Integrated products separation from fluid catalytic cracking and aromatization processes

• US 5,110,446 A
• Filed: 09/07/1990
• Issued: 05/05/1992
• Est. Priority Date: 02/14/1989
• Status: Expired due to Fees

• Current Assignee: Mobil Oil Corporation (Exxon Mobil Corporation)
• Original Assignee: Mobil Oil Corporation (Exxon Mobil Corporation)
• Inventors: Harandi, Mohsen N., Owen, Hartley
• Primary Examiner(s): MYERS, HELANE ELEANORA
• Application Number:
  US07/579,417
• Time in Patent Office: 606 Days
• Field of Search: 208/70, 208/100, 208/103, 208/105, 208/92, 208/93, 208/94, 585/300, 585/315, 585/322, 585/413, 585/314
• US Class Current: 208/100
• CPC Class Codes: C10G 57/02 with polymerisation
• CPC Class Codes: C10G 63/04 including at least one cracking step
• CPC Class Codes: C10G 70/00 Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00

Abstract

The present invention provides a process for decreasing the energy consumption of a catalytic cracking process product recovery section while improving gasoline yield by integrating multistage vapor compression and product recovery with deacidification and conversion of C₂ -C₄ aliphatics to C₅ + normally liquid hydrocarbons.

Claims

1. A method for improving the gasoline product yield in a catalytic cracking process comprising the steps of:

(a) catalytically cracking a hydrocarbon feedstock containing gas oil or heavier fractions to a cracked product stream containing distillate, gasoline, lighter boiling range hydrocarbon fractions, and H₂ S, CO₂, or both H₂ S and CO₂ ;

(b) providing a product fractionation section for separating and recovering gasoline and lighter components from said product stream, said product fractionation section including a primary cracked product separation zone, a multistage compressor, and a central debutanizer separator;

(c) flowing a stream containing cracked gasoline and lighter boiling hydrocarbons withdrawn from an upper section of said primary cracked product separation zone to a first accumulation zone to provide a vapor stream enriched in C₄ -cracked hydrocarbons containing H₂ S, CO₂, or both H₂ S and CO₂, and a liquid stream enriched in C₅ +hydrocarbons;

(d) compressing said vapor stream of step (c) in a first stage of said multistage compressor of step (b) to evolve a deacidification charge stream;

(e) deacidifying said deacidification charge stream of step (d) by countercurrently contacting said vapor deacidification charge stream in a first sorption zone with an acid sorbent whereby said acid sorbent becomes enriched in H₂ S, CO₂, or both H₂ S and CO₂ ;

(f) withdrawing a deacidified stream enriched in C₄ -cracked hydrocarbons from said first sorption zone and flowing said deacidified stream to a second accumulation zone;

(g) contacting a deacidified vapor stream withdrawn from said second accumulation zone of step (f) with a catalyst comprising a zeolite under conversion conditions to convert C₄ -cracked hydrocarbon products to a reactor effluent stream containing gasoline boiling range constituents including aromatics;

(h) cooling and at least partially condensing said reactor effluent stream and flowing said cooled reactor effluent stream to a third accumulation zone;

(i) compressing a vapor stream withdrawn from said third accumulation zone in a second stage of said multistage compressor of step (b);

(j) cooling said second stage compressor effluent of step (i) to at least partially condense said second stage compressor effluent;

(k) flowing said at least partially condensed second stage compressor effluent to a fourth accumulation zone to separate said at least partially condensed second stage compressor effluent into a vapor stream enriched in C₃ -components and a liquid stream containing C₄ +components;

(l) charging liquid product streams from said first accumulation zone, said second accumulation zone, said third accumulation zone, and said fourth accumulation zone to said central debutanizer separator to separate said liquid product streams into a central debutanizer overhead stream enriched in C₄ -components and a bottom stream enriched in C₅ +gasoline boiling range components; and

(m) flowing a portion of said central debutanizer bottom stream to a second sorption zone to countercurrently sorb and remove C₃ +components from said fourth accumulation zone overhead stream of step (l) and recycling said sorbed C₃ +components to said fourth accumulation zone.

2. The method of claim 1 wherein said zeolite of step (g) has a Constraint Index of from about 1 to about 12.

3. The method of claim 2 wherein said zeolite has the structure of at least one selected from the group consisting of ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM-35, ZSM-48, and MCM-22.

4. The method of claim 3 wherein said zeolite contains gallium.

5. A method for improving the gasoline product yield in a catalytic cracking process comprising the steps of:

(a) catalytically cracking a hydrocarbon feedstock containing gas oil or heavier fractions to a cracked product stream containing distillate, gasoline, lighter boiling range hydrocarbon fractions, and H₂ S, CO₂, or both H₂ S and CO₂ ;

(b) providing a product fractionation section for separating and recovering gasoline and lighter components from said product stream, said product fractionation section including a primary cracked product separation zone, a multistage compressor, and a central debutanizer separator;

(c) flowing a stream containing cracked gasoline and lighter boiling hydrocarbons withdrawn from an upper section of said primary cracked product separation zone to a first accumulation zone to provide a vapor stream enriched in C₄ -cracked hydrocarbons containing H₂ S, CO₂, or both H₂ S and CO₂, and a liquid stream enriched in C₅ +hydrocarbons;

(d) compressing said vapor stream of step (c) in a first stage of said multistage compressor of step (b);

(e) cooling said first stage compressor effluent of step (d) to at least partially condense said first stage compressor effluent;

(f) flowing said at least partially condensed first stage compressor effluent to a second accumulation zone to provide a vapor deacidification charge stream containing H₂ S, CO₂, or both H₂ S and CO₂, and a second accumulation zone liquid stream enriched in C₄ +hydrocarbons;

