what is theoretically required by a given power demand is sometimes referred to as “stoich”. For example, 1 anode stoich refers to 100% of the hydrogen theoretically required to meet a given power demand, whereas 1.2 stoich refers to 20% excess hydrogen over what is theoretically required. Since in real conditions it is typical that not all of the hydrogen or air supplied to a fuel cell will actually react, it may be desirable to supply excess fuel and air to meet a give power demand.  
           [0016]    The fuel cell system may provide power to a load, such as a load that is formed from residential appliances and electrical devices that may be selectively turned on and off to vary the power that is demanded. Thus, in some applications the load may not be constant, but rather the power that is consumed by the load may vary over time and change abruptly. For example, if the fuel cell system provides power to a house, different appliances/electrical devices of the house may be turned on and off at different times to cause the load to vary in a stepwise fashion over time.  
           [0017]    There is a continuing need for integrated fuel cell systems designed to achieve objectives including the forgoing in a robust, cost-effective manner.  
         SUMMARY  
         [0018]    In general, the invention provides integrated fuel cell systems and associated operation methods where water vapor in the cathode exhaust of a high temperature PEM fuel cell is used to provide steam utilized by a fuel processor providing hydrogen to the fuel cell.  
           [0019]    As an example, in one embodiment of the invention, a fuel cell system includes a PEM fuel cell with an operating temperature of at least 120° C. The fuel cell has a cathode inlet and a cathode outlet. The system includes a cathode blower with an electrical connection to a controller, and the cathode blower is adapted to vary a flow of air through the fuel cell from the cathode inlet to the cathode outlet according to a first control signal from the controller.  
           [0020]    The PEM used in the fuel cell stack can be based on the PBI membrane available from Celanese. U.S. patents describing this material include U.S. Pat. Nos. 5,525,436, 6,099,988, 5,599,639, and 6,124,060, which are each incorporated herein by reference. The term “high temperature PEM fuel cell” refers to a fuel cell that is operated at a temperature above 100° C., and that utilizes a polymer electrolyte membrane to support the fuel cell reaction. It should be noted that phosphoric acid, molten carbonate, alkaline and solid oxide fuel cell systems, which all operate at temperatures above 100° C., are not considered PEM systems since they do not utilize a polymer electrolyte membrane. Polybenzimidazole (PBI) and polyether ether ketone (PEEK) based fuel cell systems are considered high temperature PEM fuel cell systems, as examples. In some embodiments, the fuel cell stack can be operated at a temperature between 150-200° C. In still other embodiments, the fuel cell stack can be operated at a temperature between 160-180° C.  
           [0021]    A fuel processing reactor has an inlet and an outlet, the inlet and outlet being in fluid communication with a catalyst suitable for converting a hydrocarbon into a gas containing hydrogen and carbon monoxide, and the outlet being in fluid communication with an anode chamber of the fuel cell. A fuel blower has an electrical connection to the controller, and the fuel blower is adapted to vary a flow of fuel through the reactor according to a second control signal form the controller. The cathode outlet is in fluid communication with the reactor inlet in order to provide water vapor to the reactor.  
           [0022]    Various embodiments of the invention can include the following features, alone or in combination. The fuel cell can have an operating temperature in the range 160-200° C. The PEM of the fuel cell can comprise a polybenzimidazole material. The cathode blower can be adapted to flow ambient air directly through the fuel cell (i.e., the air is not humidified prior to entering the fuel cell). The controller can be adapted to modulate the first control signal to maintain a molar ratio of oxygen to methane in the reactor inlet, the ratio being in the range 0.4-0.7. The controller can also be adapted to modulate the second control signal to prevent hydrogen starvation in the fuel cell. It will be appreciated that hydrogen starvation refers to the condition when there is not enough hydrogen available to the fuel cell that can be reacted to provide the power demanded by a given electrical load. The controller can also be adapted to measure a voltage of the fuel cell stack and modulate the second control signal in response to the voltage measurement (e.g., if the voltage falls below a desired threshold indicating that additional hydrogen is needed to supply a given electrical load).  
           [0023]    The system can further include a mixing vessel having a first inlet adapted to receive an air flow from the cathode outlet, a second inlet adapted to receive a fuel flow from the fuel blower, and an outlet adapted to flow a mixture of the air flow and fuel flow into the fuel processing reactor. The mixing vessel can further comprise a third inlet adapted to receive a flow of ambient air. The mixing vessel can further comprise a fourth inlet adapted to receive a flow of steam.  
