Universal Oil Products Company

Uop Lcc

Other

Frederick C Wilhelm

Dehydrogenatable hydrocarbons are dehydrogenated by contacting them, at dehydrogenation conditions, with a catalytic composite comprising a combination of catalytically effective amounts of a platinum or palladium component, a rhodium component, and a lead component with a porous carrier material. A specific example of the catalytic composite disclosed herein is a combination of a platinum or palladium component, a rhodium component, a lead component, and an alkali or alkaline earth component with a porous carrier material, wherein substantially all of the platinum or palladium component and the rhodium component are present therein as the corresponding elemental metals and substantially all of the lead component and the alkali or alkaline earth component are present therein in an oxidation state above the elemental metal, and wherein the composite contains about 0.01 to about 2 wt. % platinum or palladium, about 0.01 to about 2 wt. % rhodium, about 0.1 to about 5 wt. % alkali metal or alkaline earth metal, and lead in an amount sufficient to result in an atomic ratio of lead to platinum or palladium of about 0.05:1 to about 0.9:1.

Dehydrogenation using multimetallic catalyst

Hydrocarbons are converted by contacting them in a substantially sulfur-free environment at hydrocarbon conversion conditions with an acidic, sulfur-free trimetallic catalytic composite comprising a combination of catalytically effective amounts of a platinum group component, a tin or lead component, a nickel component and a halogen component with a porous carrier material. The platinum group component, tin or lead component, nickel component, and halogen component are present in the trimetallic catalyst in amounts respectively, calculated on an elemental basis, corresponding to about 0.01 to about 2 wt. % platinum group metal, about 0.01 to about 5 wt. % tin or lead, about 0.01 to about 5 wt. % nickel, and about 0.1 to about 3.5 wt. % halogen. Moreover, these metallic components are uniformly dispersed throughout the porous carrier material in carefully controlled oxidation states such that substantially all of the platinum group metal is present therein in the elemental metallic state, the major portion of the nickel component is present in the elemental metallic state, while substantially all of the tin or lead is present therein in an oxidation state above that of the elemental metal. A specific example of the type of hydrocarbon conversion process disclosed is a process for the catalytic reforming of a low-octane gasoline fraction wherein the gasoline fraction and a hydrogen stream are contacted in a substantially sulfur-free environment with the acidic, sulfur-free trimetallic catalyst disclosed herein at reforming conditions.

Hydrocarbon conversion with an acidic, sulfur-free trimetallic catalytic

Hydrocarbons are converted by contacting them at hydrocarbon conversion conditions with an acidic multimetallic catalytic composite comprising a combination of catalytically effective amounts of a platinum or paladium component, a rhodium component, a rhenium component, a lead component, and a halogen component with a porous carrier material. The platinum or paladium component, rhodium component, rhenium component, lead component, and halogen component are present in the multimetallic catalyst in amounts respectively, calculated on an elemental basis, corresponding to about 0.01 to about 2 wt. % platinum or palladium metal, about 0.01 to about 2 wt. % rhodium, about 0.01 to about 2 wt. % rhenium, about 0.1 to about 3.5 wt. % halogen, and an atomic ratio of lead to platinum or palladium of about 0.05:1 to about 0.9:1. Moreover, these metallic components are uniformly dispersed throughout the porous carrier material in carefully controlled oxidation states such that substantially all of the platinum or palladium component is present therein in the elemental metallic state, substantially all of the rhenium and rhodium components are present therein in the elemental metallic state or in a state which is reducible to the elemental metallic state under hydrocarbon conversion conditions or in a mixture of these states and substantially all of the lead component is present in an oxidation state above that of the elemental metal. A specific example of the type of hydrocarbon conversion process disclosed is a process for the catalytic reforming of a low-octane gasoline fraction wherein the gasoline fraction and a hydrogen stream are contacted with the acidic multimetallic catalyst disclosed herein at reforming conditions.

Hydrocarbon conversion with an acidic multi-metallic catalytic composite

A dehydrogenatable hydrocarbon is dehydrogenated by contacting the hydrocarbon, hydrogen, and water or a water-producing substance, at dehydrogenation conditions, with a nonacidic catalytic composite comprising a combination of catalytically effective amounts of a platinum group metal component, a nickel component, a Group IVA metallic component, and an alkali or alkaline earth component with a porous carrier material. A specific example of the nonacidic, multimetallic catalytic composite disclosed herein is a combination of a platinum metal component, a nickel component, a germanium component, and an alkali or alkaline earth component with an alumina carrier material. The amounts of the catalytically active components contained in this last composite are, on an elemental basis, 0.01 to 2 wt. % platinum, 0.01 to 5 wt. % nickel, 0.01 to 5 wt. % germanium, and 0.1 to 5 wt % of the alkali or alkaline earth metal.

