A catalytic composite comprises a first component selected from Group VIII noble metal components and mixtures thereof, a second component selected from one or more of alkali and alkaline earth metal components, and a third component selected from one or more of tin, germanium, lead, indium, gallium, and thallium, all supported on an alumina support comprising delta alumina having an X-ray diffraction pattern comprising at least three 2θ diffraction angle peaks between 32.0° and 70.0°. The at least three 2θ diffraction angle peaks comprise a first 2θ diffraction angle peak of 32.7°±0.4°, a second 2θ diffraction angle peak of 50.8°±0.4°, and a third 2θ diffraction angle peak of 66.7°±0.8°, wherein the second 2θ diffraction angle peak has an intensity of less than about 0.06 times the intensity of the third 2θ diffraction angle peak.

Provided herein is an alkane dehydrogenation catalyst, a method of manufacturing an alkane dehydrogenation catalyst, and a method of converting alkanes to alkenes.

Provided herein is an alkane dehydrogenation catalyst, a method of manufacturing an alkane dehydrogenation catalyst, and a method of converting alkanes to alkenes.

A composite media for non-oxidative C2H6 dehydrogenation comprises an aluminosilicate zeolite matrix, and an EDH catalyst on one or more of an external surface of the aluminosilicate zeolite matrix and internal surfaces within pores of the aluminosilicate zeolite matrix. The EDH catalyst comprises one or more of Fe, Zn, Pt, Ga, alloys thereof, and oxides thereof. A C2H6 activation system, and a method of processing a C2H6-containing stream are also described.

Methods of preparing unsaturated compounds or analogs through dehydrogenation of corresponding saturated compounds and/or hydrogenation of aromatic compounds are disclosed.

Methods of preparing unsaturated compounds or analogs through dehydrogenation of corresponding saturated compounds and/or hydrogenation of aromatic compounds are disclosed.

A double-layer structured catalyst for use in dehydrogenation of light hydrocarbon gas within a range of C3 to C6, configured such that platinum, tin, and an alkali metal are carried in a phase-changed carrier, wherein the tin component is present in an entire region inside the carrier, and the platinum and the tin form a single complex and are present in an alloy form within a range of a predetermined thickness from an outer periphery of the carrier.

A double-layer structured catalyst for use in dehydrogenation of light hydrocarbon gas within a range of C3 to C6, configured such that platinum, tin, and an alkali metal are carried in a phase-changed carrier, wherein the tin component is present in an entire region inside the carrier, and the platinum and the tin form a single complex and are present in an alloy form within a range of a predetermined thickness from an outer periphery of the carrier.

Processes for upgrading a hydrocarbon. The process can include (I) contacting a hydrocarbon-containing feed with a catalyst 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 (II) contacting at least a portion of the coked catalyst with an oxidant to effect combustion of at least a portion of the coke to produce a regenerated catalyst. The process can also include (III) contacting an additional quantity of the hydrocarbon-containing feed with at least a portion of the regenerated catalyst. A cycle time from the contacting the hydrocarbon-containing feed with the catalyst in step (I) to the contacting the additional hydrocarbon-containing feed with the regenerated catalyst in step (III) can be ≤5 hours.

Processes for upgrading a hydrocarbon. The process can include (I) contacting a hydrocarbon-containing feed with a catalyst 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 (II) contacting at least a portion of the coked catalyst with an oxidant to effect combustion of at least a portion of the coke to produce a regenerated catalyst. The process can also include (III) contacting an additional quantity of the hydrocarbon-containing feed with at least a portion of the regenerated catalyst. A cycle time from the contacting the hydrocarbon-containing feed with the catalyst in step (I) to the contacting the additional hydrocarbon-containing feed with the regenerated catalyst in step (III) can be ≤5 hours.