Catalytic cracking with reduced emission of noxious gases

Claim 2

In a process for the cyclic, fluidized catalytic cracking of a hydrocarbon feedstock containing organic sulfur compounds wherein: (i) said feedstock is subjected to cracking in a reaction zone through contact with a particulate cracking catalyst at a temperature in the range from about 850° to 1,200° F.; (ii) cracking catalyst, which is deactivated by sulfur-containing coke deposits, is separated from reaction zone effluent and passes to a stripping zone wherein volatile deposits are removed from said catalyst by contact with a stripping gas comprising steam at a temperature in the range from about 850° to about 1,200° F.; (iii) stripped catalyst is separated from stripping zone effluent and passes to a catalyst regeneration zone and non-stripped, sulfur-containing coke deposits are removed from the stripped catalyst by burning with an oxygen containing regeneration gas at a temperature in the range from about 1,050° to about 1,450° F., thereby forming sulfur oxides; and (iv) resulting catalyst is separated from regeneration zone effluent gas and recycled to the reaction zone; a method for reducing emissions of sulfur oxides in the regeneration zone effluent gas which comprises: (a) absorbing sulfur oxides in said regeneration zone with a fluidizable particulate solid other than said cracking catalyst, wherein said particulate solid is physically admixed with said cracking catalyst and comprises at least one free or combined first metal selected from the group consisting of the rare earth metals, at least one free or combined second metal selected from the group consisting of ruthenium, rhodium, palladium, osmium, iridium, platinum and rhenium, and at least one inorganic oxide selected from the group consisting of silica and alumina, and (b) removing said absorbed sulfur oxides from the particulate solid as a sulfur-containing gas by contacting said particulate solid with the hydrocarbon feedstock in said reaction zone and with steam in said stripping zone while physically admixed with the cracking catalyst.

Claim 3

The process as set forth in claim 1 wherein said cracking catalyst comprises a crystalline aluminosilicate.

Claim 4

The process as set forth in claim 2 wherein said stripping gas provides an amount of steam such that the ratio by weight of steam to said particles of cracking catalyst being supplied to the stripping zone is from about 0.005 to about 0.025.

Claim 5

The process as set forth in claim 3 wherein the amount of said first metal, calculated as the metal, is from about 0.2 to about 10 weight percent with respect to said admixture of cracking catalyst and particulate solid other than cracking catalyst.

Claim 6

The process as set forth in claim 4 wherein the amount of said second metal, calculated as the metal, is from about 0.1 part per million to about 10 parts per million with respect to said admixture of cracking catalyst and particulate solid other than cracking catalyst.

Claim 7

The process as set forth in claim 5 wherein said free or combined second metal is selected from the group consisting of platinum and palladium.

Claim 8

The process as set forth in claim 6 wherein said inorganic oxide comprises alumina.

Claim 9

The process as set forth in claim 7 wherein said free or combined first metal comprises cerium.

Claim 10

The process as set forth in claim 8 wherein said inorganic oxide comprises a major portion of the particulate solid other than said cracking catalyst.

Claim 11

In a process for the cyclic, fluidized catalytic cracking of a hydrocarbon feedstock containing organic sulfur compounds wherein: (i) said feedstock is subjected to cracking in a reaction zone through contact with a particulate cracking catalyst at a temperature in the range from about 850° to 1,200° F.; (ii) cracking catalyst, which is deactivated by sulfur-containing coke deposits, is separated from reaction zone effluent and passes to a stripping zone wherein volatile deposits are removed from said catalyst by contact with a stripping gas comprising steam at a temperature in the range from about 850° to about 1,200° F.; (iii) stripped catalyst is separated from stripping zone effluent and passes to a catalyst regeneration zone and non-stripped, sulfur-containing coke deposits are removed from the stripped catalyst by burning with an oxygen containing regeneration gas at a temperature in the range from about 1,050° to about 1,450° F., thereby forming sulfur oxides; and (iv) resulting catalyst is separated from regeneration zone effluent gas and recycled to the reaction zone; a method for reducing emissions of sulfur oxides in the regeneration zone effluent gas which comprises: (a) circulating fluidizable particulate solids through the cyclic catalytic cracking process which are physically admixed with said particulate cracking catalyst and comprise: (i) a first particulate solid other than said particulate cracking catalyst comprising at least one free or combined first metal selected from the group consisting of the rare earth metals in association with at least one inorganic oxide selected from the group consisting of silica and alumina and (ii) a second particulate solid other than said particulate cracking catalyst comprising at least one free or combined second metal selected from the group consisting of ruthenium, rhodium, palladium, osmium, iridium, platinum and rhenium in association with at least one inorganic oxide selected from the group consisting of silica and alumina; (b) absorbing sulfur oxides in said regeneration zone with said fluidizable particulate solids other than cracking catalyst; and (c) removing said absorbed sulfur oxides from the particulate solids other than cracking catalyst by contacting said particulate solids with the hydrocarbon feedstock in said reaction zone and with steam in said stripping zone.

