Abstract:
A hydrocarbon fueled hydrogen generator and hydrogen fueled electric power generating system and apparatus comprising hydrocarbon fuel and oxidizer delivery and mixing apparatus, ignition and combustion apparatus igniting the mixture of fuel and oxidizer, apparatus receiving and conducting the gases of combustion through a sulfur absorbing unit and removing sulfur from the gases, a steam reformer unit reforming carbon monoxide gas into hydrogen gas and carbon dioxide gas, a carbon monoxide scavenger unit reforming residual carbon monoxide gas to hydrogen gas and carbon dioxide gas; apparatus receiving the hydrogen gas and carbon dioxide gas and operating to liquefy and separate the carbon dioxide gas from the hydrogen gas; and, structure to hold and deliver the liquid carbon dioxide to useful end; and structure to hold and deliver hydrogen gas to the anode of a hydrogen fueled electric power generating fuel cell.

Description:
BRIEF SUMMARY OF THE INVENTION  
         [0001]    This invention relates to a hydrocarbon fueled, hydrogen fuel generator system and apparatus for fuel cells. The primary application for this invention is generating hydrogen fuel for use in fuel cells that convert chemical energy into electricity. The hydrogen fuel generator is fueled by hydrocarbons such as propane, butane, methanol, ethanol, pentane, kerosene, and gasoline. The invention provides a polymer-electrolyte membrane fuel cell anode hydrogen fuel stream that is free of carbon monoxide, carbon dioxide, and sulfur. The invention provides an alkaline-electrolyte fuel cell anode hydrogen fuel that is free of carbon monoxide, carbon dioxide, sulfur, and/or nitrogen. In addition, alkaline-electrolyte oxidizer (air) for the fuel cell cathode is free of carbon dioxide.  
         PRIOR ART  
         [0002]    A hydrogen generating apparatus and a fuel cell is described in U.S. Pat. No. 5,429,886, issued to Ralph C. Struthers on Jul. 4, 1995, and entitled, “HYDROCARBON (HYDROGEN)/AIR AEROGEL CATALYZED CARBON ELECTRODE FUEL CELL SYSTEM”. This invention relates to a hydrogen fuel generator that produces carbon monoxide and nitrogen concentrations in the hydrogen fuel. This type of hydrogen generating system is undesirable for polymer-electrolyte membrane fuel cells because of carbon monoxide poisoning.  
           [0003]    A hydrogen generating apparatus is described in U.S. Pat. No. 5,942,346, issued to Shabbir Ahmed et al., on Aug. 24, 1999, and entitled, “METHANOL PARTIAL OXIDATION REFORMER”. This invention relates to a hydrogen fuel generator that produces carbon monoxide, carbon dioxide, and nitrogen concentrations in the hydrogen fuel. This type of hydrogen generating system is undesirable for polymer-electrolyte membrane fuel cells because of carbon monoxide poisoning and alkaline-electrolyte fuel cells because of carbon dioxide poisoning.  
           [0004]    A hydrogen generating apparatus described in U.S. Pat. No. 6,083,425 issued to Clawson et al., on Jul. 4, 2000, and entitled, “METHOD FOR CONVERTING HYDROCARBON FUEL INTO HYDROGEN GAS AND CARBON DIOXIDE”. This invention relates to a hydrogen fuel generator that produces carbon monoxide, carbon dioxide, and nitrogen concentrations in the hydrogen fuel. This type of hydrogen generating system is undesirable for polymer-electrolyte membrane fuel cells because of carbon monoxide poisoning and alkaline-electrolyte fuel cells because of carbon dioxide poisoning.  
         SUMMARY OF THE INVENTION  
         [0005]    The present invention is directed the provision of fuel cell powered electric vehicles that are efficient, reduce noise and emissions and unburdened of the problems associated with the use of short range batteries that need to be charged; and, current gasoline-electric hybrid vehicles that need a gasoline combustion engine. Such vehicles will gain about three times the fuel mileage of comparable vehicles with internal combustion engines. The hydrogen fuel generator of this invention is fueled by hydrocarbons such as propane, butane, methanol, ethanol, pentane, kerosene, and gasoline. Accordingly, the existing petroleum fuel infrastructure for producing and distributing fuels is practical and economical for fueling such vehicles.  
           [0006]    The advantages of the invention over the prior art are noted below:  
           [0007]    1. The present invention provides hydrogen fuel for polymer-electrolyte membrane and alkaline-electrolyte fuel cells that constitute mature forms of the fuel cell technology.  
           [0008]    2. The present invention provides an oxidizer (air) stream free of carbon dioxide for alkaline-electrolyte fuel cell cathodes.  
           [0009]    3. Fluid-metering pump means move fluids of different physical characteristics in different quantities.  
           [0010]    4. An ignition system means and electronic processor control means detonates the hydrocarbon fuel yielding a hot pressurized output gas in a pressure chamber.  
           [0011]    5. Hydrocarbon fuel is partially oxidized in a partial oxidizer means yielding a hot pressurized fuel stream of hydrogen and carbon monoxide.  
           [0012]    6. Hydrocarbon fuel is completely oxidized in an oxidizer means yielding a hot pressurized fuel stream of steam and carbon dioxide.  
           [0013]    7. A steam generating means that generates hot pressurized steam;  
           [0014]    8. Heat exchanger means cools the hot pressurized fuel gas stream to a preferred reaction temperature as required for sulfur absorbing, steam reforming and carbon monoxide scavenging.  
           [0015]    9. A sulfur absorbing means removes all elemental sulfur compounds in the pressurized fuel stream of hydrogen and carbon monoxide.  
           [0016]    10. Steam reformer means reforms carbon monoxide in the fuel stream yielding a pressurized gas stream of hydrogen and carbon dioxide.  
           [0017]    11. A carbon monoxide scavenger means converts remaining carbon monoxide to a pressurized gas stream of carbon dioxide.  
           [0018]    12. Heat exchanger means cools carbon dioxide gas within carbon dioxide liquid limits.  
           [0019]    13. A hydrogen and carbon dioxide separation means separates pressurized hydrogen fuel from pressurized liquid-carbon dioxide.  
