Multiple riser fluidized catalytic cracking process utilizing hydrogen and carbon-hydrogen contributing fragments

• US 4,853,105 A
• Filed: 02/01/1988
• Issued: 08/01/1989
• Est. Priority Date: 09/03/1986
• Status: Expired due to Fees

• Current Assignee: Mobil Oil Corporation (Exxon Mobil Corporation)
• Original Assignee: Mobil Oil Corporation (Exxon Mobil Corporation)
• Inventors: Owen, Hartley, Schipper, Paul H., Herbst, Joseph A.
• Primary Examiner(s): CALDAROLA, GLENN A
• Application Number:
  US07/148,204
• Time in Patent Office: 547 Days
• Field of Search: 208/153, 208/144, 208/145, 208/157, 208/74-78, 208/73, 208/111, 208/120
• US Class Current: 208/74
• CPC Class Codes: C10G 11/18 according to the "fluidised-bed" technique
• CPC Class Codes: C10G 51/06 plural parallel stages only

Abstract

A catalytic cracking process is provided which comprises:

(a) cracking a first heavy hydrocarbon feed in a first riser in the presence of a mixed catalyst composition comprising, as a first catalyst component, an amorphous cracking catalyst and/or a large pore crystalline cracking catalyst and, as a second catalyst component, a shape selective medium pore crystalline silicate zeolite, to provide gasoline boiling range material and one or more light hydrocarbons; and,

(b) cracking a thermally treated second heavy hydrocarbon feed in a second riser in the presence of said mixed catalyst composition and in admixture with a gasiform material contributing mobile hydrogen species and/or carbon-hydrogen fragments at the reaction conditions employed to provide gasoline boiling range material in increased yield and/or of higher quality.

Claims

1. A catalytic cracking process which comprises:

(a) cracking a gas oil in a first riser in the presence of a mixed cataylst composition comprising, as a first catalyst component, at least one member of the group of amorphous cracking catalyst and large pore crystalline cracking catalyst and as a second catalyst component, a shape selective zeolite, at a mixed catalyst to feed ratio from about 2;

1 to about 20;

1 and a temperature from about 900°

to 1150°

F. to produce cracked products comprising C₁ to C₅ hydrocarbons, gasoline boiling range materials and spent catalyst, and stripping at least a portion of spent catalyst to produce stripped catalyst which is regenerated in a catalyst regeneration zone to produce hot, regenerated catalyst;

(b) generating in a lower region of a second riser reactor at least one of mobile hyrogen species and carbon-hydrogen fragments by contacting a stream of light hydrocarbons with hot regenerated catalyst at a catalyst to feed ratio of about 50;

1 to 200;

1 and at a temperature of about 1100°

to 1500°

F. to form a catalyst-hydrocarbon suspension comprising carbon-hydrogen fragments, which suspension is discharged into an upper region of said second riser;

(c) adding a visbroken resid feed to said upper region to contact the catalyst-hyrocarbon suspension discharged from the lower region of the second riser and reacting said visbroken resid in the presence of said mixed catalyst composition under conditions effecting cracking and additive carbon-hydrogen reactions with said resid and forming a resid-catalyst mixture;

(d) quenching said resid-catalyst mixture in said second riser by adding thereto a portion of said spent catalyst, discharged from said first riser to produce a quenched resid-catalyst mixture having a temperature of about 950°

to 1150°

F. and discharging from said second riser a mixture of catalytically cracked products and spent catalyst.

2. The process of claim 1 wherein the visbroken second heavy hydrocarbon feed and the gasiform material are reacted in the presence of said mixed catalyst composition under conditions affecting cracking and additive carbon-hydrogen reactions to produce products of a quality improved over those formed in the absence of said added gasiform material.

3. The process of claim 1 wherein the gasiform material comprises one or more C₁ to C₅ hydrocarbons recovered from the process.

4. The process of claim 1 wherein thermal treatment of the second heavy hydrocarbon feed is by visbreaking.

5. The process of claim 1 wherein the first catalyst component is a large pore crystalline silicate zeolite.

6. The process of claim 1 wherein the first catalyst component is a large pore crystalline silicate zeolite selected from the group consisting of zeolite X, Y, REY, USY, RE-USY, mordenite and/or mixtures thereof and the second catalyst component is selected from the group consisting of ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35, ZSM-38 and ZSM-48.

7. The process of claim 6 in which the second catalyst component contains at least one element selected from the group consisting of boron, gallium, zirconium and titanium in the framework structure thereof and/or deposited thereon.

8. The process of claim 6 wherein, in the first riser, the zeolite concentration of the second catalyst component represents from about 0.01 to about 10 weight percent of the total catalyst mixture, the temperature is within the range of from about 900°

to about 1150°

F., the catalyst to oil ratio is from about 2;

1 to about 20;

1 and the catalyst contact time is from about 0.5 to about 30 seconds.

9. The process of claim 6 wherein, in the first riser, the zeolite concentration of the second catalyst component represents from about 0.1 to about 5.0 weight percent of the total catalyst mixture, the temperature is within the range of from about 925°

to about 1000°

F., the catalyst to oil ratio is from about 4;

1 to about 10;

1 and the catalyst contact time is from about 1 to about 15 seconds.

10. The process of claim 1 wherein, in the first riser, the zeolite concentration of the second catalyst component represents from 0.5 to about 25 weight percent of the total catalyst mixture, to 1150°

F., the catalyst;

oil ratio is from 2;

1 to 20;

1 and the catalyst contact time is from 0.5 to about 30 seconds.

11. The process of claim 6 wherein, in the first riser, the zeolite concentration of the second catalyst component represents from about 1 to about 10 weight percent of the total catalyst mixture, the temperature is within the range of from about 925°

F. to about 1000°

F., the catalyst;

oil ratio is from about 4;

1 to about 10;

1 and the catalyst contact time is from about 1 to about 15 seconds.

12. The process of claim 6 wherein, in the lower region of the second riser, the temperature is within the range of from about 1100°

to about 1500°

F., the catalyst to oil ratio is from about 50;

1 to about 200;

1 and the catalyst contact time is from about 10 to about 50 seconds.

13. The process of claim 6 wherein, in the lower region of the second riser, the temperature is within the range of from about 1250°

to about 1350°

F., the catalyst to oil ratio is from about 100;

1 to about 150;

1 and the catalyst contact time is from about 15 to about 35 seconds.

14. The process of claim 6 wherein, in the upper region of the second riser, the temperature is within the range of from about 950°

to about 1150°

F., the total catalyst to hydrocarbon ratio is from about 3;

1 to about 10;

1 and the catalyst contact time is from about 0.5 to about 10 seconds.

15. The process of claim 6 wherein, in the upper region of the second riser, the temperature is within the range of from about 1000°

to about 1100°

F., the total catalyst to hydrocarbon ratio is from about 4;

1 to about 8;

1 and the catalyst contact time is from about 1 to about 5 seconds.

16. The process of claim 1 wherein the first heavy hydrocarbon feed is subjected to hydrotreatment prior to its introduction in the first riser.

17. The process of claim 16 wherein the hydrotreatment utilizes process hydrogen.

18. The process of claim 1 wherein cracking step (a) is also carried out in the presence of a gasiform material contributing mobile hydrogen species and/or carbon-hydrogen fragments at the reaction conditions employed.

19. The process of claim 1 wherein the first and/or second catalyst component contains a hydrogen-activating function.

20. The process of claim 6 wherein the first and/or second catalyst component contains a hyrogen-activating function.