This disclosure relates to catalyst compositions including gallium and a zirconium-based mixed oxide support, to methods for making such catalysts, and to methods for dehydrogenating hydrocarbons with such catalysts. For example, in one embodiment, a catalyst composition includes a mixed oxide support comprising at least about 50 wt. % of zirconium oxide, the mixed oxide support being present in the composition in an amount within the range of about 40 wt. % to about 99.9 wt. %; and disposed on the support, gallium, present in the composition in an amount within the range of about 0.1 wt. % to about 30 wt. %, calculated as Ga.sub.2O.sub.3 on a calcined basis.

In an embodiment, A catalyst comprises a zeolite comprising Si, Al, and Ge in the framework with Pt deposited thereon; wherein the catalyst has an Si:Al.sub.2 mole ratio of greater than or equal to 125, an Si:Ge mole ratio of 40 to 400, and an Na:Al mole ratio of 0.9 to 2.5; wherein the catalyst has an aluminum content of less than or equal to 0.75 wt %; wherein the catalyst is non-acidic.

A catalyst for the dehydrogenation of alkanes to alkenes comprises a catalytically active material supported on a carrier, wherein the catalytically active material is a metallic sulfide (MeS) comprising Fe, Co, Ni, Cu, Mo or W or any combination of two or more metals selected from Pb, Sn, Zn, Fe, Co, Ni, Cu, Mo and W. The catalyst is regenerated in several steps. The dehydrogenation is carried out at a temperature between 450 and 650 C. and a pressure from 0.9 bar below ambient pressure to 5 bar above ambient pressure.

In an embodiment, a method for making a catalyst, comprises: forming a mixture comprising a germanium source, an alkali metal source, an aluminum source, and a silica source, wherein the mixture has a pH; adjusting the pH of the mixture to a value of greater than or equal to 9.5; crystallizing and calcining the mixture to form a zeolite; depositing platinum on the zeolite; and calcining the zeolite to form the final catalyst. The final catalyst is non-acidic and has an aluminum content of less than or equal to 0.75 wt % based on the total weight of the final catalyst excluding any binder and extrusion aide and a Si:Al2 mole ratio of greater than or equal to 125.

A catalyst for the dehydrogenation of alkanes to alkenes comprises lead(II) sulfide (PbS) as catalytically active material supported on a carrier. The dehydrogenation is carried out at a temperature between 500 and 650 C. and at a pressure from 0.5 bar below ambient pressure to 5 bar above ambient pressure.

A catalyst for the dehydrogenation of alkanes to alkenes comprises lead(II) sulfide (PbS) as catalytically active material supported on a carrier. The dehydrogenation is carried out at a temperature between 500 and 650 C. and at a pressure from 0.5 bar below ambient pressure to 5 bar above ambient pressure.

According to an embodiment of the present invention, there are provided a catalytic body, a method of manufacturing the same, and a method of preparing 1,3-butadiene using the same. The catalytic body includes an inactive support; an intermediate layer disposed on a surface of the inactive support; and an active layer disposed on a surface of the intermediate layer, wherein the active layer includes catalyst powder and a binder.

Oxidative dehydrogenation is an alternative to the energy extensive steam cracking process presently used for the production of olefins from paraffins, but has not been implemented commercially partially due to the unstable nature of hydrocarbon/oxygen mixtures, and partially due to the cost involved in the construction of new facilities. An oxidative dehydrogenation chemical complex designed to reduce costs by including integration of an oxygen separation module that also addresses safety concerns and reduces emission of greenhouse gases is described.

Processes for regenerating an at least partially deactivated catalyst that can include a Group (10) element, an inorganic support, and a contaminant. The Group (10) element can have a concentration of from 0.06 wt % to 6 wt %, based on the weight of the inorganic support. The process can include (I) heating the deactivated catalyst using a heating gas mixture that includes H.sub.2O at a concentration >5 mol %, based on the total moles in the mixture to produce a precursor catalyst. The process can also include (II) providing an oxidative gas that includes ?5 mol % of H.sub.2O, based on the total moles in the oxidative gas, and (III) contacting the precursor catalyst at an oxidizing temperature with the oxidative gas for a duration of at least 30 seconds to produce an oxidized precursor catalyst. The process can also include (IV) obtaining a regenerated catalyst from the oxidized precursor catalyst.

Processes for regenerating an at least partially deactivated catalyst that can include a Group (10) element, an inorganic support, and a contaminant. The Group (10) element can have a concentration of from 0.06 wt % to 6 wt %, based on the weight of the inorganic support. The process can include (I) heating the deactivated catalyst using a heating gas mixture that includes H.sub.2O at a concentration >5 mol %, based on the total moles in the mixture to produce a precursor catalyst. The process can also include (II) providing an oxidative gas that includes ?5 mol % of H.sub.2O, based on the total moles in the oxidative gas, and (III) contacting the precursor catalyst at an oxidizing temperature with the oxidative gas for a duration of at least 30 seconds to produce an oxidized precursor catalyst. The process can also include (IV) obtaining a regenerated catalyst from the oxidized precursor catalyst.