           [0020]    14. Pressurized steam pumping means pumps atmospheric air into a high-pressure air tank.  
           [0021]    15. Carbon dioxide separating means removing carbon dioxide from the air by pressurizing and cooling within carbon dioxide liquid limits.  
           [0022]    16. Carbon dioxide and moisture separating means removing carbon dioxide from the air by adsorbent column beds.  
           [0023]    It is an object of this invention to provide a sulfur removal means using various porous metal oxide aerogel microspheres of cerium, zinc, strontium, magnesium, copper, lanthanum, barium, iron, yttrium, chromium, cobalt, vanadium, zirconium, and/or suitable precious metals.  
           [0024]    It is another object of this invention to provide an improved steam reformer means using a catalyst made from various porous metal aerogel microspheres of nickel, copper, zinc, iron, cobalt, zirconium, chromium, rare earth metals, and/or suitable precious metals.  
           [0025]    Yet, another object of this invention is to provide a carbon monoxide scavenger means utilizing various porous metal oxide aerogel microspheres of nickel, manganese, tin, copper, silver, iron, zinc and/or chromium.  
           [0026]    Still, another object of this invention is to provide a novel, improved heat exchanger means or system that both heats and cools system components, as required.  
           [0027]    Another object of this invention is to provide a propellant of pressurized carbon dioxide liquid for energizing fluid-metering pump means.  
           [0028]    Another object of this invention is to provide propellant of pressurized steam for energizing fluid-metering pump means.  
           [0029]    It is another object of this invention is to provide a supply of carbon dioxide liquid coolant and a heat exchanger means suitable for secondary use, such as cooling the interior cabin of a related electric vehicle.  
           [0030]    Another object of this invention is to provide a hot steam and a heat exchanger means suitable for secondary use, such as heating of the interior cabin of the electric vehicle.  
           [0031]    Another object of this invention is to provide electric powered vehicle or the like with our new hydrogen generator system and apparatus as the supply power means that converts hydrocarbon fuel energy to electric energy; an operating strategy for a fuel cell electric powered vehicle that manages the flow of energy to maximize fuel economy; an inverter that converts the direct current output from the fuel cells, and energy stored in a battery pack to a three-phase alternating current. A motor/generator receives the alternating current and produces a rotating driving force that is transmitted through a continuously variable or automatic transmission to vehicular wheels. A controller is connected to the motor/generator, accelerator pedal and brake pedal. When the vehicle is coasting or the brakes are applied, the wheels drive the motor/generator, converting the vehicle&#39;s kinetic energy to electricity that charges the battery pack.  
           [0032]    Finally, it is object of this invention is to recycle atmospheric carbon dioxide to methanol fuel. The earth&#39;s ozone layer is being depleted and it could be reversed if recycled carbon dioxide methanol fuel was used to operate automobiles and/or the like. The reduction of carbon dioxide to methanol is represented by the chemical equation of CO 2 +6H + +6e−=CH 3 OH+H 2 O.  
           [0033]    The above objects and features of this invention will be understood from the following detailed description of the invention, wherein reference is made to the accompanying drawings.  
       
    
    
     DESCRIPTION OF THE DRAWINGS  
       [0034]    [0034]FIG. 1 is a schematic illustration of our new hydrogen fuel generator system and apparatus in which a polymer-electrolyte membrane fuel cell is utilized;  
         [0035]    [0035]FIG. 2 is a schematic illustration of our new hydrogen fuel generator system and apparatus in which a circulating alkaline-electrolyte fuel cell is utilized;  
         [0036]    [0036]FIG. 3 is a schematic illustration of our new hydrogen fuel generator system and apparatus in which a matrix alkaline-electrolyte fuel cell is utilized;  
         [0037]    [0037]FIG. 4 is a sectional view of a form of fluid-metering pump suitable for use in carrying out the invention;  
         [0038]    [0038]FIG. 5 is a cross sectional view of chambers and electrodes shown in FIG. 1, FIG. 2 and FIG. 3;  
         [0039]    [0039]FIG. 6 is a sectional view of a form of a direct acting reciprocating, steam-driven high-pressure air pump suitable for use in carrying out the invention;  
         [0040]    [0040]FIG. 7 is a theoretical computation of chemical formula, polymer-electrolyte membrane and circulating alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when propane fueled and air-oxidized;  
         [0041]    [0041]FIG. 8 is a theoretical computation of chemical formula, polymer-electrolyte membrane and matrix alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when propane fueled and hydrogen peroxide-oxidized;  
         [0042]    [0042]FIG. 9 is a theoretical computation of chemical formula, polymer-electrolyte membrane and circulating alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when methanol fueled and air-oxidized;  
         [0043]    [0043]FIG. 10 is a theoretical computation of chemical formula, polymer-electrolyte membrane matrix alkaline-electrolyte fuel cell efficiency of the hydrogen gas generator when methanol fueled and hydrogen peroxide-oxidized;  
         [0044]    [0044]FIG. 11 is a theoretical computation of chemical formula, polymer-electrolyte membrane and circulating alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when gasoline fueled and air-oxidized;  
         [0045]    [0045]FIG. 12 is a theoretical computation of chemical formula, polymer-electrolyte membrane matrix-alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when gasoline fueled and hydrogen peroxide-oxidized;  
         [0046]    [0046]FIG. 13 is a theoretical computation of chemical formula, polymer-electrolyte membrane and circulating alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when kerosene fueled and air-oxidized;  
         [0047]    [0047]FIG. 14 is a theoretical computation of chemical formula, polymer-electrolyte membrane and matrix alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when kerosene fueled and hydrogen peroxide-oxidized;  
         [0048]    [0048]FIG. 15 is a theoretical computation of chemical formula, polymer-electrolyte membrane and circulating alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when ethanol fueled and air-oxidized; and  
         [0049]    [0049]FIG. 16 is a theoretical computation of chemical formula, polymer-electrolyte membrane and matrix alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when ethanol fueled and hydrogen peroxide-oxidized.  
