An anatase titanium dioxide includes at least one compound selected from oxides of Si, Al, and Zr in an amount of 2-50% b.w., calculated as oxides, of a total weight of the oxides, and a sulfur content of less than 150 ppm based on the total weight of the oxides.

An anatase titanium dioxide includes at least one compound selected from oxides of Si, Al, and Zr in an amount of 2-50% b.w., calculated as oxides, of a total weight of the oxides, and a sulfur content of less than 150 ppm based on the total weight of the oxides.

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.

Integrated liquid fuel catalytic partial oxidation (CPOX) reformer and fuel cell systems can include a plurality or an array of spaced-apart CPOX reactor units, each reactor unit including an elongated tube having a gas-permeable wall with internal and external surfaces. The wall encloses an unobstructed gaseous flow passageway. At least a portion of the wall has CPOX catalyst disposed therein and/or comprising its structure. The catalyst-containing wall structure and open gaseous flow passageway enclosed thereby define a gaseous phase CPOX reaction zone, the catalyst-containing wall section being gas-permeable to allow gaseous CPOX reaction mixture to diffuse therein and hydrogen rich product reformate to diffuse therefrom. The liquid fuel CPOX reformer also can include a vaporizer, one or more igniters, and a source of liquid reformable fuel. The hydrogen-rich reformate can be converted to electricity within a fuel cell unit integrated with the CPOX reactor unit.

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 of preparing a catalyst comprising a) contacting a titanium-containing compound, a solvating agent, and a solvent to form a solution; b) contacting the solution with a chrominated silica-support to form a pre-catalyst; and c) thermally treating the pre-catalyst by heating to a temperature of from about 400 C. to about 1000 C. for a time period of from about 1 minute to about 24 hours to form the catalyst.

A method of preparing a catalyst comprising a) contacting a titanium-containing compound, a solvating agent, and a solvent to form a solution; b) contacting the solution with a chrominated silica-support to form a pre-catalyst; and c) thermally treating the pre-catalyst by heating to a temperature of from about 400 C. to about 1000 C. for a time period of from about 1 minute to about 24 hours to form the catalyst.

Disclosed is an olefin production method which includes: (a) providing the regenerated catalyst and the hydrocarbon including not less than 90 wt % of LPG into Riser of Fast Fluidization Regime, and dehydrogenating in the presence of an alumina type catalyst; (b) separating an effluent from the dehydrogenation reaction into the catalyst and propylene mixture; (c) stripping to remove the hydrocarbon compound included in the catalyst separated at stage (b); (d) mixing the catalyst stripped at stage (c) with the gas including oxygen, and continuously regenerating it; (e) recycling the catalyst regenerated at stage (d) to stage (a), and providing it again into Riser; and (f) producing propylene product by cooling, compressing and separating propylene mixture of the reaction product separated at stage (b).