Catalyst and hydrocarbon conversion process

Claim 2

A process for the catalytic reforming of a hydrocarbon feed, said feed comprising a hydrocarbon stream boiling in the range of about 70° F. to about 500° F., which process comprises contacting a catalyst consisting of from about 0.1 to about 2 weight percent rhenium and from about 0.1 to about 2 weight percent gallium supported on a solid porous refractory inorganic oxide support, with said hydrocarbon feed and hydrogen, at a pressure of about 50 psig to about 1,000 psig, a weight hourly space velocity of about 0.5 to about 10 weight units of hydrocarbon per hour per weight unit of catalyst, a hydrogen addition rate of about 1,500 to about 15,000 standard cubic feet per barrel of feed and at an average catalyst temperature of about 850° F. to about 1,050° F.

Claim 3

The process of claim 1 wherein the pressure is about 50 psig to about 450 psig, the weight hourly space velocity is about 0.9 to about 4 weight units of hydrocarbon per hour per weight unit of catalyst, the hydrogen addition rate is about 4,000 to about 10,000 standard cubic feet per barrel of feed and the average catalyst temperature is about 875° F. to about 1,000° F.

Claim 4

The process of claim 1 wherein the preparation of said catalyst comprises impregnating the solid support with soluble compounds of rhenium and gallium followed by drying and calcining.

Claim 5

The process of claim 1 wherein the refractory inorganic oxide is a halogen-free inorganic oxide.

Claim 6

The process of claim 1 wherein the rhenium and gallium are characterized as metal, oxide, sulfide, or mixtures thereof.

Claim 7

The process of claim 1 wherein said catalyst consists essentially of from about 0.2 to about 0.8 weight percent rhenium and from about 0.2 to about 0.8 weight percent gallium.

Claim 8

The process of claim 1 wherein the refractory inorganic oxide of the second catalyst is a halogen-free inorganic oxide.

Claim 9

The process of claim 1 wherein the porous refractory inorganic oxide comprises catalytically active alumina, silica-alumina, silicamagnesia, titania-alumina or zinc-oxide-alumina.

Claim 10

The process of claim 8 wherein the porous refractory inorganic oxide comprises gamma alumina.

Claim 11

The process of claim 9 comprising about 0.5 weight percent rhenium and about 0.5 weight percent gallium supported on gamma alumina.

Claim 12

The process of claim 1 wherein the solid support comprises mordenite and a porous refractory inorganic oxide, said mordenite having a silica-to-alumina ratio within the range of about 6 to about 100.

Claim 13

The process of claim 11 wherein preparation of said catalyst support comprises blending finely-divided mordenite-type aluminosilicate material into a sol or gel of said refractory inorganic oxide to form a blend, gelling said blend by adding a solution of a suitable inorganic ammonium-affording compound, and drying and calcining the gel to form a calcined material.

Claim 14

The process of claim 12 wherein said refractory inorganic oxide is a catalytically active alumina and said mordenite is suspended in and distributed throughout a matrix of said alumina, said mordenite being present in an amount of about 1 weight percent to about 50 weight percent, based on the weight of said support.

Claim 15

A process for the catalytic reforming of a hydrocarbon feed, said feed comprising a hydrocarbon stream boiling in the range of about 70° F. to about 500° F., which process comprises contacting a first catalyst comprising platinum on a solid inorganic oxide support of gamma alumina with the hydrocarbon feed and hydrogen to achieve partial catalytic conversion, followed by contacting a second catalyst consisting of from about 0.1 to about 2 weight percent rhenium and from about 0.1 to about 2 weight percent gallium supported on a solid porous refractory inorganic oxide support, with the partially converted hydrocarbon feed and hydrogen, the contacting of both catalysts being conducted at a pressure of about 50 psig to about 1,000 psig, a weight hourly space velocity of about 0.5 to about 10 weight units of hydrocarbon per hour per weight unit of catalyst, a hydrogen addition rate of about 1,500 to about 15,000 standard cubic feet per barrel of feed and at an average catalyst temperature of about 850° F. to about 1,050° F.

Claim 16

A process for the catalytic reforming of a hydrocarbon feed, said feed comprising a hydrocarbon stream boiling in the range of about 70° F. to about 500° F., which process comprises contacting a first catalyst comprising platinum on a solid inorganic oxide support of gamma alumina with the hydrocarbon feed and hydrogen to achieve partial catalytic conversion, followed by contacting a second catalyst consisting of from about 0.1 to about 2 weight percent rhenium and from about 0.1 to about 2 weight percent gallium supported on a solid porous refractory inorganic oxide support, with the partially converted hydrocarbon feed and hydrogen, the contacting of both catalysts being conducted at a pressure of about 50 psig to about 1,000 psig, a weight hourly space velocity of about 0.5 to about 10 weight units of hydrocarbon per hour per weight unit of catalyst, a hydrogen addition rate of about 1,500 to about 15,000 standard cubic feet per barrel of feed and at an average catalyst temperature of about 850° F. to about 1,050° F.

Claim 17

The process of claim 14 wherein the rhenium and gallium of the second catalyst are characterized as metal, oxide, sulfide, or mixtures thereof.

Claim 18

The process of claim 14 wherein the pressure is about 50 psig to about 450 psig, the weight hourly space velocity is about 0.9 to about 4 weight units of hydrocarbon per hour per weight unit of catalyst, the hydrogen addition rate is about 4,000 to about 10,000 standard cubic feet per barrel of feed and the average catalyst temperature is about 875° F. to about 1,000° F.

Claim 19

The process of claim 14 wherein the first catalyst is promoted by an effective amount of rhenium.

Claim 20

The process of claim 14 wherein said second catalyst consists essentially of from about 0.2 to about 0.8 weight percent rhenium and from about 0.2 to about 0.8 weight percent gallium.

Claim 21

The process of claim 14 wherein preparation of said second catalyst comprises impregnating the solid support with soluble compounds of rhenium and gallium followed by drying and calcining.

Claim 22

The process of claim 14 wherein the porous refractory inorganic oxide comprises catalytically active alumina, silica-alumina, silicamagnesia, titania-alumina or zinc-oxide-alumina.

Claim 23

The process of claim 20 wherein the porous refractory inorganic oxide comprises gamma alumina.

Claim 24

The process of claim 21 wherein the second catalyst comprises about 0.5 weight percent rhenium and about 0.5 weight percent gallium supported on gamma alumina.

Claim 25

The process of claim 14 wherein the solid support of the second catalyst comprises mordenite and a porous refractory inorganic oxide, said mordenite having a silica-to-alumina ratio within the range of about 6 to about 100.

Claim 26

The process of claim 23 wherein preparation of said second catalyst support comprises blending finely-divided mordenite-type aluminosilicate material into a sol or gel of said refractory inorganic oxide to form a blend, gelling said blend by adding a solution of a suitable inorganic ammonium-affording compound, and drying and calcining the gel to form a calcined material.

Claim 27

The process of claim 24 wherein said refractory inorganic oxide is a catalytically active alumina and said mordenite is suspended in and distributed throughout a matrix of said alumina, said mordenite being present in an amount of about 1 weight percent to about 50 weight percent, based on the weight of said support.