GB999103A - Process for the production of gas containing hydrogen by conversion of hydrocarbons - Google Patents

Abstract

A modification of the process for manufacturing hydrogen containing gases according to the parent Specification wherein the catalyst is feebly active, i.e. it contains less than 1% by weight of Ni. The cyclic and catalytic conversion of hydrocarbons such as propane, butane or petrol is succeeded by a second stage in which at least the gases from the conversion phase are passed at a temperature of 150-250 DEG C. over a hydrogenation catalyst to effect saturation of the alkenes present. A heat exchanger may be interposed between the two stages. The hydrogenation catalyst may be a metal of Group IB or VIII of the Periodic Table or a compound thereof (e.g. a molybdate or thiomolybdate). The hydrogenation catalyst carrier may be alumina, silica gel or porous cement. The gases from the cyclic and catalytic conversion of the first stage may be passed over the hydrogenation catalyst during the heating phase and steam may be passed over the hydrogenation catalyst during the steaming phase of the first stage. The heating phase may be succeeded by a reduction phase during which a hydrogen rich gas is passed through both stages. A plurality of cyclic and catalytic conversion stages may be arranged in parallel to feed a single hydrogenation stage. When the hydrogenation stage is not being fed with gases from the first stage, it may be fed from an independent source of hydrocarbons different from those obtained from the conversion phase of the first stage. In an alternative embodiment, the feebly active catalyst may be replaced by a non-catalytic material (e.g. granular magnesia). Hydrogenated gases from the optional reducing phase may be mixed with hydrogenated gases previously prepared. The product may wholly or partly replace natural gas for heating purposes.ALSO:In a modification of the process for manufacturing hydrogen-containing gases according to the parent Specification, the catalyst is feebly active, i.e. it contains less than 1% by weight Ni and the cyclic and catalytic conversion of hydrocarbons such as propane, butane or petrol is succeeded by a second stage in which at least the gases from the conversion phase are passed at a temperature of 150-250 DEG C. over a hydrogenation catalyst to effect saturation of the alkenes present. A heat exchanger may be interposed between the two stages. The hydrogenation catalyst may be a metal of Group IB or VIII of the Periodic Table or a compound thereof (e.g. a molybdate or thiomolybdate). The hydrogenation catalyst carrier may be alumina, silica gel or porous cement. The gases from the cyclic and catalytic conversion of the first stage may be passed over the hydrogenation catalyst during the heating phase and steam may be passed over the hydrogenation catalyst during the steaming phase of the first stage. The heating phase may be succeeded by a reduction phase during which a hydrogen rich gas is passed through both stages. A plurality of cyclic and catalytic conversion stages may be arranged in parallel to feed a single hydrogenation stage. When the hydrogenation stage is not being fed with gases from the first stage, it may be fed from an independent source of hydrocarbons different from those obtained from the conversion phase of the first stage. In an alternative embodiment, the feebly active catalyst may be replaced by a non-catalytic material (e.g. granular magnesia). Hydrogenated gases from the optical reducing phase may be mixed with hydrogenated gases previously prepared. The product may wholly or partially replace natural gas for heating purposes.