     
    
     DETAILED DESCRIPTION OF THE INVENTION  
       [0050]    The system and apparatus of the present invention operates to provide a hydrogen fuel stream that is free of carbon monoxide, carbon dioxide, sulfur, and nitrogen. The invention is particularly suitable to providing a hydrogen fuel stream for use in fuel cell systems as might be used in electric powered vehicles and other devices and means commonly powered with internal combustion engines.  
         [0051]    Referring to FIG. 1, FIG. 2 and FIG. 3 of the drawings the hydrogen fuel generator system and apparatus EVHG and the fuel cell FC can, for example be advantageously mounted aboard an electric powered vehicle (not shown or described).  
         [0052]    The hydrogen fuel generator system and apparatus EVHG generates hydrogen fuel for use in fuel cells that convert chemical energy into electricity. The hydrogen fuel generator can be fueled by hydrocarbons of propane, butane, methanol, ethanol, pentane, kerosene, or gasoline. A propellant P powered fuel-metering pump FMP receives hydrocarbon fuel  10  from a line  11  extending from a fuel tank FT and delivers the fuel through a line  12  into a mixing and vaporizing chamber MC at the upstream end of a tank-like structure. In addition, a propellant P powered oxidizer-metering pump OMP delivers air or hydrogen peroxide oxidizer  13  through a line  14  into the mixing and vaporizing chamber MC.  
         [0053]    The oxidizer and fuel within the mixing and vaporizing chamber MC are mixed, vaporized and flow from chamber MC into an throughout an ignition chamber IC within the tank-like structure. An ignition means IS within chamber IC detonates the oxidizer and fuel vapor  15 , thereby oxidizing said fuel mixture.  
         [0054]    The oxidizer chamber OC of the tank-like structure includes an elongate cylindrical exterior part, an inner tubular part, tubular CE and an elongate rod electrode RE positioned centrally within the part CE. The electrode is suitable electrically energized to generate a high voltage arcs within the chamber IC. The product of oxidation in chamber OC advances or flows into an intake or receiving zone of a pressure chamber Pc down stream thereof.  
         [0055]    A propellant P powered water-metering pump WMP moves water  16  from a tank WT through lines  17  and  18  into a steam chamber SC, generating steam  19 . The steam chamber SC is shown as an annular chamber about the part CE and receives water from line  18 . The steam generated in chamber SC advances or flows downstream into the pressure chamber PC.  
         [0056]    In a startup mode, the hot pressurized gas HPGL in the pressure chamber PC contains carbon dioxide, steam, and sulfur.  
         [0057]    In the operational mode, the hot pressurized gas HPG 1  in the pressure chamber PC contains hydrogen, carbon monoxide, and steam (it might also contain sulfur and/or nitrogen if that gas is present).  
         [0058]    The hot pressurized gas stream HPG 1  flows about and is tempered or cooled by a first heat exchanger HB 1  to the preferred zone reaction temperature as required for sulfur absorbing, steam reforming, and carbon monoxide scavenging.  
         [0059]    A pack or bed of sulfur absorbent material SA is suitably positioned at zone  20  within the tank-like structure and works to remove all elemental sulfur compounds from the tempered pressurized gas stream HPG 1 . The zone  20  is immediately downstream of the receiving zone in the chamber PC and receives the gas BPG 1  first generated in the chamber PC.  
         [0060]    The sulfur free pressurized gases HPG 1  next advances and flows downstream from pack or bed  20  into and throughout a catalyst pack or bed  21  of a steam reformer means SR in the a zone  21  in chamber PC of the tank-like structure that is immediately downstream of the zone  20 . The steam reformer SR reforms the carbon monoxide to hydrogen fuel and carbon dioxide, producing a pressurized gas output stream HPG 2 .  
         [0061]    A carbon monoxide scavenger means CMS, including a pack or bed  22  is positioned within the tank-like structure at immediate downstream of the steam reformer means SR and works to convert residual carbon monoxide to carbon dioxide in the pressurized output gas HPG 2  that advance into a gas-collecting zone CC in the tank-like structure immediately downstream from of  22 .  
         [0062]    If air is the oxidizer  13  in the operational mode, the pressurized gas output stream HPG 2  will contain nitrogen, hydrogen, and carbon dioxide. If hydrogen peroxide is the oxidizer  13  in the operational mode, the pressurized gas output stream HPG 2  will be nitrogen free and will only contain hydrogen and carbon dioxide.  
         [0063]    In a startup mode, the controlled temperature of the pressurized gas output stream HPG 2  is less than 650° F. It flows through a solenoid-actuated value S 1  from a line  23  to the atmosphere  24 -control means for the valve S 1  induces a thermocouple T 1  between lines  23 - 24  the thermocouple must test gas temperature at less than about 650° F. to effect opening of that value.  
         [0064]    In a pressure mode, between about 734 psi to about 1052 psi, and at a temperature from about 650° F. to a preferred reaction temperature as required for sulfur absorbing, steam reforming, and carbon monoxide scavenging the pressurized gas output stream HPG 2  flows through heat exchangers HE 2  and HE 3 . The pressurized gas output stream HPG 2  flows through line  23 . A solenoid actuated value S 2  connects with an outlet of line  23 . Lines  25 ,  26 , and  27  extend from value S 2  to and through the heat exchangers HE 2  and HE 3 . A pressure sensor P 2  at value S 2  and a pressure sensor P 9  at chamber PC must test between about 734 psi to about 1052 psi. Thermocouple T 9  at the pressure chamber PC must test between about 650° F. to the preferred hydrocarbon fuel combustion exothermic reaction temperature. Thermocouple T 2  at the collecting zone CC must test between about 650° F. to the preferred zone reaction temperature as required for sulfur absorbing, steam reforming, and carbon monoxide scavenging.  
         [0065]    In a cooling mode, when pressures are from between about 734 psi to about 1052 psi and when temperatures are from about 59° F. to about 87° F., at line  28 , value S 2  operates to allow the pressurized gas output stream HPG 2  to flow through the heat exchangers HE 2  and HE 3  to an elongate vertical hydrogen and carbon dioxide separator tank  32 . The cooled pressurized gas output stream HPG 2  in the tank  32  is separates to hydrogen fuel HT and carbon dioxide liquid CT. Thermocouples T 3  between lines  28 - 29  and T 10  related to the lower end of tank  32  must both test between about 59° F. to about 87° F. and a pair of vertically spaced pressure sensors P 3  and P 10  related to the lower liquid carbon dioxide collecting portion of the tank  32  must both test between about 734 psi to about 1052 psi.  
