Cracking of heavy hydrocarbons with improved yields of valuable liquid products

Claim 2

A process for catalytically cracking a hydrocarbon charge which comprises: (a) contacting the hydrocarbon charge in a coked catalyst zone at a temperature of at least 800° F. with a coked cracking catalyst having significantly reduced cracking activity, whereby at least a portion of the hydrocarbon charge is vaporized; (b) separating the hydrocarbon vapors into at least a high boiling fraction and a low boiling fraction; (c) reducing the amount of coke on the coked catalyst of step (a) in a regeneration zone by contacting the coked catalyst with molecular oxygen for a sufficient residence time and at a suitable temperature to regenerate the cracking catalyst; (d) cracking the high boiling fraction from step (b) in the absence of added free hydrogen in a cracking zone by contacting said high boiling fraction with the regenerated cracking catalyst, whereby a hydrocarbon product having a lower average molecular weight than the high boiling fraction is produced and coke is deposited on the cracking catalyst to significantly lower its cracking activity; and (e) introducing the coked cracking catalyst of step (d) into the coked catalyst zone for the purpose of contacting additional hydrocarbon charge.

Claim 3

The process of claim 1 wherein the coked catalyst in the coked catalyst zone has a microactivity for catalytic cracking of less than 60.

Claim 4

The process of claim 2 wherein the coked catalyst in the coked catalyst zone has a microactivity for catalytic cracking of less than 40.

Claim 5

The process of claim 1 wherein the contacting between the hydrocarbon charge and the coked cracking catalyst takes place at a temperature of between about 900° F. and 1000° F.

Claim 6

The process of claim 1 wherein the high boiling fraction of step (b) comprises only a part of the feed entering the cracking zone in step (d).

Claim 7

The process of claim 1 wherein separation between the high boiling and low boiling fractions of the hydrocarbon vapors is made at a temperature of between about 400° F. and about 700° F.

Claim 8

The process of claim 1 wherein the amount of coke on the cracking catalyst is reduced to no more than about 0.5% by weight during regeneration.

Claim 9

The process of claim 1 wherein the coked catalyst zone is the stripping section of a fluid catalytic cracking reactor and the high boiling fraction of the hydrocarbon vapors is recycled to the riser of a fluid catalytic cracking reactor.

Claim 10

The process of claim 8 wherein the stripping section and the riser are incorporated in the same fluid catalytic cracking reactor.

Claim 11

The process of claims 8 or 9 wherein the high boiling fraction of the hydrocarbon vapors comprises only part of the hydrocarbons entering the riser.

Claim 12

The process of claim 8 wherein the hydrocarbon product produced by cracking the high boiling fraction is ballistically separated from the coked cracking catalyst and removed from the fluid catalytic cracking reactor separately from the hydrocarbon vapors formed in the stripping section.

Claim 13

The process of claim 1 wherein the hydrocarbon charge contains high boiling components and is characterized by a substantial Ramsbottom carbon number.

Claim 14

The process of claim 12 wherein the hydrocarbon charge has a Ramsbottom carbon number of at least 1.

Claim 15

The process of claim 1 wherein the hydrocarbon charge contains a significant fraction boiling below 650° F.

Claim 16

The process of claim 1 wherein the hydrocarbon charge has a broad boiling range and is characterized by both a substantial Ramsbottom carbon number and at least a significant fraction boiling below 650° F.

Claim 17

The process of claim 15 wherein the fraction boiling below 650° F. makes up more than 5% by volume of the hydrocarbon charge.

Claim 18

The process of claim 1 wherein the hydrocarbon charge boils between about 650° F. and 1100° F., said hydrocarbon charge further having a Ramsbottom carbon number of less than 1.

Claim 19

The process of claim 1 wherein additional heat is provided to the coked catalyst zone.

Claim 20

A process for catalytically cracking a hydrocarbon charge containing high boiling components and substantial Ramsbottom carbon number which comprises: (a) contacting the hydrocarbon charge in a decarbonization zone at a temperature of at least 800° F. with a coked cracking catalayst having significantly reduced cracking activity, whereby a hydrocarbon intermediate containing reduced Ramsbottom carbon as compared to the hydrocarbon charge is produced and additional coke is deposited on said coke catalyst; (b) separating the hydrocarbon intermediate into at least a high boiling fraction and a low boiling fraction; (c) reducing the amount of coke on the coked catalyst of step (a) in a regeneration zone by contacting the coked catalyst with molecular oxygen for a sufficient residence time and at a suitable temperature to regenerate the cracking catalyst; (d) cracking the intermediate high boiling fraction in the absence of added free hydrogen in a cracking zone by contacting the hydrocarbon intermediate with the regenerated cracking catalyst, whereby a hydrocarbon product having a lower average molecular weight than the high boiling fraction is produced and coke is deposited on the cracking catalyst to significantly lower its cracking activity; (e) recovering the hydrocarbon product of step (d) separately from the hydrocarbon intermediate of step (a); and (f) introducing the coked cracking catalyst of step (d) into the decarbonization zone for the purpose of contacting additional hydrocarbon charge.

