A catalyst for dehydrogenation of hydrocarbons includes a support including zirconium oxide and Linde type L zeolite (L-zeolite). A concentration of the zirconium oxide in the catalyst is in a range of from 0.1 weight percent (wt. %) to 20 wt. %. The catalyst includes from 5 wt. % to 15 wt. % of an alkali metal or alkaline earth metal. The catalyst includes from 0.1 wt. % to 10 wt. % of tin. The catalyst includes from 0.1 wt. % to 8 wt. % of a platinum group metal. The alkali metal or alkaline earth metal, tin, and platinum group metal are disposed on the support.

A catalyst for dehydrogenation of hydrocarbons includes a support including zirconium oxide and Linde type L zeolite (L-zeolite). A concentration of the zirconium oxide in the catalyst is in a range of from 0.1 weight percent (wt. %) to 20 wt. %. The catalyst includes from 5 wt. % to 15 wt. % of an alkali metal or alkaline earth metal. The catalyst includes from 0.1 wt. % to 10 wt. % of tin. The catalyst includes from 0.1 wt. % to 8 wt. % of a platinum group metal. The alkali metal or alkaline earth metal, tin, and platinum group metal are disposed on the support.

Methods of converting isobutylene to C5+ compounds. The methods may include contacting isobutylene with a skeletal isomerization catalyst to provide a mixture of C.sub.4 olefins, and then contacting the mixture of C.sub.4 olefins with a metathesis catalyst to convert the mixture of C.sub.4 olefins to a product mixture. The product mixture may include C.sub.5+ olefins.

Methods of converting isobutylene to C5+ compounds. The methods may include contacting isobutylene with a skeletal isomerization catalyst to provide a mixture of C.sub.4 olefins, and then contacting the mixture of C.sub.4 olefins with a metathesis catalyst to convert the mixture of C.sub.4 olefins to a product mixture. The product mixture may include C.sub.5+ olefins.

A process for the dehydrogenation of alkyl-containing compounds comprises reacting an alkyl-containing compound and a Group VI nitrosyl complex characterized as a transition metal complex having the composition Cp′M(NO)(R1)(R2), wherein Cp′ is selected from certain substituted and unsubstituted η.sup.5-cyclopentadienyl groups; M is W or Mo; and R1 and R2 are independently selected from CH.sub.2C(CH.sub.3).sub.3; CH.sub.2Si(CH.sub.3).sub.3; CH.sub.2(C.sub.6H.sub.5); CH.sub.3; hydrogen; and η.sup.3-allyl; provided that if R1 is hydrogen, R2 is η.sup.3-allyl; under conditions such that the alkyl-containing compound is converted to an olefin, and in particular embodiments, a terminal olefin. The dehydrogenation can be carried out using a neat and/or undried alkyl-containing compound and/or may be conducted under air, and does not require a sacrificial olefin to drive the reaction, thereby increasing convenience and decreasing cost in comparison with some other dehydrogenation processes.

A process for the dehydrogenation of alkyl-containing compounds comprises reacting an alkyl-containing compound and a Group VI nitrosyl complex characterized as a transition metal complex having the composition Cp′M(NO)(R1)(R2), wherein Cp′ is selected from certain substituted and unsubstituted η.sup.5-cyclopentadienyl groups; M is W or Mo; and R1 and R2 are independently selected from CH.sub.2C(CH.sub.3).sub.3; CH.sub.2Si(CH.sub.3).sub.3; CH.sub.2(C.sub.6H.sub.5); CH.sub.3; hydrogen; and η.sup.3-allyl; provided that if R1 is hydrogen, R2 is η.sup.3-allyl; under conditions such that the alkyl-containing compound is converted to an olefin, and in particular embodiments, a terminal olefin. The dehydrogenation can be carried out using a neat and/or undried alkyl-containing compound and/or may be conducted under air, and does not require a sacrificial olefin to drive the reaction, thereby increasing convenience and decreasing cost in comparison with some other dehydrogenation processes.

A process for preparing a catalyst comprising an active phase based on nickel and an alumina support, which process comprises the following steps: a) said support is impregnated with a volume V1 of a butanol solution of between 0.2 and 0.8 times the total pore volume TPV of said support in order to obtain an impregnated support; b) the impregnated support obtained at the end of step a) is left to mature for 0.5 to 40 hours; c) the matured impregnated support obtained at the end of step b) is impregnated with a solution comprising at least one precursor of the nickel active phase in order to obtain a catalyst precursor; d) the catalyst precursor obtained at the end of step c) is dried at a temperature below 250° C.

A process for preparing a catalyst comprising an active phase based on nickel and an alumina support, which process comprises the following steps: a) said support is impregnated with a volume V1 of a butanol solution of between 0.2 and 0.8 times the total pore volume TPV of said support in order to obtain an impregnated support; b) the impregnated support obtained at the end of step a) is left to mature for 0.5 to 40 hours; c) the matured impregnated support obtained at the end of step b) is impregnated with a solution comprising at least one precursor of the nickel active phase in order to obtain a catalyst precursor; d) the catalyst precursor obtained at the end of step c) is dried at a temperature below 250° C.

Increase propane dehydrogenation activity of a partially deactivated dehydrogenation catalyst by heating the partially deactivated catalyst to a temperature of at least 660° C., conditioning the heated catalyst in an oxygen-containing atmosphere and, optionally, stripping molecular oxygen from the conditioned catalyst.

Increase propane dehydrogenation activity of a partially deactivated dehydrogenation catalyst by heating the partially deactivated catalyst to a temperature of at least 660° C., conditioning the heated catalyst in an oxygen-containing atmosphere and, optionally, stripping molecular oxygen from the conditioned catalyst.