         [0066]    Referring to FIG. 3 and FIG. 6, the steam outflows from exchanger HE 1  is used as a propellant P. The steam propellant P flows by way of line  51  to power a high-pressure air pump HPP and returns used steam flows through lines  51 ′ and  49  to the water condenser WC.  
         [0067]    A propellant P powered coolant-metering pump CMP 2  moves water coolant  16  through lines  44  and  45  throughout the second heat exchanger HE 2  cooling the hydrogen fuel gas and carbon dioxide gas HPG 2  in line  26  within the exchanger HE 2 , and generates steam  46  in line  47 . The pressurized carbon dioxide  30  stored in liquid state is collected in tank  32  that flows though lines  59  and  60  to and through solenoid actuated value S 6  and line  61 . The liquid carbon dioxide expands, cooling and absorbing heat from the surface of line  27  and is vaporized by sublimation through the third heat exchanger HE 3 ; and, exits the system through line  62 . Heat exchanger HE 3  cooled carbon dioxide gas in line  27  yields carbon dioxide liquid  30  in line  28  at the downstream end of the exchanger. The liquid-phase range limits of temperature and pressure for carbon dioxide are about 59° F. to about 87° F. and about 734 psi to about 1052 psi. The carbon dioxide liquid  30  flows by way of line  29  into carbon dioxide liquid pressure tank CT and the hydrogen fuel  31  flows by way of line  29  into hydrogen pressure tank HT. The separated vapor and liquid are stored, under pressure as hydrogen fuel  31  at the top and as carbon dioxide liquid  30  at the bottom of the separator pressure tank  32 .  
         [0068]    A propellant P powered hydrogen-metering pump HMP moves the hydrogen fuel  31  from the pressure tank  32  through lines  33  and  34  into and throughout a column bed F 1  absorbing any residual carbon dioxide, carbon monoxide and/or elemental sulfur compounds from the hydrogen fuel before flowing through line  35  to and throughout a fuel cell FC anode electrodes A. The unused hydrogen  31 , steam, (and nitrogen) flow through line  36  or line  37 .  
         [0069]    Polymer-electrolyte membrane PEM type fuel cells FC, as shown in FIG. 1. A propellant P powered air-metering pump AMP move air  52  from the atmosphere by way of line  53  throughout the fuel cell FC cathode electrodes C. The unused oxidizer, steam, and nitrogen flow through line  40 .  
         [0070]    Circulating alkaline-electrolyte CIR ALK type fuel cell FC as shown in FIG. 2. The propellant P powered pressure-metering pump PMP compresses air  52  from the atmosphere by way of line  67  into a pressurized air supply tank PT. The air supply tank PT pressure range of the air is maintained between about 30 psi to about 100 psi by means of a sensor on P 11 , and temperature range is maintained between about  60 ° F. to about  120 ° F. by means of a thermocouple T 11 .  
         [0071]    In the following column beds  71  and  75  will be initially described in the adsorption mode and column beds  82  and  87  will be initially described in the regeneration mode. During the first phase of the process, airflows through three-way solenoid actuated value S 12  from line  69  to line  70  and column bed  71 . Airflows through three-way solenoid actuated value S 14  from line  72  to line  73 . Air also flows through three-way solenoid actuated value S 16  from line  73  to line  74  and column bed  75 . Air also flows through three-way solenoid actuated value S 18  from line  76  to line  77 . Air flows through propellant P powered air-metering pump AMP that moves or delivers air free of carbon dioxide from line  77  through line  78  to and throughout the fuel cell CIR ALK FC cathode electrodes C.  
         [0072]    Meanwhile, hot regeneration purge gas from line  79  of the fuel cell CIR ALK FC cathode electrodes C output exhaust flows through three-way solenoid actuated value S 17  from line  80  to line  81  and column bed  82 , purge gas flows through three-way solenoid actuated value S 19  from line  83 , the regeneration gas, and desorbed carbon dioxide exits the system through line  84 .  
         [0073]    The remainder of the hot regeneration purge gas from line  79  of the fuel cell CIR ALK FC cathode electrodes C output exhaust flows throughout heat exchanger AE, purge gas flows through three-way solenoid actuated value S 15  from line  85  to line  86  and column bed  87 , purge gas flows through three-way solenoid actuated value S 13  from line  88  with the regeneration purge gas, desorbed carbon dioxide, and moisture exits the system through line  89 . The pressurized carbon dioxide  30  stored in liquid state is collected in tank  32  that flows though line  59  to and through solenoid actuated value S 20  and line  65  expanding, cooling and absorbing heat from the surface of line  85  and is vaporized by sublimation through the heat exchanger AE and exits the system through line  66 . The thermocouple T 10  must test between about 59° F. to about 87° F., and pressure sensor P 10  must test between about 734 psi to about 1052 psi.  
         [0074]    During the second phase of the process, air flows through three-way solenoid actuated value S 13  from line  69  to line  88  and column bed  87 , air flows through three-way solenoid actuated value S 15  from line  86  to line  90 , air flows through three-way solenoid actuated value S 17  from line  90  to line  81  and column bed  82 , air flows through three-way solenoid actuated value S 19  from line  83  to line  77 , air flows through propellant P powered air-metering pump AMP that moves air free of carbon dioxide from line  77  to line  78  throughout the fuel cell CIR ALK FC cathodes C.  
         [0075]    Meanwhile, hot regeneration purge gas from line  79  of the fuel cell CIR ALK FC cathodes C output exhaust flows through three-way solenoid actuated value S 16  from line  80  to line  74  and column bed  75 , purge gas flows through three-way solenoid actuated value S 18  from line  76 , the regeneration gas, and desorbed carbon dioxide exits the system through line  91 .  