Nonacidic multimetallic dehydrogenation catalyst

Hydrocarbons are converted by contacting them at hydrocarbon conversion conditions with a sulfided acidic multimetallic catalytic composite comprising a combination of catalytically effective amounts of a platinum or palladium component, a rhodium component, a component with a porous carrier material. The platinum or palladium component, rhodium component, lead component, halogen component, and sulfur component are present in the multimetallic catalyst in amounts respectively, calculated on an elemental basis, corresponding to about 0.01 to about 2 wt. % platinum or palladium metal, about 0.01 to about 2 wt. % rhodium, an atomic ratio of lead to platinum or palladium of about 0.05:1 to about 0.9:1, about 0.1 to about 3.5 wt. % halogen, and about 0.01 to about 1 wt. % sulfur. Moreover, the metallic components are uniformly dispersed throughout the porous carrier material in carefully controlled oxidation states such that substantially all of the platinum or palladium component and the rhodium component are present therein in a sulfided state or in a mixture of the sulfided state and the elemental metallic state and such that substantially all of the lead component is present therein in an oxidation state above the elemental metal. The sulfiding of the catalytic composite is performed prior to any contact of the composite with hydrocarbon and after substantially all of the platinum or palladium and rhodium components are reduced to the elemental metallic state by treatment with a sulfiding gas at conditions selected to incorporate about 0.01 to about 1 wt. % sulfur. The resulting sulfided acidic catalyst has the capability of diminishing undesired demethylation and other hydrogenolysis reactions during initial operation of the process and markedly increasing the over-all stability of the process.

Hydrocarbon conversion with a sulfided acidic multimetallic catalytic

Dehydrogenatable hydrocarbons are dehydrogenated by contacting them, under dehydrogenation conditions, with a dehydrogenation catalyst comprising a combination of a catalytically effective amount of an alkali or alkaline earth component with a catalytic composite consisting essentially of a tin component in combination with a platinum component on a carrier material, wherein the catalytic composite is prepared by the method which comprises: (a) impregnating a high surface area porous carrier material with a solution of a complex chlorostannate (II) chloroplatinate anionic species, the solution being stabilized in contact with the carrier material with an aqueous halogen acid; and thereafter, (b) drying and calcining the impregnated carrier material. For the dehydrogenation of normal paraffin hydrocarbons, this dehydrogenation catalyst preferably contains, on an elemental basis, about 0.01 to about 2 wt. % platinum, about 0.01 to about 5 wt. % tin, and about 0.01 to about 5 wt. % alkali or alkaline earth metal.

Dehydrogenation of hydrocarbons with a multimetallic catalytic composite

A dehydrogenatable hydrocarbon is dehydrogenated by contacting the hydrocarbon, hydrogen, and water or a water-producing substance, at dehydrogenation conditions, with a nonacidic catalytic composite comprising a combination of catalytically effective amounts of a platinum group metal component, a nickel component, a Group IVA metallic component, and an alkali or alkaline earth component with a porous carrier material. A specific example of the nonacidic, multimetallic catalytic composite disclosed herein is a combination of a platinum metal component, a nickel component, a germanium component, and an alkali or alkaline earth component with an alumina carrier material. The amounts of the catalytically active components contained in this last composite are, on an elemental basis, 0.01 to 2 wt. % platinum, 0.01 to 5 wt. % nickel, 0.01 to 5 wt. % germanium, and 0.1 to 5 wt. % of the alkali or alkaline earth metal.

Dehydrogenation with a nonacidic multimetallic catalyst

Hydrocarbons are converted by contacting them at hydrocarbon conversion conditions with a bimetallic acidic catalytic composite comprising a combination of catalytically effective amounts of a platinum group component, an indium component and a halogen component with a porous carrier material. The platinum group component and halogen component are present in the bimetallic catalyst in amounts respectively, calculated on an elemental basis, corresponding to about 0.01 to about 2 wt. % platinum group metal and about 0.1 to about 3.5 wt. % halogen. The indium component is present in amounts corresponding to an atomic ratio of indium to platinum group metal of about 0.1:1 to about 1:1. Moreover, the platinum group and indium components are uniformly dispersed throughout the porous carrier material in carefully controlled oxidation states such that substantially all of the platinum group component is present therein in the corresponding elemental metallic state while substantially all of the indium component is present therein in an oxidation state above that of the corresponding metal. A specific example of the type of hydrocarbon conversion process disclosed is a process for the catalytic reforming of a low-octane gasoline fraction wherein the gasoline fraction and hydrogen stream are contacted with the novel acidic bimetallic catalyst disclosed herein at reforming conditions. Also disclosed is a novel trimetallic catalyst comprising a combination of a Group IVA metallic component with the acidic bimetallic catalyst.

Hydrocarbon conversion catalyst

Hydrocarbons are converted by contacting them at hydrocarbon conversion conditions with a trimetallic acidic catalytic composite comprising a combination of catalytically effective amounts of a platinum or palladium component, a rhodium component, a bismuth component, and a halogen component with a porous carrier material. The platinum or palladium component, rhodium component, and halogen component are present in the trimetallic catalyst in amounts respectively, calculated on an elemental basis, corresponding to about 0.01 to about 2 wt. % platinum or palladium, about 0.01 to about 2 wt. % rhodium, and about 0.1 to about 3.5 wt. % halogen. The bismuth component is present in amounts corresponding to an atomic ratio of bismuth to platinum or palladium of about 0.1:1 to about 1:1. Moreover, these metallic components are uniformly dispersed throughout the porous carrier material in carefully controlled oxidation states such that substantially all of the platinum or palladium, rhodium, and bismuth components are present therein in the corresponding elemental metallic states. A specific example of the type of hydrocarbon conversion process disclosed is a process for the catalytic reforming of a low-octane gasoline fraction wherein the gasoline fraction and hydrogen stream are contacted with the acidic trimetallic catalyst disclosed herein at reforming conditions.

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Ann Arbor, MI, United States of America

Frederick C Wilhelm