           [0024]    The carbon monoxide flowed from the fuel processing reactor to the fuel cell can have a concentration of at least 1,000 parts per million (e.g. 3,000-8,000 parts per million, or more). In another feature, as the cathode exhaust is flowed from the cathode outlet to the reactor inlet, the exhaust can be maintained at a temperature over 100° C. to keep the water in the exhaust in the vapor phase. In another feature, the cathode outlet can be connected to a conduit that is connected to the reactor inlet, where the conduit includes a by-pass vent so that a portion of the cathode exhaust can be selectively flowed to the fuel processor.  
           [0025]    In another aspect, the invention provides a method of operating a fuel cell system including the following steps: operating a first blower according to a first control signal to vary a flow of air through a cathode chamber of a fuel cell; reacting a portion of the air in the fuel cell to produce electricity; exhausting a remaining portion of the air from the fuel cell, wherein the remaining portion of air contains water vapor; mixing a portion of the exhausted air with a hydrocarbon gas to form a feed mixture; modulating the first control signal to maintain a predetermined amount of oxygen in the feed mixture; operating a second blower according to a second control signal to flow the feed mixture into a reactor where the feed mixture is contacted with a catalyst suitable for converting a portion of the hydrocarbon gas into a fuel gas containing hydrogen and carbon monoxide; flowing the fuel gas into an anode chamber of the fuel cell; and modulating the second control signal to maintain a predetermined amount of hydrogen in the fuel cell.  
           [0026]    In addition, such embodiments may also contain methods of operating a fuel cell system, embodying any of the following steps and features, either alone or in combination. The operating temperature of the fuel cell can be maintained in the range 120-200° C. The fuel cell can comprise a polybenzimidazole PEM. The first blower can be adapted to flow ambient air directly through the fuel cell. The hydrocarbon gas can comprises methane, and the method further include modulating the first control signal to maintain a molar ratio of oxygen to methane in the reactor inlet, the ratio being in the range 0.4-0.7. Additional features may also include: flowing ambient air into the reactor (e.g., to provide additional oxygen); flowing steam into the reactor to maintain a molar ratio of water to methane in an atmosphere of the reactor, the ratio being in the range 2.0-5.0; or modulating the second control signal to prevent hydrogen starvation in the fuel cell. Some embodiments may include measuring a voltage of the fuel cell stack; and modulating the second control signal in response to the voltage measurement. Under the foregoing methods, the carbon monoxide in the fuel gas flowed into the anode chamber of the fuel cell can have a concentration of at least 1,000 parts per million (e.g., 3,000-10,000 parts per million).  
           [0027]    In another aspect, the invention provides a method of operating a fuel cell system, including the following steps: operating a first blower according to a first control signal to vary a flow of ambient air through a cathode chamber of a fuel cell; reacting a portion of the air in the fuel cell to produce electricity; exhausting a remaining portion of the air from the fuel cell, wherein the remaining portion of air contains water vapor; mixing a portion of the exhausted air with methane to form a feed mixture; modulating the first control signal to maintain a molar ratio of oxygen to methane in the feed mixture, the ratio being in the range 0.4-0.7; operating a second blower according to a second control signal to flow the hydrocarbon gas into a reactor where the feed mixture is contacted with a catalyst suitable for converting a portion of the hydrocarbon gas into a fuel gas containing hydrogen and carbon monoxide; flowing the fuel gas into an anode chamber of the fuel cell; and modulating the second control signal to prevent hydrogen starvation in the fuel cell. Embodiments of this method may further include any of the additional steps and feature described above, either alone or in combination.  
           [0028]    Advantages and other features of the invention will become apparent from the following description, drawing and claims. 
       
    
    
     DESCRIPTION OF THE DRAWINGS  
       [0029]    [0029]FIG. 1 shows a flow diagram of an integrated high temperature PEM fuel cell system.  
         [0030]    [0030]FIG. 2 shows a flow diagram of an integrated high temperature PEM fuel cell system.  
         [0031]    [0031]FIG. 3 shows a schematic of a control system for an integrated high temperature PEM fuel cell system.  
         [0032]    [0032]FIG. 4 shows a prior art integrated fuel cell system.  