         [0076]    The remainder of the hot regeneration purge gas from lines  79  of the fuel cell CIR ALK FC cathodes C output exhaust flows through heat exchanger AE, purge gas flows through three-way solenoid actuated value S 14  from line  85  to line  72  and column bed  71 , purge gas flows through three-way solenoid actuated value S 12  from line  70  with the regeneration purge gas, desorbed carbon dioxide, and moisture exits the system through line  92 . The pressurized carbon dioxide  30  stored in liquid state is collected in tank  32  that flows though line  59  to and through solenoid actuated value S 20  and line  65  expanding, cooling and absorbing heat from the surface of line  85  and is vaporized by sublimation through the heat exchanger AE and exits the system through line  66 . The thermocouple T 10  must test between about 59° F. to about 87° F., and pressure sensor P 10  must test between about 734 psi to about 1052 psi.  
         [0077]    In the case of matrices alkaline-electrolyte MRX ALK type fuel cell FC as shown in FIG. 3. The steam propellant P in line  51  powers a high-pressure pump HPP as shown in FIG. 6 compressing atmospheric air in line  52  through line  93  and pressure solenoid actuated value S 11  , by way of line  94  through line  95  within the heat exchanger AE by way of line  96  to a high-pressure air pressure tank PT. In a pressure mode, when pressures are from between about 734 psi to about 1052 psi and when temperatures are from about 59° F. to about 87° F. the air is directed to flow through the cooled heat exchanger AE to an air and carbon dioxide separator tank PT. The cooled pressurized air output stream in the tank PT is separated to air  99  and carbon dioxide liquid  97 . Thermocouple T 11  related to tank PT must test between about 59° F. to about 87° F. and pressure sensor P 11  must test between about 734 psi to about 1052 psi. The pressurized carbon dioxide  30  stored in liquid state is collected in tank  32  that flows though line  60  to and through solenoid actuated value S 20  and line  65  expanding, cooling and absorbing heat from the surface of line  95  and is vaporized by sublimation through the heat exchanger AE and exits the system through line  66 . In addition, the carbon dioxide liquid coolant  97  collected in tank PT flows though line  98  to and through solenoid actuated value S 21 , line  65  into and cooling the heat exchanger AE, and exits the system through line  66 . Heat exchanger AE cooled carbon dioxide gas in line  95  yields carbon dioxide liquid  97  at the downstream end of the exchanger. The liquid-phase range limits of temperature and pressure for carbon dioxide are about 59° F. to about 87° F. and about 734 psi to about 1052 psi. A propellant P powered air-metering pump AMP moves the air  99  from the pressure tank PT by way of lines  100  and  101  throughout column bed F 2  for absorbing residual carbon dioxide and flows from line  102  throughout the fuel cell MRX AKL FC cathode electrodes C.  
         [0078]    Controlled water usage management supply  16  by electronic processor EP shown in FIG. 1. The polymer-electrolyte membrane PEM fuel cell FC cathode electrode C moves hot output exhaust gas of unused oxidant, nitrogen, and water vapor  16  by way of line  40  throughout a water condenser WC. Nitrogen and unused oxidant flows through line  41  to atmosphere.  
         [0079]    Controlled water usage management supply  16  by electronic processor EP shown in FIG. 2 and FIG. 3. The alkaline-electrolyte ALK fuel cell FC anode electrode A moves hot output exhaust gas of unused hydrogen  31  and water vapor  16  by way of line  37  throughout a water condenser WC. The return-metering pump RMP ejects said unused hydrogen  31  back to the EVHG system from line  38  of the water condenser WC by way of line  39  throughout the pressure chamber PC. The water  16  flows from the water condenser WC by way of lines  42 ,  43 , and solenoid actuated value S 4  to the water storage tank WT. The thermocouple T 4  must test less than about 212° F.  
         [0080]    A propellant P powered coolant-metering pump CMP 1  moves water coolant  16  through lines  44  and  50  for cooling gas fluids HPG 1  surrounded by the first heat exchanger HE 1 , and generates a steam propellant P within line  51 . The steam propellant P flows by way of line  51  to power the high-pressure air pump HPP as shown FIG. 3 and FIG. 6, and returns used steam to the water condenser WC. A propellant P powered coolant-metering pump CMP 2  ejects water coolant  16  through lines  44  and  45  for cooling line  26  gas fluids within the second heat exchanger HE 2 , and generates a steam  46  propellants P in line  47 . The steam  46  propellants P flows by way of line  48  to power the fluid-metering pumps MP, FMP, OMP, WMP, RMP, CMP, PMP, HMP, and AMP. Regulated steam  46  propellants P also flows by way of line  47  and solenoid actuated value S 5  and returns used steam by line  49  to water condenser WC. The pressure sensor P 5  must test between about 25 psi to about 50 psi.  
         [0081]    The carbon dioxide liquid  30  propellant P flows by way of line  59  to power the fluid-metering pumps MP, FMP, OMP, WMP, RMP, CMP, PMP, HMP, and AMP. The thermocouple T 10  must test between about 59° F. to about 87° F, and pressure sensor P 10  must test between about 734 psi to about 1052 psi.  
         [0082]    In addition, the pressurized carbon dioxide  30  stored in liquid state is collected in tank  32  that flows though lines  59  and  60  to and through solenoid actuated value S 6  and line  61  expanding, cooling and absorbing heat from the surface of line  27  and is vaporized by sublimation through the third heat exchanger HE 3  and exits the system through line  62 . The thermocouples T 6  and T 10  must both test between about 59° F. to about 87° F., and pressure sensors P 6  and P 10  must both test between about 734 psi to about 1052 psi. The carbon dioxide gas in line  27  is cooled to a carbon dioxide liquid  30  in line  28 .  
         [0083]    Electronic Processor EP regulates fluid-metering pumps MP, power propellant P, ignition system IS, heat exchangers HE 1 , HE 2  and HE 3 , heat exchanger AE, cabin heat exchanger CHE, fuel cell system FC, water condenser WC, solenoid actuated values S 1 -S 22 , thermocouples T 1 -T 11 , and pressure sensors P 1 -P 11 .  
