A process for preparing C.sub.2 to C.sub.3 olefins includes introducing a feed stream having a volumetric ratio of hydrogen to carbon monoxide from greater than 0.5:1 to less than 5:1 into a reactor, and contacting the feed stream with a bifunctional catalyst. The bifunctional catalyst includes a Cr/Zn oxide methanol synthesis component having a Cr to Zn molar ratio from greater than 1.0:1 to less than 2.15:1, and a SAPO-34 silicoaluminophosphate microporous crystalline material. The reactor operates at a temperature ranging from 350 C. to 450 C., and a pressure ranging from 10 bar (1.0 MPa) to 60 bar (6.0 MPa). The process has a cumulative productivity of C.sub.2 to C.sub.3 olefins greater than 15 kg C.sub.2 to C.sub.3 olefins/kg catalyst.

A process for preparing C.sub.2 to C.sub.3 olefins includes introducing a feed stream having a volumetric ratio of hydrogen to carbon monoxide from greater than 0.5:1 to less than 5:1 into a reactor, and contacting the feed stream with a bifunctional catalyst. The bifunctional catalyst includes a Cr/Zn oxide methanol synthesis component having a Cr to Zn molar ratio from greater than 1.0:1 to less than 2.15:1, and a SAPO-34 silicoaluminophosphate microporous crystalline material. The reactor operates at a temperature ranging from 350 C. to 450 C., and a pressure ranging from 10 bar (1.0 MPa) to 60 bar (6.0 MPa). The process has a cumulative productivity of C.sub.2 to C.sub.3 olefins greater than 15 kg C.sub.2 to C.sub.3 olefins/kg catalyst.

Direct conversion of syngas produces liquid fuels and light olefins. The catalytic reaction is conducted on a fixed bed or a moving bed. The catalyst comprises A and B components. The component A is composed of active metal oxides, and the active ingredients of the component B are zeolites with a MEL structure. The distance between the geometric centers of catalyst A and catalyst B particles is 2 nm-10 mm; a weight ratio of the catalyst A to the catalyst B is 0.1-20. The pressure of the syngas is 0.1-10 MPa; reaction temperature is 300-600 C.; and space velocity is 300-10000 h.sup.1. The reaction mainly produces gasoline with high octane number, and co-generates light olefins. Meanwhile, the selectivity for a methane byproduct is low (less than 10%).

Direct conversion of syngas produces liquid fuels and light olefins. The catalytic reaction is conducted on a fixed bed or a moving bed. The catalyst comprises A and B components. The component A is composed of active metal oxides, and the active ingredients of the component B are zeolites with a MEL structure. The distance between the geometric centers of catalyst A and catalyst B particles is 2 nm-10 mm; a weight ratio of the catalyst A to the catalyst B is 0.1-20. The pressure of the syngas is 0.1-10 MPa; reaction temperature is 300-600 C.; and space velocity is 300-10000 h.sup.1. The reaction mainly produces gasoline with high octane number, and co-generates light olefins. Meanwhile, the selectivity for a methane byproduct is low (less than 10%).

A method for preparing aromatics from syngas, which includes a) contacting a raw material stream containing syngas with a catalyst in a reaction zone under reaction conditions sufficient to convert at least part of the raw material to obtain a reaction effluent; b) separating the reaction effluent to obtain at least a recycle stream containing gas-phase hydrocarbons having 1 to 4 carbon atoms and unconverted syngas and a liquid stream containing hydrocarbons having 5 or more carbon atoms; c) returning the recycle stream to the reaction zone; and d) separating aromatic products from the liquid stream, wherein the catalyst includes at least one of an inert carrier-confined highly dispersed metal oxide material, an acidic molecular sieve, and, optionally, graphite powder and a dispersant.

Methods for preparing selective catalytic metal microstructures and nanostructures having at least one surface ligand. The methods include providing a preliminary metal microstructure or nanostructure having at least one preliminary surface ligand, and replacing the preliminary surface ligand with at least one surface ligand to provide the catalytic metal microstructure or nanostructure.

Synthesis of aromatic hydrocarbons from synthesis gas in a fixed bed or a moving bed reactor loaded with a composite catalyst comprising Catalyst Component A and Catalyst Component B mixed via a mechanical mixing mode, wherein the active ingredient of the Catalyst Component A is active metal oxides; and the Catalyst Component B is one or both of ZSM-5 zeolite and metal modified ZSM-5; the pressure of the synthesis gas is 0.1-6 MPa; the reaction temperature is 300-600 C.; and the space velocity is 500-8000 h.sup.1. The reaction process has a high product yield and selectivity, with the selectivity of aromatics reaching 50-85%, while the selectivity of the methane byproduct is less than 15%.

Synthesis of aromatic hydrocarbons from synthesis gas in a fixed bed or a moving bed reactor loaded with a composite catalyst comprising Catalyst Component A and Catalyst Component B mixed via a mechanical mixing mode, wherein the active ingredient of the Catalyst Component A is active metal oxides; and the Catalyst Component B is one or both of ZSM-5 zeolite and metal modified ZSM-5; the pressure of the synthesis gas is 0.1-6 MPa; the reaction temperature is 300-600 C.; and the space velocity is 500-8000 h.sup.1. The reaction process has a high product yield and selectivity, with the selectivity of aromatics reaching 50-85%, while the selectivity of the methane byproduct is less than 15%.

The invention relates to a catalyst containing an active cobalt phase, deposited on a support comprising alumina, silica or silica-alumina, said support also containing a mixed oxide phase containing cobalt and/or nickel, said catalyst having been prepared by introducing at least one hydrocarbon organic compound of formula C.sub.xH.sub.y. The invention also relates to the use thereof in the field of Fischer-Tropsch synthesis processes.

A process for preparing C.sub.2 to C.sub.3 olefins includes introducing a feed stream having a volumetric ratio of hydrogen to carbon monoxide from greater than 0.5:1 to less than 5:1 into a reactor, and contacting the feed stream with a bifunctional catalyst. The bifunctional catalyst includes a Cr/Zn oxide methanol synthesis component having a Cr to Zn molar ratio from greater than 1.0:1 to less than 2.15:1, and a SAPO-34 silicoaluminophosphate microporous crystalline material. The reactor operates at a temperature ranging from 350 C. to 450 C., and a pressure ranging from 10 bar (1.0 MPa) to 60 bar (6.0 MPa). The process has a cumulative productivity of C.sub.2 to C.sub.3 olefins greater than 15 kg C.sub.2 to C.sub.3 olefins/kg catalyst.