Plural stage reforming with catalysts having a skewed distribution of a platinum-group metal and rhenium

Claim 2

In a method for reforming a naphthene and paraffin-containing hydrocarbon feed boiling in the gasoline or naphtha range in the presence of molecular hydrogen wherein a series of zones are employed to provide reformates of at least about 90 RON and wherein there are hydrogen-containing recycled gas and at least one reactivation, the improvement which comprises providing at least one naphthene dehydrogenation zone in an early portion of said series of reaction zones, said naphthene dehydrogenation zone having a first catalyst comprising a catalytically effective amount of a supported platinum-group metal and rhenium and providing at least one paraffin dehydrocyclization zone in a later portion of said series of reaction zones, said paraffin dehydrocyclization zone having a second catalyst comprising a catalytically effective amount of a supported platinum-group metal and rhenium wherein the ratio of the percent by weight of the supported platinum-group metal in the first catalyst to that in the second catalyst is in the range of about 1.5 to about 10, introducing a hydrocarbon boiling in the gasoline or naphtha range into such naphthene dehydrogenation zone at an inlet temperature of at least about 820° F., passing effluent from said naphthene dehydrogenation zone serially through the reaction zone wherein the inlet temperature of a paraffin dehydrocyclization zone is in the range of about 900° to 1000° F. and controlled to provide a reformate at least about 90 RON.

Claim 3

In a method for reforming a naphthene and paraffin-containing hydrocarbon feed boiling in the gasoline or naphtha range in the presence of molecular hydrogen wherein a series of zones are employed to provide reformates of at least about 90 RON and wherein there are hydrogen-containing recycled gas and at least one reactivation, the improvement which comprises providing at least one naphthene dehydrogenation zone in an early portion of said series of reaction zones, said naphthene dehydrogenation zone having a first catalyst comprising a catalytically effective amount of a supported platinum-group metal and rhenium and providing at least one paraffin dehydrocyclization zone in a later portion of said series of reaction zones, said paraffin dehydrocyclization zone having a second catalyst comprising a catalytically effective amount of a supported platinum-group metal and rhenium wherein the ratio of the percent by weight of the supported platinum-group metal in the first catalyst to that in the second catalyst is in the range of about 1.5 to about 10, introducing a hydrocarbon boiling in the gasoline or naphtha range into such naphthene dehydrogenation zone at an inlet temperature of at least about 820° F., passing effluent from said naphthene dehydrogenation zone serially through the reaction zone wherein the inlet temperature of a paraffin dehydrocyclization zone is in the range of about 900° to 1000° F. and controlled to provide a reformate at least about 90 RON and wherein there is present during said at least one reactivation a potentially deleterious amount of SO 2 .

Claim 4

In a method for reforming a naphthene and paraffin-containing hydrocarbon feed boiling in the gasoline or naphtha range in the presence of molecular hydrogen wherein a series of zones are employed to provide reformates of at least about 90 RON and wherein there are hydrogen-containing recycled gas and at least one reactivation, the improvement which comprises providing at least one naphthene dehydrogenation zone in an early portion of said series of reaction zones, said naphthene dehydrogenation zone having a first catalyst comprising a catalytically effective amount of a supported platinum-group metal and rhenium and providing at least one paraffin dehydrocyclization zone in a later portion of said series of reaction zones, said paraffin dehydrocyclization zone having a second catalyst comprising a catalytically effective amount of a supported platinum-group metal and rhenium wherein the ratio of the percent by weight of the supported platinum-group metal in the first catalyst to that in the second catalyst is in the range of about 1.5 to about 10, introducing a hydrocarbon boiling in the gasoline or naphtha range into such naphthene dehydrogenation zone at an inlet temperature of at least about 820° F., passing effluent from said naphthene dehydrogenation zone serially through the reaction zone wherein the inlet temperature of a paraffin dehydrocyclization zone is in the range of about 900° to 1000° F. and controlled to provide a reformate at least about 90 RON and wherein there is present during said at least one reactivation a potentially deleterious amount of SO 2 .

Claim 5

The improved process of claim 2, wherein said potentially deleterious amount of SO 2 causes an increase in sulfur content of some catalyst by at least about 0.5% by weight.

Claim 7

The improved process of claim 1, or 2 wherein the first catalyst contains less than about 10 percent by weight of supported rhenium.

Claim 8

The improved process of claim 1, or 2 wherein the ratio of the percent by weight of supported platinum-group metal to that of rhenium in the first catalyst is greater than about 1.5 and that ratio in the second catalyst is less than about 1.

Claim 9

The improved process of claims 1, or 2, wherein the platinum-group metal is platinum.

Claim 10

The improved process of claim 7, wherein the first and second catalyst comprise activated alumina as the base for the supported platinum-group metal and supported rhenium.

Claim 11

The improved method of claim 8, wherein there is provided in said paraffin dehydrocyclization zone a vaporous chlorine-containing agent in an amount to supply about 0.1 to 100 ppm chlorine based on the weight of said hydrocarbon feed, while providing said paraffin dehydrocyclization zone about 10 to 1000 ppm H 2 O based on the weight of hydrocarbon boiling in the gasoline range which is charged to said zone.

Claim 12

The improved process of claim 7, wherein the inlet temperature of the naphthene dehydrogenation zone is in the range of about 840° to 920° F.

Claim 13

The improved method of claim 10, wherein the mole ratio of recycled gas to hydrocarbon in the naphthene dehydrogenation zone is in the range of about 1:1 to about 6:1 and the mole ratio of the recycled gas to hydrocarbon in the paraffin dehydrocyclization zone is about 8:1 to 20:1.

Claim 14

The improved method of claim 1, wherein the sulfur content of the total hydrocarbon feed and recycled gas passing to said naphthene dehydrogenation zone is less than about 10 ppm.

Claim 15

The improved method of claim 12, wherein the impurity levels of both the hydrocarbon feed and recycled gas are below about 10 ppm water, 5 ppm sulfur, and 2 ppm combined nitrogen.