NOVELTY - A dehydrogenation device (3) generates aromatic compound and hydrogen, by dehydrogenation of hydrogenation aromatic compound using dehydrogenation catalyst having equilibrium conversion of hydrogenation aromatics compound of 90% or more at reaction temperature of 300degreesC. A vapor-liquid separator (9), separates liquid component of aromatic compound and gas component of hydrogen.    USE - For supplying hydrogen to fuel cell mounted on ships, air crafts, motor vehicles, rail vehicle, airplane, rocket, submarine, and for large and small size fuel cell of domestic and business use generator, automatic vending machine, fixed fuel cell power supply.    ADVANTAGE - Hydrogen of high yield is obtained steadily without requiring use of heat insulation container which accommodates high pressure vessel, and liquid of ultra low temperature, by using hydrogenation aromatic compound. Requirement of complicated heat control is made unnecessary.    DETAILED DESCRIPTION - A purification device (6) removes impurity gases from the obtained hydrogen gas. Hydrogen is supplied to fuel cell mounted in vehicle, aircraft, ship, fixed type fuel cell power supply. Hydrogenation aromatics compound are mixture of cyclohexane, methylcyclohexane, decalin, and methyl decalin. The tank loaded with hydrogenation aromatics compound is divided with movable partition plate and is integrated with tank used for storing dehydrogenation product. The dehydrogenation catalyst has catalyst metal and alkaline metal supported by porous (gamma) alumina carrier having preset size pore, pore surface area and ph value fluctuating between specific regions. The catalyst metal is platinum of 0.3 -2.0 wt.% while the alkaline metal is potassium of 0.001- 1.0 wt.%. When impregnating platinum compound solution into the porous carrier, pH value of the impregnation solution is adjusted between 1.8-3.0. Metal dispersion degree of the noble metals after catalyzation is 60.% or more. The solution impregnated carrier is baked and dried. Then solution of alkaline metal is impregnated on the carrier and dried. Then final hydrogen reduction is implemented directly without baking the carrier. The drying operation is performed at room temperature of 200degreesC for 0.5-24 hours. Final hydrogen reduction is implemented using hydrogen air flow of temperature 350-550degreesC and at reduction condition of 0.5-48 hours. The dehydrogenation is preformed at preset conditions. The hydrogen generation velocity of the dehydrogenation catalyst is more than 900 Ncc/h/cc-cat. The adsorption agent filled in the hydrogen purification device is zeolite. The regeneration processing of the adsorption area of the hydrogen purification device is performed at heating temperature of 100-250 degreesC. The recovered gas component from the regenerated adsorption area is condensed and is returned to raw material tank or is discarded by burning. The hydrogenation device is connected to the electric heater.    DESCRIPTION OF DRAWING(S) - The figure shows a schematic view of the hydrogen supply apparatus. (Drawing includes non-English language text).    dehydrogenation device (3)    reactor heater (4)    vapor liquid separation devices (5,9)    hydrogen purification device (6)