         [0084]    The sulfur absorbent SA absorbent materials in zone  20  for the removal of elemental sulfur compounds from the hydrocarbon fuel  10  are made from various porous mixed metal oxide aerogel microspheres of cerium, zinc, strontium, magnesium, copper, lanthanum, barium, iron, yttrium, chromium, cobalt, vanadium, zirconium and precious metals.  
         [0085]    The steam reformer SR catalyst in zone  21  is made from mixed metal aerogel microspheres of nickel, copper, zinc, iron, cobalt, zirconium, chromium, rare earth metal, and precious metals.  
         [0086]    The metal oxide materials in zone  22  of the carbon monoxide scavenger CMS are made from porous aerogel microspheres of mixed metal M n  oxides O n  of nickel, manganese, tin, copper, silver, iron, zinc and chromium. The carbon monoxide scavenger CMS operates to remove carbon monoxide, in the following chemical formula proportions and reactions. MO 2 +2CO→M+2CO 2 , MO+CO→M+CO 2  and M 2 O+CO→2M+CO 2 .  
         [0087]    In an operational startup mode, propane fuel  10  and an air oxidizer  13  completely oxidizes said fuel in the oxidizer chamber OC. The exothermic chemical reaction of C 3 H 8 +4H 2 +7 O 2 +11.28 N 2 →3 CO 2 +8 H 2 O+11.28 N 2  ΔH 298 =−2220 kJ that heats the EVHG system to an operational temperature in a few seconds. The thermocouples T 1  and T 9  must both test less than about 650° F.  
         [0088]    In an operational mode, propane fuel  10  and a 60% hydrogen peroxide oxidizer  13  partially oxidizes said fuel in the partial oxidizer chamber PO. The exothermic chemical reaction of C 3 H 8 +1.68 H 2 O 2 +1.12 H 2 O→0.36 CO 2 +2.64 CO+1.12 H 2 O+5.68 H 2  ΔH 298 =−13.424 kJ heats the EVHG system to a sustained operational temperature. The pressure sensors P 2  and P 9  must both test between about 734 psi to about 1052 psi. Thermocouple T 9  at the pressure chamber PC must test between about 650° F. to the preferred hydrocarbon fuel combustion exothermic reaction temperature. Thermocouple T 2  at the collecting chamber CC must test between about 650° F. to the preferred zone reaction temperature as required for sulfur absorbing, steam reforming, and carbon monoxide scavenging. The exothermic temperature of the oxidizer chamber is controlled by regulating the oxidizer to hydrocarbon fuel ratio.  
         [0089]    In the operational mode, carbon monoxide is steam reformed to a pressurized gas stream yielding hydrogen fuel and carbon dioxide, The endothermic chemical reaction of 0.36 CO 2 +2.64 CO+2.66 H 2 O+5.68 H 2 →3 CO 2 +0.02 H 2 O+8.32 H 2  ΔH 298 =13.258 kJ that controls the heat of the EVHG system to a sustained operational temperature by varying the water  16  input from water-metering pump WMP. Thermocouple T 9  at the pressure chamber PC must test between about 650° F. to the preferred hydrocarbon fuel combustion exothermic reaction temperature. Thermocouple T 2  at the collecting chamber CC must test between about 650° F. to the preferred zone reaction temperature as required for sulfur absorbing, steam reforming, and carbon monoxide scavenging. Regulating the water input from water-metering pump CMP 1  controls the steam reformer chemical reaction and endothermic temperature of the pressurized gas stream.  
         [0090]    The steam  46  from heat exchanger HE 2  flows by way of line  54 , solenoid actuated value S 7 , and line  55  throughout a cabin heat exchanger CHE to atmosphere  56 . The cabin heat exchanger CHE heats the electric vehicle cabin  58  as per thermocouple T 7 .  
         [0091]    The carbon dioxide liquid  30  flows by way of lines  59  and  63 , solenoid actuated value S 8  and lines  64  and  55  throughout the cabin heat exchanger CHE to atmosphere  56 . The cabin heat exchanger CHE cools the electric vehicle cabin  58  as per thermocouple T 8 .  
         [0092]    Referring to FIG. 4 of the drawings, the fluid-metering pumps MP (e.g., FMP, OMP, WMP, RMP, CMP, PMP, HMP, HPP, and AMP) in conjunction with FIG. 1, FIG. 2 and FIG. 3. A pressurized carbon dioxide liquid  30  contained in the pressure tank CT is the propellant P in line  59  for powering the high-pressure fluid-metering pumps FMP, OMP, HPP, WMP, and RMP. The pressurized steam  46  propellants P from the heat exchanger HE 2  is also a propellant P in line  48  for powering the low-pressure fluid-metering pumps CMP, PMP, HMP, and AMP. Electronic Processor EP regulates fluid-metering pump MP flow by energizing switch  107  of a three-way solenoid actuated value S 22 . A large piston  108  compresses a small piston  109  which fluid amplifies the pneumatic pressure. The pneumatic pressure performs a pumping action comprising check ball values  110  and  111 . O-ring  112  seals the small piston. O-ring  113  seals the large piston. Return spring  114  returns the pistons to their power-stoke position, and the fluid ejects from the right end  104  to the left end  105 .  
         [0093]    Referring to FIG. 5 of the drawings is a view taken substantially as indicated by FIG. 1, FIG. 2 and FIG. 3.  
         [0094]    Referring to FIG. 6 of the drawings, We have set forth a direct acting reciprocating steam high-pressure air pump HPP. Each stroke of the rod  123  connecting pistons  122  and  135  fills or empties chambers  136  and  138  and empties or fills chambers  137  and  139 , which nearly doubles the flow rate (less the volume of the piston rod  123 ) over a single-acting force pump, it also smoothes the flow. The pressurized steam  51  propellant P enters the system through line  115  where the steam valves SV  1  and SV  2 , switch back and forth between lines  116  or  120  for intake and exhaust strokes. The air  52  from the atmosphere enters the system through line  128  where the air valves SV  5  and SV  6 , switch back and forth between lines  129  or  133  for intake and exhaust strokes. The compressed air exits the system through lines  130  or  132  where the air valves SV  7  and SV  8  switch back and forth between lines  130  and  132 .  
