Endothermic removal of coke deposited on catalytic materials during carbo-metallic oil conversion

Claim 2

In a process for regenerating a finely divided hydrocarbon cracking catalyst having deposited thereon a substantial quantity of hydrocarbonaceous coke by contacting said catalyst at an elevated temperature with a gas rich in carbon dioxide to endothermically convert said hydrocarbonaceous coke substantially to carbon monoxide and water; the improvement which consists essentially of: (a) heating said catalyst to a temperature in a range from about 1350° F. to about 1600° F., (b) contacting said catalyst with said carbon dioxide rich gas for a time sufficient to endothermically convert a substantial portion of said hydrocarbonaceous coke to carbon monoxide and water while maintaining said catalyst at a temperature in the range of about 1250° F. to about 1600° F. throughout said contacting period, and (c) recovering said catalyst from step (b); said catalyst being further characterized by having about 0.2 to 5.0 weight % copper deposited thereon by being impregnated with an aqueous solution of a water soluble copper salt.

Claim 3

A process of claim 1 in which at least 1 weight % of copper is deposited on the catalyst.

Claim 4

A process of claim 1 in which the finely divided hydrocarbon cracking catalyst is a mixture of a crystalline aluminosilicate zeolite dispersed in a matrix including one or more of a silica, an alumina, a silica-alumina or a clay, said catalyst having added thereto 0.2 to 5 weight % of copper.

Claim 5

A process of claim 1 in which titanium also is deposited on the cracking catalyst.

Claim 6

A continuous process for regenerating a finely divided hydrocarbon cracking catalyst having deposited thereon (1) about 0.2 to 5.0 weight % of copper, and (2) a substantial quantity of hydrocarbonaceous coke and recovering regenerated catalyst having a hydrocarbonaceous coke level sufficiently low so that the catalyst will efficiently crack a high-boiling hydrocarbon feed stock having a Conradson carbon content of at least about 6 weight % and less than 200 ppm of metals consisting of Ni, V, Fe, and Cu, said process consisting essentially of: (a) continuously introducing into a first catalyst regeneration zone finely divided hydrocarbon cracking catalyst having deposited thereon about 0.2 to 5.0 weight % of copper and a substantial quantity of hydrocarbonaceous coke, said catalyst having an introduction temperature of less than about 1100° F., (b) contacting the catalyst in the first regeneration zone with an oxygen containing gas to partially burn the hydrocarbonaceous coke thereon, (c) maintaining the oxygen concentration and the catalyst contact time in the first regenerating zone so that the catalyst temperature is elevated to and maintained within a range of from about 1250° F. to about 1600° F., (d) continuously transferring catalyst from said first regeneration zone to a second regeneration zone, (e) contacting the catalyst in the second regeneration zone with a carbon dioxide rich gas to convert the remainder of the hydrocarbonaceous coke on the catalyst substantially to carbon monoxide and water, (f) maintaining the carbon dioxide concentration and the contact time in the second regeneration zone so that the catalyst temperature therein is maintained within a range of from about 1250° F. to about 1600° F. and the hydrocarbonaceous coke on the catalyst is reduced to a level sufficiently low so that the regenerated catalyst will efficiently crack a high-boiling hydrocarbon feed stock having a Conradson carbon content of at least about 6 weight % and less than 200 ppm of metals consisting of Ni, V, Fe, and Cu, and (g) continuously recovering regenerated catalyst from said second regenerating zone; said catalyst being further characterized by having the copper deposited thereon by being impregnated with an aqueous solution of a water soluble copper salt.

Claim 7

A continuous process for regenerating a finely divided hydrocarbon cracking catalyst having deposited thereon (1) about 0.2 to 5.0 weight % of copper, and (2) a substantial quantity of hydrocarbonaceous coke and recovering regenerated catalyst having a hydrocarbonaceous coke level sufficiently low so that the catalyst will efficiently crack a high-boiling hydrocarbon feed stock having a Conradson carbon content of at least about 6 weight % and less than 200 ppm of metals consisting of Ni, V, Fe, and Cu, said process consisting essentially of: (a) continuously introducing into a first catalyst regeneration zone finely divided hydrocarbon cracking catalyst having deposited thereon about 0.2 to 5.0 weight % of copper and a substantial quantity of hydrocarbonaceous coke, said catalyst having an introduction temperature of less than about 1100° F., (b) contacting the catalyst in the first regeneration zone with an oxygen containing gas to partially burn the hydrocarbonaceous coke thereon, (c) maintaining the oxygen concentration and the catalyst contact time in the first regenerating zone so that the catalyst temperature is elevated to and maintained within a range of from about 1250° F. to about 1600° F., (d) continuously transferring catalyst from said first regeneration zone to a second regeneration zone, (e) contacting the catalyst in the second regeneration zone with a carbon dioxide rich gas to convert the remainder of the hydrocarbonaceous coke on the catalyst substantially to carbon monoxide and water, (f) maintaining the carbon dioxide concentration and the contact time in the second regeneration zone so that the catalyst temperature therein is maintained within a range of from about 1250° F. to about 1600° F. and the hydrocarbonaceous coke on the catalyst is reduced to a level sufficiently low so that the regenerated catalyst will efficiently crack a high-boiling hydrocarbon feed stock having a Conradson carbon content of at least about 6 weight % and less than 200 ppm of metals consisting of Ni, V, Fe, and Cu, and (g) continuously recovering regenerated catalyst from said second regenerating zone; said catalyst being further characterized by having the copper deposited thereon by being impregnated with an aqueous solution of a water soluble copper salt.

Claim 8

A process of claim 5 in which the temperature in the second catalyst regeneration zone is maintained at about 1350°-1450° F.

