TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Components: The catalyst exhibits a composite structure. The catalyst is a group VIII transition element such as cobalt, molybdenum, iron and/or nickel (preferably molybdenum-cobalt); a composite catalyst such as alkaline earth metal oxides, silicon and/or silicon oxide; and VIIIB element and f- or a d-transition metal, preferably vanadium, chromium, manganese, molybdenum, palladium, platinum or rare earth metals. The composite catalyst is an inert component such as oxides and/or hydroxides of alkaline-earth metal, silicon, aluminum, boron and/or titanium, where caustically burned magnesia and/or freshly precipitated magnesium hydroxide with a specific surface area of greater than 1 m2/g is particularly preferred.    TECHNOLOGY FOCUS - INSTRUMENTATION AND TESTING - Preferred Components: The catalyst, in the gas station plant, is a nano-structured catalyst. The cooling device is able to convert the exhaust gas of the reformers into a cooled, liquid hydrogen-containing fluid. The gas station plant further comprises a mixing apparatus for mixing the hydrogen-containing gas or liquid with a hydrocarbon gas or liquid; a measuring and a metering unit; an inlet for a hydrocarbon-containing feed gas and a device with a reactor. The reformer has an inlet and discharge mechanism for continuous feeding and removal of the catalyst. The reformer, in the gas station plant, is a steam reformer. The reactor exhibits a pre-heating zone, which is appropriate preferably at an operating temperature of 100-900degreesC. The discharge port for the reactor gas is intended in the pre-heating zone (preferred) or the heating zone. The cooling zone is designed for operating at 100-600degreesC and/or the heating zone is designed for operating at 300-1400degreesC, preferably 500-1000degreesC. The discharge port for the catalyst and the produced solid carbon is intended in the cooling zone. A constantly decreasing temperature gradient from the heating to the cooling zone is intended in the reactor. The inlet of the catalyst is intended in the heating zone or optionally in the pre-heating zone. The heating zone of the reactor comprises winding heater or gas burner apart from heating strips. The heating and cooling zone constitutes up to 50%, preferably up to 30%, of the length of the reactor from the feed gas-inlet to the reactor gas-discharge port. The device further comprises a pressure control valve at the reactor for a high pressure of 1-500 mbar, preferably 90-250 mbar. The device is a mechanical device, preferably a conveyer, a conveyer revolving tube or a conveyer band that is intended at the catalyst through the reactor. The device further comprises an adsorption plant with alternating pressure after the reactor gas-discharge port, a filter after the reactor gas-discharge port and optionally before an adsorption plant with alternating pressure, a reactor gas compressor after the reactor gas-discharge port and optionally after a filter, and/or a quantity regulation mechanism for the feed gas and optionally feed gas compressor in each case before the feed gas-inlet.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Process: The catalyst is a nano-structured catalyst, at which the feed gas is converted to hydrogen and nano-carbon. At least a part of the exhaust gas of the reformer is led into a steam reformer, in which the remaining feed gas reacts with water vapor to form hydrogen. The exhaust gas of the reformer is preheated before entering into the steam reformer. The exhaust gas of the steam reformer is post-combusted for the removal of carbon monoxide, where preferably the exhaust gas of the reformer is combined with the hydrogen-containing gas mixture leaving the steam reformer and cooled down before the post-combustion. The catalyst is arranged on a carrier, preferably a laminar carrier such as particulate ceramic- or glass bodies. The catalyst is continuously fed in and out of the reformer, optionally with respect to the hydrogen content in the exhaust gas, where the catalyst and the feed gas are preferably led either in direct or counter current into the reformer. The feed gas in the reformer is contacted with the catalyst at 300-1400degreesC, preferably 400-700degreesC. The catalyst in the reformer is removed continuously or batch-wise and is separated from adhering carbon compounds, where the catalyst is preferably mechanically separated from the adhering carbon compounds, especially by scraping off or in a cyclone; the catalyst is preferably chemically separated from adhering carbon compounds, especially by an etching technique; or the catalyst is preferably separated physically from adhering carbon compounds by high temperature treatment, radio frequency- or high frequency induction heating. The feed gas is natural gas or optionally prepurified biogas. A part of the feed gas is used as heating gas for heating the reformer. The waste heat of the steam reformer is used for preheating the feed gas for the reformer and/or heating-up of the reformer. In the procedure for the production of a hydrogen-containing gas, the catalyst is led towards the catalyst discharge port and optionally the produced solid carbon is cooled down. In the reactor the catalytic cracking of the feed gas is accomplished at an excess pressure of 1-500 mbar, preferably 90-250 mbar. The hydrogen is separated from the reactor gas. The average retention time of the feed gas in the reactor is 5-100 seconds, preferably 10-15 seconds. The input pressure of the feed gas and the initial pressure of the reactor gas at the reactor are essentially identical. The feed gas is natural gas or methane. EXAMPLE - A gas mixture containing methane (94%) and hydrogen (6%) was fed into an oven with nitrogen. The gas mixture was contacted with molybdenum-cobalt-powder-catalyst with magnesium. The gas flow was set to 2500 Nccm and was heated. The heating rate was 10degreesC/min and the crack process temperature was 850degreesC for 10 hours. The addition of hydrogen and methane flow was adjusted to 2500 Nccm, half an hour after reaching the process temperature. The obtained exhaust fume contains up to 82 vol.% of hydrogen.