Claim 21

A process for catalytically cracking a hydrocarbon charge containing high boiling components and substantial Ramsbottom carbon number which comprises: (a) contacting the hydrocarbon charge in a decarbonization zone at a temperature of at least 800° F. with a coked cracking catalayst having significantly reduced cracking activity, whereby a hydrocarbon intermediate containing reduced Ramsbottom carbon as compared to the hydrocarbon charge is produced and additional coke is deposited on said coke catalyst; (b) separating the hydrocarbon intermediate into at least a high boiling fraction and a low boiling fraction; (c) reducing the amount of coke on the coked catalyst of step (a) in a regeneration zone by contacting the coked catalyst with molecular oxygen for a sufficient residence time and at a suitable temperature to regenerate the cracking catalyst; (d) cracking the intermediate high boiling fraction in the absence of added free hydrogen in a cracking zone by contacting the hydrocarbon intermediate with the regenerated cracking catalyst, whereby a hydrocarbon product having a lower average molecular weight than the high boiling fraction is produced and coke is deposited on the cracking catalyst to significantly lower its cracking activity; (e) recovering the hydrocarbon product of step (d) separately from the hydrocarbon intermediate of step (a); and (f) introducing the coked cracking catalyst of step (d) into the decarbonization zone for the purpose of contacting additional hydrocarbon charge.

Claim 22

The process of claim 19 wherein step (a) is carried out in a separate reactor vessel from step (d).

Claim 23

The process of claim 19 wherein the high boiling fraction of the hydrocarbon intermediate comprises only part of the hydrocarbons entering the cracking zone in step (d).

Claim 24

The process of claim 19 wherein step (a) is carried out in the stripping section of a fluid catalytic cracking reactor and step (d) is carried out by recycling the high boiling fraction to the riser of said fluid catalytic cracking reactor, the hydrocarbon intermediate from the stripper and the hydrocarbon product from the riser being recovered separately from the fluid catalytic cracking reactor by the additional steps of ballistically separating the cracking catalyst from the hydrocarbon product and withdrawing the hydrocarbon product by recovery means opening directly into the riser and separate from the means used to withdraw the hydrocarbon intermediate from the stripping section.

Claim 25

A process for catalytically cracking a hydrocarbon charge boiling below about 1100° F. with a Ramsbottom carbon number of less than 1, the process comprising: (a) contacting the hydrocarbon charge in an coked catalyst zone at a temperature of at least 800° F. with a coked cracking catalyst having significantly reduced cracking activity , whereby hydrocarbon vapors are produced; (b) separating the hydrocarbon vapors into at least a high boiling fraction and a lower boiling fraction; (c) reducing the amount of coke on the coked catalyst of step (a) in a regeneration zone by contacting the coked catalyst with molecular oxygen for a sufficient residence time and at a suitable temperature to regenerate the cracking catalyst; (d) cracking the high boiling fraction from step (b) in the absence of added free hydrogen in a cracking zone by contacting the high boiling fraction with the regenerated cracking catalyst, whereby a hydrocarbon product having a lower average molecular weight than the high boiling fraction is produced and coke is deposited on the cracking catalyst to significantly lower its cracking activity; (e) recovering the hydrocarbon product of step (d) separately from the hydrocarbon vapors of step (a); and (f) introducing the coked cracking catalyst of step (d) into the coked catalyst zone for the purpose of contacting additional hydrocarbon charge.

Claim 26

A process for catalytically cracking a hydrocarbon charge boiling below about 1100° F. with a Ramsbottom carbon number of less than 1, the process comprising: (a) contacting the hydrocarbon charge in an coked catalyst zone at a temperature of at least 800° F. with a coked cracking catalyst having significantly reduced cracking activity , whereby hydrocarbon vapors are produced; (b) separating the hydrocarbon vapors into at least a high boiling fraction and a lower boiling fraction; (c) reducing the amount of coke on the coked catalyst of step (a) in a regeneration zone by contacting the coked catalyst with molecular oxygen for a sufficient residence time and at a suitable temperature to regenerate the cracking catalyst; (d) cracking the high boiling fraction from step (b) in the absence of added free hydrogen in a cracking zone by contacting the high boiling fraction with the regenerated cracking catalyst, whereby a hydrocarbon product having a lower average molecular weight than the high boiling fraction is produced and coke is deposited on the cracking catalyst to significantly lower its cracking activity; (e) recovering the hydrocarbon product of step (d) separately from the hydrocarbon vapors of step (a); and (f) introducing the coked cracking catalyst of step (d) into the coked catalyst zone for the purpose of contacting additional hydrocarbon charge.

Claim 27

The process of claim 23 wherein step (a) is carried out in a separate reactor vessel from step (d).

Claim 28

The process of claim 23 wherein step (a) is carried out in the stripping section of a fluid catalytic cracking reactor and step (d) is carried out by recycling the high boiling fraction to the riser of said fluid catalytic cracking reactor, the hydrocarbon intermediate from the stripper and the hydrocarbon product from the riser being recovered separately from the fluid catalytic cracking reactor by the additional steps of ballistically separating the cracking catalyst from the hydrocarbon product and withdrawing the hydrocarbon product by recovery means opening directly into the riser which is separate from the means used to withdraw the hydrocarbon vapors from the stripping section.