The present disclosure provides a modified catalyst, and preparation method and a method for producing aromatic hydrocarbons by aromatization of olefins using the modified catalyst. The modified catalyst comprises an acidic molecular sieve and an olefin aromatization active metal component, the total acid amount of the catalyst as measured by NH3-TPD method is not higher than 0.35mmo1/g, and ratio of the strong acid to weak acid is within a range of 0.8-1.2.

The present invention relates to a catalyst for dehydration of a primary alcohol, a method of preparing the same, and a method of producing an alpha-olefin using the same. The catalyst for dehydration of a primary alcohol according to the present invention has an excellent catalyst stability while having an excellent activity with respect to dehydration, and a high turnover frequency, such that a linear alpha-olefin with high purity may be produced with a high selectivity even in a case where a relatively small amount of a cocatalyst is added as compared with a homogeneous catalyst system.

A hydrogenolysis catalyst comprises a catalytic component that includes copper oxide, manganese oxide, and aluminum oxide, and a binder that includes a zirconium component, wherein the catalyst comprises at least about 30.0 wt % copper oxide, and the catalyst is substantially free of silicon or an oxide thereof. The hydrogenolysis catalysts are effective for converting fatty acid esters to fatty alcohols.

A process for isobutanol synthesis is described. Ethanol and synthesis gas (syngas) are reacted in the presence of a heterogeneous catalyst in a first reaction zone. The products of the first reaction can be separated into one or more streams comprising methanol and propanol. The methanol and propanol from the first reaction are reacted in the presence of a second catalyst to form isobutanol in a second reaction zone.

The present disclosure relates to a process for preparing long-chain alkanes and alkenes from alcohols, aldehydes, or both. The process proceeds via acceptorless dehydrogenation and decarbonylative coupling using a supported catalyst.

According to one or more embodiments described herein, a method for dehydrogenating hydrocarbons may include passing a hydrocarbon feed comprising one or more alkanes or alkyl aromatics into a fluidized bed reactor, contacting the hydrocarbon feed with a dehydrogenation catalyst in the fluidized bed reactor to produce a dehydrogenated product and hydrogen, and contacting the hydrogen with an oxygen-rich oxygen carrier material in the fluidized bed reactor to combust the hydrogen and form an oxygen-diminished oxygen carrier material. In additional embodiments, a dual-purpose material may be utilized which has dehydrogenation catalyst and oxygen carrying functionality.

Processes of making [1.1.1]propellane utilize reaction conditions that include reacting 1,1-dibromo-2,2-bis(chloromethyl)cyclopropane with an effective amount of solid magnesium.

Methods of producing an isomerization catalyst include preparing a catalyst precursor solution, hydrothermally treating the catalyst precursor solution to produce a magnesium oxide precipitant, and calcining the magnesium oxide precipitant to produce the isomerization catalyst. The catalyst precursor solution includes at least a magnesium precursor, a hydrolyzing agent, and cetrimonium bromide. Methods of producing 1-butene from a 2-butene-containing feedstock with the isomerization catalyst are also disclosed.

Processes for upgrading a hydrocarbon. The process can include contacting a hydrocarbon-containing feed with fluidized catalyst particles that can include a Group 8-10 element or a compound thereof disposed on a support to effect one or more of dehydrogenation, dehydroaromatization, and dehydrocyclization of at least a portion of the hydrocarbon-containing feed to produce a coked catalyst and an effluent. The process can also include contacting at least a portion of the coked catalyst particles with an oxidant to effect combustion of at least a portion of the coke to produce regenerated catalyst particles. The process can also include contacting an additional quantity of the hydrocarbon-containing feed with at least a portion of the regenerated catalyst particles to produce additional effluent and re-coked catalyst particles.

A supported catalyst for preparing light olefin using direct conversion of syngas is a composite catalyst and formed by compounding component I and component II in a mechanical mixing mode. The active ingredient of component I is a metal oxide; and the component II is a supported zeolite. A carrier is one or more than one of hierarchical pores Al.sub.2O.sub.3, SiO.sub.2, TiO.sub.2, ZrO.sub.2, CeO.sub.2, MgO and Ga.sub.2O.sub.3; the zeolite is one or more than one of CHA and AEI structures; and the load of the zeolite is 4%-45% wt. A weight ratio of the active ingredients in the component I to the component II is 0.1-20. The reaction process has an extremely high light olefin selectivity; the sum of the selectivity of the light olefin comprising ethylene, propylene and butylene can reach 50-90%, while the selectivity of a methane side product is less than 7%.