         [0033]    [0033]FIG. 5 shows a prior art integrated fuel cell system.  
         [0034]    [0034]FIG. 6 shows a schematic diagram of an integrated high temperature PEM fuel cell system.  
         [0035]    [0035]FIG. 7 shows a schematic diagram of an integrated high temperature PEM fuel cell system.  
         [0036]    [0036]FIG. 8 shows a schematic diagram of a fuel processor.  
         [0037]    [0037]FIG. 9 shows a schematic diagram of a fuel processor.  
         [0038]    [0038]FIG. 10 shows a perspective drawing of various elements within a particular fuel processor.  
         [0039]    [0039]FIG. 11 shows a schematic diagram of an integrated high temperature PEM fuel cell system.  
         [0040]    [0040]FIG. 12 shows a schematic diagram of an integrated high temperature PEM fuel cell system.  
         [0041]    [0041]FIG. 13 shows a chart of possible fuel processor reactor configurations. 
     
    
     DETAILED DESCRIPTION  
       [0042]    Referring to FIG. 1, a flow diagram is shown of an integrated high temperature PEM fuel cell system, including the following steps: ( 100 ) air is sent to a fuel cell stack; ( 102 ) the air is reacted in the stack at a temperature in the range 120-200° C.; ( 104 ) cathode exhaust from the fuel cell is sent to a fuel processor; ( 106 ) the cathode exhaust is reacted with hydrocarbon in the fuel processor to produce reformate; ( 108 ) the reformate is sent to a fuel cell stack; ( 110 ) the reformate is reacted in the stack at a temperature in the range 120-200° C.; ( 112 ) the anode exhaust from the fuel cell is sent to an oxidizer; and ( 114 ) the exhaust from the oxidizer is vented to ambient.  
         [0043]    Referring to FIG. 2, another flow diagram is shown of an integrated high temperature PEM fuel cell system; including the following steps: ( 200 ) cathode exhaust from a fuel cell is mixed with a hydrocarbon and reacted to produce a fuel stream containing hydrogen and carbon monoxide; ( 202 ) the fuel stream is reacted in a fuel cell at a temperature in the range 120-200° C.; ( 204 ) the anode exhaust from the fuel cell is sent to an oxidizer to reduce carbon monoxide levels; and ( 206 ) the exhaust from the oxidizer is vented to ambient (the atmosphere around the system).  
         [0044]    Referring to FIG. 3, a schematic is shown of a control system for an integrated high temperature PEM fuel cell system Such a control system can include the following components, as examples: ( 300 ) an electronic controller, e.g., a programmable microprocessor; ( 302 ) a graphical user interface; ( 304 ) software for instructing the controller; ( 306 ) an air blower for providing the system with air, e.g., the fuel cell cathode and/or the fuel processor; ( 308 ) a fuel blower for driving hydrocarbon into the fuel processor; ( 310 ) a stack voltage scanner for measuring the stack voltage and/or the individual voltages of fuel cells within the stack; ( 312 ) a coolant pump for circulating a coolant through the fuel cell stack to maintain a desired stack operating temperature; ( 314 ) a coolant radiator and fan for expelling heat from the coolant to ambient; ( 316 ) a fuel processor inlet air by-pass valve for controlling the amount of air fed to the fuel processor; and ( 318 ) an oxidizer inlet air control valve.  
         [0045]    Such a control system can operate to control the following variables, as examples: ( 320 ) the fuel processor inlet oxygen to fuel ratio; ( 322 ) the fuel processor inlet water to fuel ratio; ( 324 ) a fuel processor reactor temperature; ( 326 ) the voltage of the fuel cell stack or of individual fuel cells within the stack; ( 328 ) the oxidizer temperature; ( 330 ) electrical demand on the fuel cell system; ( 332 ) the cathode air stoich; ( 334 ) the anode fuel stoich; and ( 336 ) the system coolant temperature.  
