A catalyst for a selective conversion of hydrocarbons. The catalyst includes a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof. The catalyst is a support formed as a spherical catalyst particle with a median diameter between 1.6 mm and 2.5 mm and an apparent bulk density between 0.6 and 0.3 g/cc. Also a process of using such a catalyst for a selective hydrocarbon conversion reaction and a process for regenerating such a catalyst by removing coke from same.

The present invention relates to a molding comprising a zeolitic material, phosphorous, one or more metals M of groups 3, 6, 10 to 14 of the periodic system of the elements, and a binder material. The molding is useful as a catalyst, in particular for preparing aromatic compounds from methanol with selectivity toward p-xylene.

The present disclosure relates to the technical field of fine chemical engineering, and particularly discloses a stepwise solidus synthesis method for a micro-mesoporous calcium aluminate catalyst, comprising: mixing a calcium oxide-based powder with an alumina-based powder and an adhesion pore-enlarging agent; pelleting and molding the mixture; pyrolyzing and coking the pelleted and molded product in a rotary kiln reactor under the conditions including an outlet reaction temperature of 300 C.500 C. and a residence time of 0.23.5 h; and subsequently carrying out a solidus reaction in an internal heating rotary kiln reactor under the conditions including an outlet reaction temperature of 900 C.1,500 C. and a residence time of 0.15 h to produce calcium aluminate; decomposing and gasifying the pyrolyzed char in the calcium aluminate to promote the formation of pores, thereby producing micro-mesoporous calcium aluminate catalyst; wherein the weight ratio between the calcium oxide-based powder and the alumina-based powder is within a range of 12:(215), the added amount of the adhesion pore-enlarging agent accounts for 0.115% by weight of a total amount of the calcium oxide-based powder and alumina-based powder; wherein the weight of the calcium oxide-based powder is calculated based on calcium oxide, and the weight of the alumina-based powder is calculated based on alumina. The calcium aluminate catalyst prepared with the method provided by the present disclosure has advantages of large specific surface area, low density and high strength.

The invention relates to CuAlMn shaped catalyst bodies in extruded form, and to a process for their preparation. The shaped catalyst body is suitable for the hydrogenation of organic compounds containing a carbonyl function, in particular for the hydrogenation of aldehydes, ketones and carboxylic acids and/or their esters. In particular, the shaped catalyst body is suitable for the hydrogenation of fatty acids or their esters, such as fatty acid methyl esters, to form the corresponding alcohols and dicarboxylic acid anhydrides, such as maleic anhydride, or esters of di-acids and di-alcohols, such as butane diol.

A process for producing unsaturated nitrile, using a fluidized bed reactor having an internal space having a catalyst capable of being fluidized therein, a feed opening to feed a starting material gas comprising hydrocarbon to the internal space, and a discharge port to discharge a reaction product gas from the internal space, the process comprising a reaction step of subjecting the hydrocarbon to a vapor phase catalytic ammoxidation reaction in the presence of the catalyst in the internal space to produce the corresponding unsaturated nitrile, wherein when in the internal space, a space where an existing amount of the catalyst per unit volume is 150 kg/m.sup.3 or more is defined as a dense zone and a space where an existing amount of the catalyst per unit volume is less than 150 kg/m.sup.3 is defined as a sparse zone in the reaction step, a gas residence time in the sparse zone is 5 to 50 sec.

A sorbent composition that is useful for injection into a flue gas stream of a coal burning furnace to efficiently remove mercury from the flue gas stream. The sorbent composition may include a sorbent with an associated ancillary catalyst component that is a catalytic metal, a precursor to a catalytic metal, a catalytic metal compound or a precursor to a catalytic metal compound. Alternatively, a catalytic metal or metal compound, or their precursors, may be admixed with the coal feedstock prior to or during combustion in the furnace, or may be independently injected into a flue gas stream. A catalytic promoter may also be used to enhance the performance of the catalytic metal or metal compound.

Provided is a catalyst system for oxidative dehydrogenation, a reactor for preparing butadiene including the catalyst system, and a method of preparing 1,3-butadiene. In the catalyst system for oxidative dehydrogenation, a coating catalyst is diluted with a specific dilution filler and a reactor is filled with the diluted catalyst, or a reactor is filled with a catalyst for oxidative dehydrogenation so that the concentration of an active ingredient included in the catalyst gradually increases in the direction from reactants inlet in which reactants are fed into the reactor to products outlet. The catalyst system for oxidative dehydrogenation can efficiently control heat generated inside a reactor, thereby improving conversion rate, selectivity, yield, and long-term stability of a catalyst.

A sorbent composition that is useful for injection into a flue gas stream of a coal burning furnace to efficiently remove mercury from the flue gas stream. The sorbent composition may include a sorbent with an associated ancillary catalyst component that is a catalytic metal, a precursor to a catalytic metal, a catalytic metal compound or a precursor to a catalytic metal compound. Alternatively, a catalytic metal or metal compound, or their precursors, may be admixed with the coal feedstock prior to or during combustion in the furnace, or may be independently injected into a flue gas stream. A catalytic promoter may also be used to enhance the performance of the catalytic metal or metal compound.

A catalyst includes a support, where the support includes an external surface, about 60 wt % to about 99 wt % silica, and about 1.0 wt % to about 5.0 wt % alumina. A catalytic layer is disposed within the support adjacent to the external surface, where the catalytic layer further includes Pd, Au, and potassium acetate (KOAc). In the catalyst, (a) the KOAc is from about 60 kg/m.sup.3 to about 150 kg/m.sup.3 of the catalyst; or (b) the catalytic layer has an average thickness from about 50 m to about 150 m; or (c) both (a) and (b). The catalyst also possesses a Brunauer-Emmett-Teller surface area of about 130 m.sup.2/g to about 300 m.sup.2/g and a geometric surface area per packed bed volume from about 550 m.sup.2/m.sup.3 to about 1500 m.sup.2/m.sup.3. The catalyst is highly active for the synthesis of vinyl acetate monomer and exhibits a high selectivity for vinyl acetate monomer.

In one aspect, catalyst modules are described herein comprises structural catalyst bodies having cross-sectional flow channel geometries and surface features for enhanced catalytic activity. In some embodiments, the catalyst modules and associated structural catalyst bodies are suitable for use in high particulate matter environments. Briefly, a catalyst module comprises a framework and a plurality of structural catalyst bodies positioned in the framework, a structural catalyst body comprising an outer peripheral wall and a plurality of inner partition walls forming individual flow channels of rectangular cross-section, the outer peripheral wall resistant to localized flexural failures induced by material between adjacent structural catalyst bodies of the module.