A process for preparing C.sub.2 to C.sub.5 hydrocarbons includes introducing a feed stream into a reaction zone of a reactor, the feed stream including hydrogen gas and carbon monoxide. An additional stream is introduced into the reaction zone of the reactor, the additional stream comprising water, carbon dioxide, or mixtures thereof. A combined stream that includes the feed stream and the additional stream is converted into a product stream comprising C.sub.2 to C.sub.5 hydrocarbons in the reaction zone in the presence of a hybrid catalyst. The hybrid catalyst includes a metal oxide catalyst component, and a microporous catalyst component.

A method is disclosed for rejuvenation a cobalt Fischer Tropsch catalyst used in a Fischer Tropsch process operating in recycle mode. The method permits the use of specific inert gases to adjust the mole weight of the gas so that the recycle compressor designed for normal steady state operation can also be used in the method. Hydrogen from a membrane permeate stream is added to the reactor loop at a temperature between 300 F and 400 F and the carbon oxides are reacted out to purify the hydrogen. This stream is continuously recycled and the temperature is raised to between 425 F and 500 F and held at the final temperature for between 4 hours and 48 hours. The cobalt Fischer Tropsch catalyst is effectively rejuvenated in-situ by the method.

A method is disclosed for rejuvenation a cobalt Fischer Tropsch catalyst used in a Fischer Tropsch process operating in recycle mode. The method permits the use of specific inert gases to adjust the mole weight of the gas so that the recycle compressor designed for normal steady state operation can also be used in the method. Hydrogen from a membrane permeate stream is added to the reactor loop at a temperature between 300 F and 400 F and the carbon oxides are reacted out to purify the hydrogen. This stream is continuously recycled and the temperature is raised to between 425 F and 500 F and held at the final temperature for between 4 hours and 48 hours. The cobalt Fischer Tropsch catalyst is effectively rejuvenated in-situ by the method.

A process for preparing C.sub.2 to C.sub.5 olefins includes introducing a feed stream comprising hydrogen and at least one carbon-containing component selected from the group consisting of CO, CO.sub.2, and mixtures thereof into a reaction zone. The feed stream is contacted with a hybrid catalyst in the reaction zone, and a product stream is formed that exits the reaction zone and includes C.sub.2 to C.sub.5 olefins. The hybrid catalyst includes a methanol synthesis component and a solid microporous acid component that is selected from molecular sieves having 8-MR access and having a framework type selected from the group consisting of CHA, AEI, AFX, ERI, LTA, UFI, RTH, and combinations thereof. The methanol synthesis component comprises a metal oxide support and a metal catalyst. The metal oxide support includes titania, zirconia, hafnia or mixtures thereof, and the metal catalyst includes zinc.

A supported catalyst and preparation method thereof, the catalyst comprising an organic polymer material carrier and Raney alloy particles supported on the organic polymer material carrier, wherein substantially all of the Raney alloy particles are partially embedded in the organic polymer material carrier. The catalyst can be used in hydrogenation, dehydrogenation, amination, dehalogenation or desulfuration reactions.

Embodiments of the present invention relates to two improved catalysts and associated processes that directly converts carbon dioxide and hydrogen to liquid fuels. The catalytic converter is comprised of two catalysts in series that are operated at the same pressures to directly produce synthetic liquid fuels or synthetic natural gas. The carbon conversion efficiency for CO.sub.2 to liquid fuels is greater than 45%. The fuel is distilled into a premium diesel fuels (approximately 70 volume %) and naphtha (approximately 30 volume %) which are used directly as “drop-in” fuels without requiring any further processing. Any light hydrocarbons that are present with the carbon dioxide are also converted directly to fuels. This process is directly applicable to the conversion of CO.sub.2 collected from ethanol plants, cement plants, power plants, biogas, carbon dioxide/hydrocarbon mixtures from secondary oil recovery, and other carbon dioxide/hydrocarbon streams. The catalyst system is durable, efficient and maintains a relatively constant level of fuel productivity over long periods of time without requiring re-activation or replacement.

Embodiments of the present invention relates to two improved catalysts and associated processes that directly converts carbon dioxide and hydrogen to liquid fuels. The catalytic converter is comprised of two catalysts in series that are operated at the same pressures to directly produce synthetic liquid fuels or synthetic natural gas. The carbon conversion efficiency for CO.sub.2 to liquid fuels is greater than 45%. The fuel is distilled into a premium diesel fuels (approximately 70 volume %) and naphtha (approximately 30 volume %) which are used directly as “drop-in” fuels without requiring any further processing. Any light hydrocarbons that are present with the carbon dioxide are also converted directly to fuels. This process is directly applicable to the conversion of CO.sub.2 collected from ethanol plants, cement plants, power plants, biogas, carbon dioxide/hydrocarbon mixtures from secondary oil recovery, and other carbon dioxide/hydrocarbon streams. The catalyst system is durable, efficient and maintains a relatively constant level of fuel productivity over long periods of time without requiring re-activation or replacement.

Fischer-Tropsch process for the synthesis of hydrocarbons by bringing a feedstock including synthesis gas into contact with a catalyst prepared by the following: a porous support is brought into contact with a cobalt metal salt of which the melting point of the cobalt metal salt is between 30 and 150° C. for between 5 minutes and 5 hours, in order to form a solid mixture, the weight ratio of said cobalt metal salt to the porous oxide support being between 0.1 and 1; the solid mixture obtained is heated with stirring under atmospheric pressure at a temperature between the melting point of the cobalt metal salt and 200° C. for a period of time of between 30 minutes and 12 hours; the solid obtained is calcined at a temperature above 200° C. and below or equal to 1100° C.

Processes for forming multimetallic catalysts by grafting nickel precursors to metal oxide supports. Dry reforming reaction catalysts having nickel and promotors grafted to metal oxides supports. Methanation reaction catalysts having nickel and promotors grafted to metal oxides supports.

Processes for forming multimetallic catalysts by grafting nickel precursors to metal oxide supports. Dry reforming reaction catalysts having nickel and promotors grafted to metal oxides supports. Methanation reaction catalysts having nickel and promotors grafted to metal oxides supports.