         [0046]    Referring to FIG. 4, a prior art integrated fuel cell system  400  is shown. Natural gas is injected into the system through conduit  402  The natural gas flows through desulfurization vessel  404 , which contains a sulfur-adsorbent material such as activated carbon. The de-sufurized natural gas is then flowed to a conversion reactor  410  via conduit  405 . Before being reacted in the conversion reactor  410 , the de-sulfurized natural gas is mixed with air  406  and steam  408 . It will be appreciated that the conversion reactor  410  is an autothermal reactor (see equations 3 and 4). The converted natural gas, referred to as reformate, then flows through a series of high temperature shift reactors  412  and  414  (see equation 5), through a low temperature shift reactor  416 , and then through a PROX reactor  418  (see equation 6). It will be appreciated that the primary function of this series of reactors is to maximize hydrogen production while minimizing carbon monoxide levels in the reformate. The reformate is then flowed via conduit  420  to the anode chambers (not shown) of a fuel cell stack  422 .  
         [0047]    Air enters the system via conduit  424  and through conduit  406  as previously mentioned. In the present example, the fuel cell stack  422  uses sulfonated fluourocarbon polymer PEMs that need to be kept moist during operation to avoid damage. While the reformate  420  tends to be saturated with water, the ambient air  424  tends to be subsaturated. To prevent the ambient air  424  from drying out the fuel cells in stack  422 , the air  424  is humidified by passing it through an enthalpy wheel  426 , which also serves to preheat the air  424 . The theory and operation of enthalpy wheels are described in U.S. Pat. No. 6,013,385, which is hereby incorporated by reference. The air  424  passes through the enthalpy wheel  426  through the cathode chambers (not shown) of the fuel cell stack  422 . The air  424  picks up heat and moisture in the stack  422 , and is exhausted via conduit  428  back through the enthalpy wheel  426 . The enthalpy wheel  426  rotates with respect to the injection points of these flows such that moisture and heat from the cathode exhaust  428  is continually passed to the cathode inlet air  424  prior to that stream entering the fuel cell.  
         [0048]    The anode exhaust from the fuel cell is flowed via conduit  430  to an oxidizer  432 , sometimes referred to as an “anode tailgas oxidizer”. The cathode exhaust leaves the enthalpy wheel  426  via conduit  434  and is also fed to the oxidizer  432  to provide oxygen to promote the oxidation of residual hydrogen and hydrocarbons in the anode exhaust  430 . As examples, the oxidizer  432  can be a burner or a catalytic burner (similar to automotive catalytic converters). The exhaust of the oxidizer is vented to ambient via conduit  436 . The heat generated in the oxidizer  432  is used to convert a water stream  438  into steam  408  that is used in the system.  
         [0049]    Referring to FIG. 5, another prior art integrated fuel cell system  500  is shown. Natural gas enters the system via conduit  502  and is injected into a desulfurization vessel  506  via conduit  520 . The de-sulfurized natural gas is then injected into a mixing vessel  506  where is it mixed with air  522  and steam (not shown), and then injected via conduit  524  into an autothermal reactor  508 . The reformate is then flowed through a shift reactor  510  and then through a PROX reactor  512 , before it is injected via conduit  526  into the anode chambers (not shown) of a fuel cell stack  514 . The anode exhaust is flowed via conduit  530  to an oxidizer  516  that is vented to ambient via conduit  534 . Air enters the system as previously mentioned via conduit  522 , and also via conduit  536  that injects ambient air into a humidifier  518  (e.g., steam humidifier or enthalpy wheel). The humidified air is then injected via conduit  532  into the cathode chambers (not shown) of fuel cell stack  514 . The cathode exhaust is flowed via conduit  528  to oxidizer  516 .  
         [0050]    In some embodiments of the present invention, the cathode exhaust is the sole source of steam utilized in the ATR. This provides an advantageous simplification of systems such as that shown in FIGS. 4 and 5, since the simplified systems under the present invention do not require subsystems to humidify the hydrocarbon fuel fed to the fuel processor. Likewise, embodiments under the present invention utilizing the PBI PEM material do not require humidification of the PEM, and thus it is not necessary to humidify the cathode inlet stream, such that subsystems such as the enthalpy wheel  426  (FIG. 4) and the steam humidifier  518  (FIG. 5) can be eliminated.  
         [0051]    One aspect of the present invention is the application of the concept that when the cathode exhaust is maintained at a stoich greater than 1 (e.g., 2 stoich), there is enough water vapor present to provide a desired ratio of the molar flow of water in the cathode exhaust to the molar flow of methane into the fuel processor to meet a given electric load. As an example, it may be preferable to keep this ratio over 2.0, such as in the range 2.0-5.0. Likewise, it will be appreciated that the cathode air stoich can be increased for a given electrical load to provide more oxygen to the fuel processor, since for a higher stoich, a lower percentage of the oxygen in the air will be reacted in the fuel cell.  
