TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Components: The feed gas mixture in (P1) comprises a primary alcohol selected from methanol and/or ethanol.Preferred Method: (P1) additionally involves introducing hydrogen from the reforming product mixture and oxygen into a fuel cell to produce electric power.The feed gas mixture is contacted with the reforming catalyst at a temperature of below 400 (preferably 200 - 375, especially 250 - 325) degrees C.The reforming catalyst/the dehydrogenation catalyst is incorporated onto the surface of a pellet or a monolith substrate.The reforming catalyst/dehydrogenation catalyst comprises a nickel sponge supporting structure.When the alcohol is ethanol, the reforming catalyst has a thermal conductivity of at least about 50 (preferably at least 70) W/mxK at 300K.(P2) further involves transferring the heat of combustion produced in the combustion chamber to the dehydrogenation reaction zone; or capturing the energy of combustion for the generation of mechanical and/or additional electric power.The energy of combustion from the combustion chamber is used to drive a generator for the production of additional electric power.The dehydrogenation catalyst and the combustion chamber are part of a vehicular power system and the electric power and/or the mechanical power produced is used to drive the vehicle.(P2) also involves introducing a separate cold start fuel source into the combustion chamber and combusting the separate cold start fuel source in the presence of oxygen.The fuel cell effluent and the cold start fuel source are introduced into a combustion chamber of a flexible fuel source internal combustion engine capable of combusting methane and/or the separate cold start fuel source.The dehydrogenation zone and the flexible fuel source internal combustion engine are part of a vehicular power system and (P2) additionally involves capturing the energy of combustion for the generation of mechanical and/or additional electric power and using the mechanical power and/or the electric power to drive the vehicle.The feed gas mixture is contacted with the dehydrogenation catalyst at a temperature of below 400 (preferably 250 - 300) degrees C.    TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Catalyst: The reforming catalyst and the dehydrogenation catalyst have a surface area of 10 - 100 (preferably 25 - 100, especially 30 - 80) m2/g as measured by the Brunauer-Emmett-Teller method.The reforming catalyst and the dehydrogenation catalyst comprise at least 10 (preferably 10 - 90, or 10 - 80, especially 20 - 45) wt.% of copper.The metal sponge supporting structure of the reforming catalyst/the dehydrogenation catalyst has a surface area of at least 10 (preferably at least 50, especially 70) m2/g as measured by the Brunauer-Emmett-Teller method.The metal sponge supporting structure comprises nickel (at least 50, preferably at least 85 wt.%).The reforming/dehydrogenation catalyst comprises 5 - 100 (preferably 10 - 80, especially 15 - 75) micromol/g of nickel at the surface of the catalyst.In (P2), the feed gas mixture further comprises water.The dehydrogenation reaction zone further comprises a water-gas shift catalyst effective for catalyzing the water-gas shift reaction between carbon monoxide produced by the dehydrogenation of ethanol and water to form carbon dioxide and hydrogen.The water-gas shift catalyst is separate from the dehydrogenation catalyst. EXAMPLE - A copper-plated nickel sponge catalyst was prepared as follows: RANEY 4200 (RTM; a nickel sponge supporting structure) (68.7 g) was suspended in nitrogen sparged water (400 ml). A solution of 12% NaBH4 (50 g) in 14 M NaOH was added with stirring. After 10 minutes of stirring, the catalyst was allowed to settle and the supernatant decanted. An additional portion of nitrogen-sparged water was added and stirred. The catalyst was again settled and the rinse was decanted. A nitrogen-sparged water (250 ml) was added to the catalyst. Glacial acetic acid (8 ml) was added to reduce the pH to 5. The catalyst suspension was then contacted with a nitrogen-sparged solution of CuSO4.5H2O (54 g) and tetrasodium EDTA dehydrate (108 g) in water (300 ml). 2.5 N NaOH (3 ml) was added over 103 minutes. The pH of the suspension rose form 6.8 to 11.3. The catalyst was allowed to settle and the blue supernatant was decanted. CuSO4.5H2O (67.5 g) was dissolved in nitrogen-sparged water (200 ml) to form a copper solution. A catalyst suspension was formed by adding a hot (74 degrees C) mixture of 50% gluconic acid (159 g), 2.5 N NaOH (54 ml) and nitrogen-sparged water (250 ml) to the catalyst. The copper solution was then added to the catalyst suspension with stirring over 95 minutes while the heat was applied at 72 degrees C. The pH fell from 3.8 to 3.1. The catalyst was settled and the green supernatant was decanted. The catalyst was rinsed with nitrogen-sparged water (700 ml). The rinse was decanted and 75.6 g of a dull copper colored catalyst was recovered and the composition of the catalyst was 66.1% Ni, 30.4% Cu and 3.5% Al. A reactor was charged by depositing silicon carbide (1 g) initially, followed by a slurry comprising the catalyst (2.50 g) and silicon carbide (5 g). Temperature was monitored by a thermocouple inserted down the bore of the reactor to a position approximately 10.2 cm above the bottom of the catalyst bed. The reactor was operated such that the temperature of the product mixture exiting the catalyst bed was maintained at 280 degrees C. The temperature of the upper thermocouple remained relatively constant at 430 degrees C. An ethanol/water feed mixture (70:30 ethanol/water) was introduced to the dehydrogenation zone at a rate of 0.3 ml/minute with 100 sccm of nitrogen. The reactor was operated for 44 hours and the pressure rose from 28 to 80 psig. No ethanol or acetaldehyde was detected in the product mixture during this period and conversion to methane was 100% within analytical uncertainty. The yield of ethanol reforming products CO/CO2% at time of 2, 5, 12, 20, 25, 31, 35, 40 and 44 hours was 34/66, 60/40, 81/19, 85/15, 85/15, 88/12, 88/12, 88/12 and 87/12 using the 70% ethanol feed at 280 degrees C.