A process for isomerizing an aromatic cut containing at least one aromatic compound containing eight carbon atoms per molecule is described, comprising bringing said cut into contact with at least one catalyst comprising at least one metal from group VIII of the periodic classification of the elements, at least one zeolitic support comprising a zeolite selected from zeolites with structure type EUO and MOR, used alone or as a mixture, and at least one matrix, such that the specific surface area of the matrix in the zeolitic support of said catalyst is in the range 5 to 200 m.sup.2/g.

The present invention relates to the field of isobutylene preparation. Disclosed are a catalyst and preparation method thereof, and method for preparing isobutylene by applying the same; the catalyst has a core-shell structure, the core an amorphous silica-alumina particle and/or an aggregate molding thereof, and the shell aluminum oxide comprising silicon and tin; the weight ratio of aluminum oxide comprising silicon and tin to amorphous silica-alumina is 1:60-1:3; in the aluminum oxide comprising silicon and tin, on basis of the weight of aluminum oxide comprising silicon and tin, the content of silicon is 0.5-2 wt %, and of tin is 0.2-1 wt %. The catalyst of the present invention is used to catalyze a mixture of MTBE and TBA to prepare isobutylene, enabling the MTBE cleavage reaction and TBA dehydration reactions to be conducted simultaneously to generate isobutylene, achieving higher conversion rates of TBA and MTBE, and higher selectivity for generating isobutylene.

The invention relates to an oligomerization catalyst comprising nickel oxide and silica-alumina support material and to a process for oligomerization of C3- to C6-olefins using the oligomerization catalyst.

Oligomerization of C.sub.3- to C.sub.5-olefins using a catalyst is inhibited, wherein the oligomerization is carried out in at least one reaction stage including at least one reactor and at least one distillation column, and wherein the oligomer content in the feed stream to the at least one reactor of the at least one reaction stage is at least 1% by weight.

A heterogeneous catalyst suitable for use in alkane dehydrogenation has an active layer that includes alumina and gallia. The active layer is dispersed on a support such as alumina or silica-modified alumina.

Embodiments of processes and multiple-stage catalyst systems for producing propylene comprising introducing a hydrocarbon stream comprising 2-butene to an isomerization catalyst zone to isomerize the 2-butene to 1-butene, passing the 2-butene and 1-butene to a metathesis catalyst zone to cross-metathesize the 2-butene and 1-butene into a metathesis product stream comprising propylene and C.sub.4-C.sub.6 olefins, and cracking the metathesis product stream in a catalyst cracking zone to produce propylene. The isomerization catalyst zone comprises a silica-alumina catalyst with a ratio by weight of alumina to silica from 1:99 to 20:80. The metathesis catalyst comprises a mesoporous silica catalyst support impregnated with metal oxide. The catalyst cracking zone comprises a mordenite framework inverted (MFI) structured silica catalyst.

A system and a method for isomerizing a 2-butene feed stream to form a 1-butene product stream are provided. An exemplary method includes calcining the red mud, flowing a butene feedstock over the red mud in an isomerization reactor, and separating 1-butene from a reactor effluent.

An improved catalytic dehydrogenation process which process comprises contacting an alkane or alkyl aromatic feedstream with a dehydrogenation catalyst under catalytic conditions in an up-flow fluidized reactor, wherein the fluidized reactor comprises one or more reactors, which catalytic conditions include a temperature within a range of from 500 to 800° C., a weight hourly space velocity within a range of from 0.1 to 1000, a gas residence time within a range of from 0.1 to 10 seconds, and, subsequent to the fluidized reactor, effecting separation of entrained catalyst from reactor effluent by use of a cyclonic separation system, wherein the improvement comprises interposing a cooling means between an up-flow fluidized reactor and the cyclonic separation system to substantially halt thermal reactions, thereby effectively increasing overall molar selectivity to alkene product is provided.

This invention relates to process for producing biphenyl esters, the process comprising: (a) contacting a feed comprising toluene, xylene or mixtures thereof with hydrogen in the presence of a hydroalkylation catalyst to produce a hydroalkylation reaction product comprising (methylcyclohexyl)toluene, wherein the hydroalkylation catalyst comprises: 1) binder present at 40 wt % or less (based upon weight of final catalyst composition), 2) a hydrogenation component present at 0.2 wt % or less (based upon weight of final catalyst composition), and 3) an acidic component comprising a molecular sieve having a twelve membered (or larger) ring pore opening, channel or pocket and a largest pore dimension of 6.0 angstroms or more present at 60 wt % or more, (based upon weight of final catalyst composition); (b) dehydrogenating the hydroalkylation reaction product using a dehydrogenation catalyst to produce a dehydrogenation reaction product comprising a mixture of methyl-substituted biphenyl compounds; (c) contacting at the dehydrogenation reaction product with an oxidizing gas to convert the methyl-substituted biphenyl compounds to biphenyl carboxylic acids; and (d) reacting the biphenyl carboxylic acids with one or more C.sub.1 to C.sub.14 alcohols to produce biphenyl esters.

Systems, processes, and catalysts are disclosed for obtaining fuels and fuel blends containing selected ratios of open-chain and closed-chain fuel-range hydrocarbons suitable for production of alternate fuels including gasolines, jet fuels, and diesel fuels. Fuel-range hydrocarbons may be derived from ethylene-containing feedstocks and ethanol-containing feedstocks.