Claim 12

In a process for the cyclic, fluidized catalytic cracking of a hydrocarbon feedstock containing organic sulfur compounds wherein: (i) said feedstock is subjected to cracking in a reaction zone through contact with a particulate cracking catalyst at a temperature in the range from about 850° to 1,200° F.; (ii) cracking catalyst, which is deactivated by sulfur-containing coke deposits, is separated from reaction zone effluent and passes to a stripping zone wherein volatile deposits are removed from said catalyst by contact with a stripping gas comprising steam at a temperature in the range from about 850° to about 1,200° F.; (iii) stripped catalyst is separated from stripping zone effluent and passes to a catalyst regeneration zone and non-stripped, sulfur-containing coke deposits are removed from the stripped catalyst by burning with an oxygen containing regeneration gas at a temperature in the range from about 1,050° to about 1,450° F., thereby forming sulfur oxides; and (iv) resulting catalyst is separated from regeneration zone effluent gas and recycled to the reaction zone; a method for reducing emissions of sulfur oxides in the regeneration zone effluent gas which comprises: (a) circulating fluidizable particulate solids through the cyclic catalytic cracking process which are physically admixed with said particulate cracking catalyst and comprise: (i) a first particulate solid other than said particulate cracking catalyst comprising at least one free or combined first metal selected from the group consisting of the rare earth metals in association with at least one inorganic oxide selected from the group consisting of silica and alumina and (ii) a second particulate solid other than said particulate cracking catalyst comprising at least one free or combined second metal selected from the group consisting of ruthenium, rhodium, palladium, osmium, iridium, platinum and rhenium in association with at least one inorganic oxide selected from the group consisting of silica and alumina; (b) absorbing sulfur oxides in said regeneration zone with said fluidizable particulate solids other than cracking catalyst; and (c) removing said absorbed sulfur oxides from the particulate solids other than cracking catalyst by contacting said particulate solids with the hydrocarbon feedstock in said reaction zone and with steam in said stripping zone.

Claim 13

The process as set forth in claim 10 wherein said cracking catalyst comprises a crystalline aluminosilicate.

Claim 14

The process as set forth in claim 11 wherein said stripping gas provides an amount of steam such that the ratio by weight of steam to said particles of cracking catalyst being supplied to the stripping zone is from about 0.005 to about 0.025.

Claim 15

The process as set forth in claim 12 wherein the amount of said first metal, calculated as the metal, is from about 0.2 to about 10 weight percent with respect to said admixture of cracking catalyst and particulate solids other than cracking catalyst.

Claim 16

The process as set forth in claim 13 wherein the amount of said second metal, calculated at the metal, is from about 0.1 part per million to about 10 parts per million with respect to said admixture of cracking catalyst and particulate solids other than cracking catalyst.

Claim 17

The process as set forth in claim 14 wherein said free or combined second metal is selected from the group consisting of platinum and palladium.

Claim 18

The process as set forth in claim 15 wherein said inorganic solid comprises alumina.

Claim 19

The process as set forth in claim 16 wherein said free or combined first metal comprises cerium.

Claim 20

The process as set forth in claim 17 wherein said inorganic oxide comprises a major portion of the particulate solid other than said cracking catalyst.