         [0052]    For a given electrical demand, the fuel cell stack reacts enough air and fuel to meet the demand. Also corresponding to the given electrical demand, the fuel processor must produce enough reformate to support the amount of fuel required in the fuel cell stack to meet the electrical demand. It will be appreciated that in various embodiments of the present invention, the amount of water in the cathode exhaust at the given electrical demand is sufficient when added to the fuel processor to achieve an appropriate steam to carbon ratio (e.g., more than 2, or more than 2.5) with respect to the amount of hydrocarbon required by the fuel processor to meet the demand for reformate. In some cases, this may be true over the entire power output range of the system, and in other cases, this may not be true at certain operating points. In such cases, the fuel, air and steam may be supplemented or adjusted as needed.  
         [0053]    While the forgoing discussion relates to embodiments designed to utilize natural gas (e.g., methane), it will be appreciated that embodiments under the present invention may also include system designed to utilize other hydrocarbon materials, such as propane, methanol, gasoline, etc.  
         [0054]    Referring to FIG. 6, a schematic diagram is shown of an integrated high temperature PEM fuel cell system  600  under one possible embodiment of the present invention. Natural gas enters the system via conduit  602  and is injected into a de-sulfurization vessel  604 . The de-sulfurized natural gas is then injected via conduit  605  into an autothermal reactor  608 . The reformate is then flowed through a shift reactor  610 . The reformate is then flowed via conduit  626  through the anode chambers (not shown) of fuel cells in fuel cell stack  614 . The anode exhaust is vented via conduit  615  to oxidizer  616 . The oxidizer exhaust is vented to ambient via conduit  636 . Air enters the system via conduit  630 , and is supplied via conduit  632  to the oxidizer  616 , and via  634  to the fuel cell stack  614 . Unlike the prior art, the cathode exhaust is flowed via conduit  627  into the fuel mixture reacted in autothermal reactor  608 . Under the present invention, cathode exhaust may be maintained at a temperature over 100° C. to prevent any condensation of water in the cathode exhaust. Likewise, the cathode exhaust plumbing may be insulated to prevent heat loss that might result in water loss through condensation.  
         [0055]    Referring to FIG. 7 a schematic diagram is shown of an integrated high temperature PEM fuel cell system  700  under the present invention. Natural gas enters the system via conduit  702  and is injected into a fuel processor  704 . The reformate is flowed via conduit  706  to the anode chambers (not shown) of fuel cells in fuel cell stack  708 . The anode exhaust is flowed via conduit  710  to oxidizer  712 , which is vented to ambient via conduit  714 . Air enters the system via conduit  716 , and is flowed into the cathode chambers (not shown) of fuel cells in fuel cell stack  708 . The cathode exhaust is flowed via conduit  718  to oxidizer  712 , and via conduit  722  into the feed mixture fuel processor  704 .  
         [0056]    Referring to FIG. 8, a schematic diagram is shown of a fuel processor  800 . This diagram illustrates a mixing chamber  802  that receives a flow of cathode exhaust  806 , and a flow of hydrocarbon gas  808  (e.g., methane). The cathode exhaust  806  and hydrocarbon gas  808  are thus mixed before flowing into reactor  804 . Alternatively, referring to FIG. 9, a schematic diagram is shown of a fuel processor  1000  utilizing a reactor  1002  that receives a fuel air mixture via conduit  1008 . Air is injected via conduit  1006  directly into fuel conduit  1004 , which then flows to the reactor under the designation of conduit  1002 .  
         [0057]    Referring to FIG. 10, a perspective drawing is shown of various elements within a particular fuel processor. Hydrocarbon gas enters the system via conduit  902  and is flowed through an autothermal catalyst monolith  904 . Catalyst monolith  904  can be, as an example, a ceramic honeycomb monolith that has been washed coated with platinum. The reformate  906  is exhausted from monolith  904  and passed across a heat transfer surface  908  which reduces the temperature of the reformate. The reduced temperature reformate  910  is flowed through a shift reaction catalyst monolith  912 . Similar to monolith  904 , catalyst monolith  912  can be, as an example, a ceramic honeycomb monolith that has been washed coated with platinum. The reformate then exits the fuel processor via conduit  914 .  