         [0095]    When the piston rod  123  of pistons  122  and  135  in cylinders  121  and  134  reaches the extreme right limit of its stroke, and rod collar  124  contacts limit  126  of limit switch LS- 127  and the following events occur in the following sequence:  
         [0096]    The pressurized steam propellant  51  from the heat exchanger HE 1  in line  115  for powering the direct acting reciprocating steam high-pressure air pump HPP  
         [0097]    (a) Steam valves SV  2  and SV  3  opens, SV  1  and SV  4  closes  
         [0098]    (b) Air valves SV  6  and SV  7  opens, SV  5  and SV  8  closes  
         [0099]    (c) Pistons  122  and  135  starts to extend left  
         [0100]    (d) Air is compressed in lines  131  and  132   
         [0101]    When the piston rod  123  of pistons  122  and  135  in cylinders  121  and  134  reaches the extreme left limit of its stroke, and rod collar  124  contacts limit  125  of limit switch LS- 127  and the following events occur in the following sequence:  
         [0102]    (e) Steam valves SV  1  and SV  4  opens, SV  2  and SV  3  closes  
         [0103]    (f) Air valves SV  5  and SV  8  opens, SV  6  and SV  7  closes  
         [0104]    (g) Pistons  122  and  135  starts to extend right  
         [0105]    (h) Air is compressed in lines  130  and  131 .  
         [0106]    Referring to FIGS.  7 - 16  of the drawings. We have set forth-theoretical weights or amounts of products, and reactants used in carrying out the invention from one gallon of hydrocarbon fuels of propane, methanol, gasoline, kerosene, and ethanol. Next, attention is directed to the operation of the hydrogen gas generator. we start with one gallon of hydrocarbon fuel as a base line and air from the atmosphere are fed into the partial oxidizer chamber; and water is fed into the steam reformer and its products of reaction pressurized fuel gas stream of carbon dioxide (CO 2 ) and hydrogen (H 2 ). The carbon monoxide scavenger converts any remaining carbon monoxide to a pressurized gas stream of carbon dioxide. The heat exchanger cools hydrogen and carbon dioxide gas within carbon dioxide liquid limits. The hydrogen and carbon dioxide separation separates pressurized hydrogen fuel from pressurized liquid-carbon dioxide.  
         [0107]    Referring to FIG. 7 of the drawings, is a theoretical computation of chemical formula of polymer-electrolyte membrane and circulating alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when methanol fueled and air-oxidized. The theoretical weights or amounts of products and reactants used in carrying out the invention starts with one gallon of propane (C 3 H 8 ) as a base line and 19.52 pounds of air from the atmosphere. The fuel and air are fed into the partial oxidizer chamber, and 0.77 gallons of water (H 2 O) is fed into the steam reformer and its products of reaction are a pressurized fuel gas stream of 12.51 pounds of carbon dioxide (CO 2 ) and 1.34 pounds of hydrogen (H 2 ). The polymer-electrolyte membrane fuel cell at 45 percent efficiency generates 8,980-watt hours per one gallon of propane fuel. The circulating alkaline-electrolyte fuel cell at 70 percent efficiency generates 13,969-watt hours per one gallon of propane fuel.  
         [0108]    Referring to FIG. 8 of the drawings, is a theoretical computation of chemical formula of polymer-electrolyte membrane and matrix alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when methanol fueled and air-oxidized. The theoretical weights or amounts of products and reactants used in carrying out the invention starts with one gallon of propane (C 3 H 8 ) as a base line and 7.32 pounds of 60 percent hydrogen peroxide. The fuel and hydrogen peroxide are fed into the partial oxidizer chamber, and 0.55 gallons of water (H 2 O) is fed into the steam reformer and its products of reaction are a pressurized fuel gas stream of 12.51 pounds of carbon dioxide (CO 2 ) and 1.59 pounds of hydrogen (H 2 ). The polymer-electrolyte membrane fuel cell at 45 percent efficiency generates 10,676-watt hours per one gallon of propane fuel. The circulating alkaline-electrolyte fuel cell at 70 percent efficiency generates 16,607-watt hours per one gallon of propane fuel.  
         [0109]    Referring to FIG. 9 of the drawings, is a theoretical computation of chemical formula of polymer-electrolyte membrane and circulating alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when methanol fueled and air-oxidized. The theoretical weights or amounts of products and reactants used in carrying out the invention starts with one gallon of methanol (CH 3 OH) as a base line and 7.08 pounds of air from the atmosphere. The fuel and air are fed into the partial oxidizer chamber, and 0.24 gallons of water (H 2 O) is fed into the steam reformer and its products of reaction are a pressurized fuel gas stream of 9.08 pounds of carbon dioxide (CO 2 ) and 1.04 pounds of hydrogen (H 2 ). The polymer-electrolyte membrane fuel cell at 45 percent efficiency generates 6984-watt hours per one gallon of propane fuel. The circulating alkaline-electrolyte fuel cell at 70 percent efficiency generates 10,863-watt hours per one gallon of propane fuel.  
         [0110]    Referring to FIG. 10 of the drawings, is a theoretical computation of chemical formula of polymer-electrolyte membrane and matrix alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when methanol fueled and air-oxidized. The theoretical weights or amounts of products and reactants used in carrying out the invention starts with one gallon of methanol (CH 3 OH) as a base line and 3.56 pounds of 60 percent hydrogen peroxide. The fuel and hydrogen peroxide are fed into the partial oxidizer chamber, and 0.13 gallons of water (H 2 O) is fed into the steam reformer and its products of reaction are a pressurized fuel gas stream of 9.08 pounds of carbon dioxide (CO 2 ) and 1.09 pounds of hydrogen (H 2 ). The polymer-electrolyte membrane fuel cell at 45 percent efficiency generates 7,333-watt hours per one gallon of propane fuel. The circulating alkaline-electrolyte fuel cell at 70 percent efficiency generates 11,407-watt hours per one gallon of propane fuel.  