(g) deacidifying said vapor deacidification charge stream of step (f) by countercurrently contacting said vapor deacidification charge stream in a first sorption zone with an acid sorbent whereby said acid sorbent becomes enriched in H₂ S, CO₂, or both H₂ S and CO₂ ;

(h) withdrawing a deacidified vapor stream enriched in C₄ -cracked hydrocarbons from first sorption zone and flowing said deacidified vapor stream to a third accumulation zone;

(i) contacting at least a portion of said deacidified vapor stream with a catalyst comprising a zeolite under conversion conditions to convert C₄ -cracked hydrocarbon products to a reactor effluent stream containing gasoline boiling range constituents including aromatics;

(j) cooling and at least partially condensing said reactor effluent stream and flowing said cooled reactor effluent stream to a fourth accumulation zone;

(k) compressing a vapor stream withdrawn from said fourth accumulation zone in a second stage of said multistage compressor of step (b);

(l) cooling said second stage compressor effluent of step (k) to at least partially condense said second stage compressor effluent;

(m) flowing said at least partially condensed second stage compressor effluent to a fifth accumulation zone to separate said at least partially condensed second stage compressor effluent into a vapor stream enriched in C₃ -components and a liquid stream containing C₄ +components;

(n) charging liquid product streams from said first accumulation zone, said second accumulation zone, said fourth accumulation zone, and said fifth accumulation zone to said central debutanizer separator to separate said liquid product streams into a central debutanizer overhead stream enriched in C₄ -components and a bottom stream enriched in C₅ +gasoline boiling range components;

(o) flowing a portion of said central debutanizer bottom stream to a second sorption zone to countercurrently sorb and remove C₃ +components from said fifth accumulation zone overhead stream of step (m) and recycling said sorbed C₃ +components to said fifth accumulation zone; and

(p) recycling at least a portion of said central debutanizer overhead stream to said catalytic conversion step (i).

6. The process of claim 5 wherein said zeolite of step (i) has a Constraint Index of from about 1 to 12.

7. The process of claim 6 wherein said zeolite has the structure of at least one selected from the group consisting of ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM-35, ZSM-48, and MCM-22.

8. The process of claim 7 wherein said zeolite contains gallium.

9. A method for improving the gasoline product yield in a catalytic cracking process comprising the steps of:

(a) catalytically cracking a hydrocarbon feedstock containing gas oil or heavier fractions to a cracked product stream containing distillate, gasoline, lighter boiling range hydrocarbon fractions, and H₂ S, CO₂, or both H₂ S and CO₂ ;

(b) providing a product fractionation section for separating and recovering gasoline and lighter components from said product stream, said product fractionation section including a primary cracked product separation zone, a multistage compressor, and a central debutanizer separator;

(c) flowing a stream containing cracked gasoline and lighter boiling hydrocarbons withdrawn from an upper section of said primary cracked product separation zone to a first accumulation zone to provide a vapor stream enriched in C₄ -cracked hydrocarbons containing H₂ S, CO₂, or both H₂ S and CO₂, and a liquid stream enriched in C₅ +hydrocarbons;

(d) compressing said vapor stream of step (c) in a first stage of said multistage compressor of step (b);

(e) cooling said first stage compressor effluent of step (d) to at least partially condense said first stage compressor effluent;

(f) flowing said at least partially condensed first stage compressor effluent to a second accumulation zone to provide a vapor deacidification charge stream containing H₂ S, CO₂, or both H₂ S and CO₂, and a second accumulation zone liquid stream enriched in C₄ +hydrocarbons;

(g) deacidifying said vapor deacidification charge stream of step (f) by countercurrently contacting said vapor deacidification charge stream in a first sorption zone with an acid sorbent whereby said acid sorbent becomes enriched in H₂ S, CO₂, or both H₂ S and CO₂ ;

(h) withdrawing a deacidified vapor stream enriched in C₄ -cracked hydrocarbons from first sorption zone and flowing said deacidified vapor stream to a third accumulation zone;

(i) contacting a deacidified vapor stream withdrawn from said third accumulation zone of step (h) with a catalyst comprising a zeolite under conversion conditions to convert C₄ -cracked hydrocarbon products to a reactor effluent stream containing gasoline boiling range constituents including aromatics;

(j) cooling and at least partially condensing said reactor effluent stream and flowing said cooled reactor effluent stream to a fourth accumulation zone;

(k) compressing a vapor stream withdrawn from said fourth accumulation zone in a second stage of said multistage compressor of step (b);

(l) cooling said second stage compressor effluent of step (k) to at least partially condense said second stage compressor effluent;

(m) flowing said at least partially condensed second stage compressor effluent to a fifth accumulation zone to separate said at least partially condensed second stage compressor effluent into a vapor stream enriched in C₃ -components and a liquid stream containing C₄ +components;

(n) charging liquid product streams from said first accumulation zone, said second accumulation zone, said fourth accumulation zone, and said fifth accumulation zone to said central debutanizer separator to separate said liquid product streams into a central debutanizer overhead stream enriched in C₄ -components and a bottom stream enriched in C₅ +gasoline boiling range components;

(o) flowing a portion of said central debutanizer bottom stream to a second sorption zone to countercurrently sorb and remove C₃ +components from said fifth accumulation zone overhead stream of step (m) and recycling said sorbed C₃ +components to said fifth accumulation zone; and

(p) recycling at least a portion of said central debutanizer overhead stream to said catalytic conversion step (i).

10. The process of claim 9 wherein said zeolite of step (i) has a Constraint Index of from about 1 to about 12.

11. The process of claim 10 wherein said zeolite has the structure of at least one selected from the group consisting of ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM-35, ZSM-48, and MCM-22.

12. The process of claim 11 wherein said zeolite contains gallium.