         [0058]    Referring to FIG. 11, a schematic diagram is shown of an integrated high temperature PEM fuel cell system  1100 . In this case, a fuel processor  1104  is shown directly abutting a fuel cell stack assembly  1102 . Hydrocarbon gas enters the system through conduit  1106  and reformate exits the fuel processor  1104  via conduit  1108 . The reformate is flowed through fuel cell stack  1102  and exits the fuel cell stack  1102  via conduit  1112 . Air enters the fuel cell stack  1102  via conduit  1110  and is exhausted directly into fuel processor  1104  due to its abutting connection to the stack  1102 . In this manner, heat loss from the cathode exhaust is minimized along with any associated water loss from condensation.  
         [0059]    Referring to FIG. 12, a schematic diagram is shown of an integrated high temperature PEM fuel cell system. In this case, a fuel processor  1204  is shown connected to a fuel cell stack assembly  1202  via conduit  1203 . Hydrocarbon gas enters the system through conduit  1206  and reformate exits the fuel processor  1204  via conduit  1208 . The reformate is flowed through fuel cell stack  1202  and exits the fuel cell stack  1202  via conduit  1212 . Air enters the fuel cell stack  1202  via conduit  1210  and is exhausted directly into fuel processor  1204  due to its abutting connection to the stack  1202 . Cathode exhaust is flowed to fuel processor  1204  via conduit  1203 . Conduit  1203  is insulated to minimize heat loss from the cathode exhaust along with any associated water loss from condensation.  
         [0060]    Referring to FIG. 13, a chart is shown of possible fuel processor reactor configurations under the present invention: (A) ATR with single stage HTS; (B) ATR with single stage HTS and single stage LTS; (C) ATR with double stage HTS; (D) ATR with double stage HTS and single stage LTS; (E) CPO with single stage HTS; and (F) steam reformer with single stage HTS. As will be appreciated by those of ordinary skill in the art, other reactor configurations are also possible.  
         [0061]    In some embodiments, the autothermal and shift reactors may be sized and operated such that the reformate that is sent to the fuel cell contains 100-100,000 ppm carbon monoxide. Operation in the 100-200° C. temperature range allows the stack to tolerate carbon monoxide levels in this range without poisoning the fuel cell catalyst. Reducing the demands of the fuel processor for minimizing carbon monoxide production (e.g., needing to produce less CO than this range) enables a less expensive and simplified reformer design (e.g., less ATR and shift reactor catalysts, and no PROX require). In such systems, the spent fuel from the fuel cell stack can be sent to an oxidizer to reduce or eliminate residual hydrogen and hydrocarbons (e.g., reducing carbon monoxide to below 100 parts per million or some other desired range).  
         [0062]    Under embodiments of the present invention, the catalyst in the fuel cell can be platinum-based, as is known in the art. Since the fuel cell stack is tolerant to carbon monoxide, an advantage of the invention is that it is not necessary to include a ruthenium-based catalyst or platinum ruthenium alloy to improve carbon monoxide tolerance, as is common in the prior art, and thus the cost associated with the fuel cell stack is reduced. Thus, some embodiments utilize a catalyst consisting essentially of platinum (platinum is the only catalytically active material in the catalyst layer of the fuel cell).  
         [0063]    Embodiments of the invention may also include a controller adapted to achieve these objectives (e.g., microprocessor controlled blowers and valves that are responsive to the electrical load on the fuel cell stack, or on the performance condition of the fuel cell stack). Such a controller may include software or hardware programmed to manipulate system operating variables by controlling the operation of components within the system (see FIG. 3).  
         [0064]    Also, the air supplied to the fuel cell stack may be preheated before it is introduced. As examples, the air may be preheated by passing it across a hot surface of the fuel processor such as the ATR vessel, or through a gas/gas heat exchanger associated with the reformate, or through a gas/liquid heat exchanger associated with a coolant system of the fuel cell stack or the fuel processor, or both.  
         [0065]    While the invention has been disclosed with respect to a limited number of embodiments, those skilled in the art, having the benefit of this disclosure, will appreciate numerous modifications and variations therefrom. It is intended that the invention covers all such modifications and variations as fall within the true spirit and scope of the invention.