Claim 9

A process of claim 6 in which the oxygen-containing gas employed in the first catalyst regeneration zone is a mixture of oxygen and the flue gas from the second catalyst regeneration zone.

Claim 10

A process of claim 5 in which the finely divided hydrocarbon cracking catalyst is a mixture of a crystalline aluminosilicate zeolite dispersed in a matrix including one or more of a silica, an alumina, a silica-alumina or a clay, said catalyst having added thereto 0.2 to 5 weight % of copper.

Claim 11

A process of claim 5 in which titanium also is deposited on the cracking catalyst.

Claim 12

A continuous process for regenerating a finely divided hydrocarbon cracking catalyst having deposited thereon (1) about 0.2 to 5.0 weight % copper, and (2) a substantial quantity of hydrocarbonaceous coke and recovering regenerated catalyst having a hydrocarbonaceous coke level sufficiently low so that the catalyst will efficiently crack a high-boiling hydrocarbon feed stock having a Conradson carbon content of at least about 6 weight % and less than 200 ppm of metals consisting of Ni, V, Fe, and Cu, said process consisting essentially of: (a) continuously withdrawing from a hydrocarbon cracking zone finely divided hydrocarbon cracking catalyst at a temperature of less than about 1100° F., said catalyst having deposited thereon about 0.2 to 5.0 weight % of copper and a substantial quantity of hydrocarbonaceous coke, (b) heating the catalyst withdrawn in step (a) to a temperature in a range from about 1250° F. to about 1600° F., (c) continuously transferring the heated catalyst from step (b) to a first regeneration zone, (d) contacting the catalyst in the first regeneration zone with a carbon dioxide-rich gas to convert a substantial portion of the hydrocarbonaceous coke on the catalyst substantially to carbon monoxide and water while maintaining the carbon dioxide concentration at a level such that the catalyst is maintained at a temperature in the range of from about 1250° F. to about 1600° F., (e) continuously transferring catalyst from said first regeneration zone to a second regeneration zone, (f) contacting the catalyst in the second regeneration zone with an oxygen containing gas to burn substantially the remainder of the hydrocarbonaceous coke on the catalyst, (g) maintaining the oxygen concentration and the contact time in the second regeneration zone so that the catalyst temperature therein is maintained within a range of from about 1250° F. to about 1600° F. and the hydrocarbonaceous coke on the catalyst is reduced to a level sufficiently low so that the regenerated catalyst will efficiently crack a high-boiling hydrocarbon feed stock having a Conradson carbon content of at least about 6 weight % and less than 200 ppm of metals consisting of Mi, V, Fe, and Cu, and (h) continuously recovering regenerated catalyst from said second regenerating zone; said catalyst being further characterized by having the copper deposited thereon by being impregnated with an aqueous solution of a water soluble copper salt.

Claim 13

A continuous process for regenerating a finely divided hydrocarbon cracking catalyst having deposited thereon (1) about 0.2 to 5.0 weight % copper, and (2) a substantial quantity of hydrocarbonaceous coke and recovering regenerated catalyst having a hydrocarbonaceous coke level sufficiently low so that the catalyst will efficiently crack a high-boiling hydrocarbon feed stock having a Conradson carbon content of at least about 6 weight % and less than 200 ppm of metals consisting of Ni, V, Fe, and Cu, said process consisting essentially of: (a) continuously withdrawing from a hydrocarbon cracking zone finely divided hydrocarbon cracking catalyst at a temperature of less than about 1100° F., said catalyst having deposited thereon about 0.2 to 5.0 weight % of copper and a substantial quantity of hydrocarbonaceous coke, (b) heating the catalyst withdrawn in step (a) to a temperature in a range from about 1250° F. to about 1600° F., (c) continuously transferring the heated catalyst from step (b) to a first regeneration zone, (d) contacting the catalyst in the first regeneration zone with a carbon dioxide-rich gas to convert a substantial portion of the hydrocarbonaceous coke on the catalyst substantially to carbon monoxide and water while maintaining the carbon dioxide concentration at a level such that the catalyst is maintained at a temperature in the range of from about 1250° F. to about 1600° F., (e) continuously transferring catalyst from said first regeneration zone to a second regeneration zone, (f) contacting the catalyst in the second regeneration zone with an oxygen containing gas to burn substantially the remainder of the hydrocarbonaceous coke on the catalyst, (g) maintaining the oxygen concentration and the contact time in the second regeneration zone so that the catalyst temperature therein is maintained within a range of from about 1250° F. to about 1600° F. and the hydrocarbonaceous coke on the catalyst is reduced to a level sufficiently low so that the regenerated catalyst will efficiently crack a high-boiling hydrocarbon feed stock having a Conradson carbon content of at least about 6 weight % and less than 200 ppm of metals consisting of Mi, V, Fe, and Cu, and (h) continuously recovering regenerated catalyst from said second regenerating zone; said catalyst being further characterized by having the copper deposited thereon by being impregnated with an aqueous solution of a water soluble copper salt.

Claim 14

A process of claim 10 in which the temperature in both the first and the second catalyst regeneration zones is maintained at about 1350°-1450° F.

Claim 15

A process of claim 11 in which the carbon dioxide-containing gas introduced into the first catalyst regeneration zone also contains oxygen.

Claim 16

A process of claim 10 in which the finely divided hydrocarbon cracking catalyst is a mixture of a crystalline aluminosilicate zeolite dispersed in a matrix including one or more of a silica, an alumina, a silica-alumina or a clay, said catalyst having added thereto 0.2 to 5 weight % of copper.

Claim 17

A process of claim 10 in which titanium also is deposited on the cracking catalyst.