The present application discloses a supported PtZn intermetallic alloy catalyst, a method for preparing the same and application thereof. The catalyst uses SiO.sub.2 as a support and Zn as a promoter, and a small amount of active component Pt is supported; the weight percentage of Pt is 0.025%-1%, and the weight percentage of Zn is 0.025%-1.7%, a co-impregnation method is adopted in preparation, the SiO.sub.2 support is impregnated in aqueous solution of chloroplatinic acid and zinc nitrate, and then drying and high-temperature reduction are performed to obtain a PtZn/SiO.sub.2 catalyst. The catalyst has the advantages of high activity, high stability, low price and low toxicity. The catalyst provided by the present application is applicable to preparation of alkene through short-chain alkane dehydrogenation, in particular to preparation of propylene through propane dehydrogenation in a hydrogen atmosphere. Under high-temperature conditions, the dehydrogenation activity is very high, the propylene selectivity can reach more than 90%, the stability is good, and the amount of used Pt is small, the utilization rate is high, and it is cheaper than industrial Pt series catalysts.

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.

Methods for gas-phase deoxygenation of a bio-oil are provided. In embodiments, such a method comprises exposing a bio-oil vapor comprising hydrocarbon compounds having oxygenated aromatic groups, to hydrogen gas in the presence of catalyst under conditions to induce deoxygenation of the oxygenated aromatic groups to provide a deoxygenated aromatic species, wherein the catalyst is a transition metal-incorporated mesoporous silicate having platinum deposited thereon and the transition metal is selected from Nb, W, Zr, and combinations thereof. The transition metal-incorporated mesoporous silicate catalysts are also provided.

Provided are: novel zeolite having an extremely small amount of specific Bronsted acid sites on the surface thereof, which is expected to be useful as a catalyst for the aromatization of a non-aromatic hydrocarbon typified by an aliphatic hydrocarbon; and a catalyst for use in the production of an aromatic hydrocarbon, which comprises the zeolite. Zeolite characterized by satisfying the following requirements (i) to (iii). (i) The zeolite has an average particle diameter of 100 nm or less. (ii) The zeolite is 10-membered ring microporous zeolite. (iii) The amount of the Bronsted acid sites on the outer surface of the zeolite is 0.1 to 10.0 μmol/g.

Provided are: novel zeolite having an extremely small amount of specific Bronsted acid sites on the surface thereof, which is expected to be useful as a catalyst for the aromatization of a non-aromatic hydrocarbon typified by an aliphatic hydrocarbon; and a catalyst for use in the production of an aromatic hydrocarbon, which comprises the zeolite. Zeolite characterized by satisfying the following requirements (i) to (iii). (i) The zeolite has an average particle diameter of 100 nm or less. (ii) The zeolite is 10-membered ring microporous zeolite. (iii) The amount of the Bronsted acid sites on the outer surface of the zeolite is 0.1 to 10.0 μmol/g.

Embodiments of catalyst systems and methods of synthesizing catalyst systems are provided. The catalyst system may include a core comprising a zeolite; and a shell comprising a microporous fibrous silica. The shell may be in direct contact with at least a majority of an outer surface of the core. The catalyst system may have a Si/Al molar ratio greater than 5. At least a portion of the shell may have a thickness of from 50 nanometers (nm) to 600 nm.

Embodiments of catalyst systems and methods of synthesizing catalyst systems are provided. The catalyst system may include a core comprising a zeolite; and a shell comprising a microporous fibrous silica. The shell may be in direct contact with at least a majority of an outer surface of the core. The catalyst system may have a Si/Al molar ratio greater than 5. At least a portion of the shell may have a thickness of from 50 nanometers (nm) to 600 nm.

The present invention relates to a catalyst comprising at least one oxide of vanadium, at least one oxide of tungsten, at least one oxide of cerium, at least one oxide of titanium and at least one oxide of niobium, and an exhaust system containing said oxides.

Methods of simultaneously converting butanes and methanol to olefins over Ti-containing zeolite catalysts are described. The exothermicity of the alcohols to olefins reaction is matched by endothermicity of dehydrogenation reaction of butane(s) to light olefins resulting in a thermo-neutral process. The Ti-containing zeolites provide excellent selectivity to light olefins as well as exceptionally high hydrothermal stability. The coupled reaction may advantageously be conducted in a staged reactor with methanol/DME conversion zones alternating with zones for butane(s) dehydrogenation. The resulting light olefins can then be reacted with iso-butane to produce high-octane alkylate. The net result is a highly efficient and low cost method for converting methanol and butanes to alkylate.