         [0111]    Referring to FIG. 11 of the drawings, is a theoretical computation of chemical formula of polymer-electrolyte membrane and circulating alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when methanol fueled and air-oxidized. The theoretical weights or amounts of products and reactants used in carrying out the invention starts with one gallon of gasoline (C 8 H 18 ) as a base line and 28.19 pounds of air from the atmosphere. The fuel and air are fed into the partial oxidizer chamber, and 1.12 gallons of water (H 2 O) is fed into the steam reformer and its products of reaction are a pressurized fuel gas stream of 18.07 pounds of carbon dioxide (CO 2 ) and 1.74 pounds of hydrogen (H 2 ). The polymer-electrolyte membrane fuel cell at 45 percent efficiency generates 11,815-watt hours per one gallon of propane fuel. The circulating alkaline-electrolyte fuel cell at 70 percent efficiency generates 18,378-watt hours per one gallon of propane fuel.  
         [0112]    Referring to FIG. 12 of the drawings, is a theoretical computation of chemical formula of polymer-electrolyte membrane and matrix alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when methanol fueled and air-oxidized. The theoretical weights or amounts of products and reactants used in carrying out the invention starts with one gallon of gasoline (C 8 H 18 ) as a base line and 10.59 pounds of 60 percent hydrogen peroxide. The fuel and hydrogen peroxide are fed into the partial oxidizer chamber, and 0.80 gallons of water (H 2 O) is fed into the steam reformer and its products of reaction are a pressurized fuel gas stream of 18.07 pounds of carbon dioxide (CO 2 ) and 2.12 pounds of hydrogen (H 2 ). The polymer-electrolyte membrane fuel cell at 45 percent efficiency generates 14,257-watt hours per one gallon of propane fuel. The circulating alkaline-electrolyte fuel cell at 70 percent efficiency generates 22,178-watt hours per one gallon of propane fuel.  
         [0113]    Referring to FIG. 13 of the drawings, is a theoretical computation of chemical formula of polymer-electrolyte membrane and circulating alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when methanol fueled and air-oxidized. The theoretical weights or amounts of products and reactants used in carrying out the invention starts with one gallon of kerosene (C 12 H 26 ) as a base line and 40.83 pounds of air from the atmosphere. The fuel and air are fed into the partial oxidizer chamber, and 1.21 gallons of water (H 2 O) is fed into the steam reformer and its products of reaction are a pressurized fuel gas stream of 19.38 pounds of carbon dioxide (CO 2 ) and 1.85 pounds of hydrogen (H 2 ). The polymer-electrolyte membrane fuel cell at 45 percent efficiency generates 12,423-watt hours per one gallon of propane fuel. The circulating alkaline-electrolyte fuel cell at 70 percent efficiency generates 19,324-watt hours per one gallon of propane fuel.  
         [0114]    Referring to FIG. 14 of the drawings, is a theoretical computation of chemical formula of polymer-electrolyte membrane and matrix alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when methanol fueled and air-oxidized. The theoretical weights or amounts of products and reactants used in carrying out the invention starts with one gallon of kerosene (C 12 H 26 ) as a base line and 10.97 pounds of 60 percent hydrogen peroxide. The fuel and hydrogen peroxide are fed into the partial oxidizer chamber, and 0.87 gallons of water (H 2 O) is fed into the steam reformer and its products of reaction are a pressurized fuel gas stream of 19.38 pounds of carbon dioxide (CO 2 ) and 2.26 pounds of hydrogen (H 2 ). The polymer-electrolyte membrane fuel cell at 45 percent efficiency generates 15,156-watt hours per one gallon of propane fuel. The circulating alkaline-electrolyte fuel cell at 70 percent efficiency generates 23,575-watt hours per one gallon of propane fuel.  
         [0115]    Referring to FIG. 15 of the drawings, is a theoretical computation of chemical formula of polymer-electrolyte membrane and circulating alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when methanol fueled and air-oxidized. The theoretical weights or amounts of products and reactants used in carrying out the invention starts with one gallon of ethanol (C 2 H 6 O) as a base line and 12.20 pounds of air from the atmosphere. The fuel and air are fed into the partial oxidizer chamber, and 0.55 gallons of water (H 2 O) is fed into the steam reformer and its products of reaction are a pressurized fuel gas stream of 12.58 pounds of carbon dioxide (CO 2 ) and 1.37 pounds of hydrogen (H 2 ). The polymer-electrolyte membrane fuel cell at 45 percent efficiency generates 9,207-watt hours per one gallon of propane fuel. The circulating alkaline-electrolyte fuel cell at 70 percent efficiency generates 14,321-watt hours per one gallon of propane fuel.  
         [0116]    Referring to FIG. 16 of the drawings, is a theoretical computation of chemical formula of polymer-electrolyte membrane and matrix alkaline-electrolyte fuel cell efficiencies of the hydrogen gas generator when methanol fueled and air-oxidized. The theoretical weights or amounts of products and reactants used in carrying out the invention starts with one gallon of ethanol (C 2 H 6 O) as a base line and 6.12 pounds of 60 percent hydrogen peroxide. The fuel and hydrogen peroxide are fed into the partial oxidizer chamber, and 0.36 gallons of water (H 2 O) is fed into the steam reformer and its products of reaction are a pressurized fuel gas stream of 12.58 pounds of carbon dioxide (CO 2 ) and 1.46 pounds of hydrogen (H 2 ). The polymer-electrolyte membrane fuel cell at 45 percent efficiency generates 9,812-watt hours per one gallon of propane fuel. The circulating alkaline-electrolyte fuel cell at 70 percent efficiency generates 15,264-watt hours per one gallon of propane fuel.  
         [0117]    Unfortunately, not all the power from the fuel cell FC comes out as useful electric power for performing desired work. Combustion and thermal inefficiencies cause loss of energy in the hydrogen fuel generator, chemical reaction losses, and fuel cell losses. Therefore, the power output of the hydrocarbon fueled, hydrogen fuel generator, and control system EVHG is equal to the theoretical power minus all the power losses.  
         [0118]    Having described only typical preferred forms and applications of our invention, We do not wish to be limited to the specific details here in set forth but wish to reserve to ourselves any modifications and/or variations that might appears to those skilled in the art and that fall within the scope of the following claims.