PROCESS FOR RECOVERING HYDROCRACKED EFFLUENT

• US 20190085251A1
• Filed: 09/20/2017
• Published: 03/21/2019
• Est. Priority Date: 09/20/2017
• Status: Active Grant

• Current Assignee: UOP Llc (Honeywell International Inc.)
• Original Assignee: UOP Llc (Honeywell International Inc.)
• Inventors: Eizenga, Donald A., Sangalli, Massimo, Hoehn, Richard K., Ulas Acikgoz, Saadet, Pham, Trung
• Granted Patent: US 10,457,878 B2
• Time in Patent Office: Days
• CPC Class Codes: C10G 47/00 Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions C10G15/00 takes precedence; destructive hydrogenation of non-melting solid carbonaceous or similar materials C10G1/06
• CPC Class Codes: C10G 49/22 Separation of effluents
• CPC Class Codes: C10G 65/12 including cracking steps and other hydrotreatment steps
• CPC Class Codes: C10G 7/00 Distillation of hydrocarbon oils

Abstract

We have discovered a process for hydrocracking a distillate stream and separating it into several product cuts including LPG, light naphtha, heavy naphtha and distillate without a stripper column. Additionally, no more than two heaters relying on external utilities are required for reboiling fractionator bottoms.

Claims

1. A hydroprocessing process comprising:

hydrocracking a diesel feed stream in a hydrocracking reactor with a hydrogen stream over hydrocracking catalyst to provide a hydrocracked stream;

separating said hydroprocessed effluent stream in a separator to provide a vaporous hydrocracked stream and a liquid hydrocracked stream;

fractionating the liquid hydrocracked stream in a first fractionation column to provide a first overhead stream comprising LPG and light naphtha and a first bottoms stream comprising heavy naphtha and kerosene;

fractionating the first overhead stream in a second fractionation column to provide a second overhead stream comprising LPG and a second bottoms stream comprising light naphtha; and

fractionating the first bottoms stream in a third fractionation column to provide a third overhead stream comprising heavy naphtha and a second bottoms stream comprising distillate.

2. The hydroprocessing process of claim 1 further comprising heat exchanging the first bottoms stream with a boilup stream taken from the second bottoms stream to reboil the boilup stream and return it to the second fractionation column.

3. The hydroprocessing process of claim 1 wherein the third fractionation column is operated at a lower pressure than the second fractionation column.

4. The hydroprocessing process of claim 1 wherein the third fractionation column is operated at a lower pressure than the first fractionation column.

5. The hydroprocessing process of claim 1 further comprising taking the first overhead stream as a liquid stream.

6. The hydroprocessing process of claim 1 further comprising taking the second overhead stream as a liquid stream.

7. The hydroprocessing process of claim 1 wherein the first bottoms stream comprises more heavy naphtha than the first overhead stream.

8. The hydroprocessing process of claim 1 wherein the diesel feed stream has a T5 between about 150°

C. (302°

F.) and about 200°

C. (392°

F.) and a T95 between about 343°

C. (650°

F.) and about 399°

C. (750°

F.) using the TBP distillation method.

9. The hydroprocessing process of claim 1 wherein said third bottoms stream has a T5 between about 177°

C. (350°

F.) and about 204°

C. (400°

F.) and a T95 between about 266°

C. (510°

F.) and about 371°

C. (700°

F.) using the ASTM D-86 distillation method.

10. The hydroprocessing process of claim 1 further comprising heat exchanging the third overhead stream with a boilup stream taken from the second bottoms stream to reboil the boilup stream and return it to the second fractionation column.

11. The hydroprocessing process of claim 1 wherein said third overhead stream has a T5 between about 99°

C. (210°

F.) and about 110°

C. (230°

F.) and a T95 between about 154°

C. (310°

F.) and about 193°

C. (380°

F.) using the ASTM D-86 distillation method.

12. A hydroprocessing process comprising:

hydrocracking a diesel feed stream in a hydrocracking reactor with a hydrogen stream over hydrocracking catalyst to provide a hydrocracked stream;

separating said hydroprocessed effluent stream in a separator to provide a vaporous hydrocracked stream and a liquid hydrocracked stream;

fractionating the liquid hydrocracked stream in a first fractionation column to provide a first overhead stream comprising LPG and light naphtha and a first bottoms stream comprising heavy naphtha and kerosene;

fractionating the first overhead stream in a second fractionation column to provide a second overhead stream comprising LPG and a second bottoms stream comprising light naphtha;

taking a boilup stream from the second bottoms stream and returning the boilup stream to the second fractionation column;

fractionating the first bottoms stream in a third fractionation column to provide a third overhead stream comprising heavy naphtha and a second bottoms stream comprising distillate; and

heat exchanging the first bottoms stream with the boilup stream to reboil the boilup stream.

13. The hydroprocessing process of claim 12 wherein the third fractionation column is operated at a lower pressure than the second fractionation column.

14. The hydroprocessing process of claim 12 wherein the third fractionation column is operated at a lower pressure than the first fractionation column.

15. The hydroprocessing process of claim 12 further comprising taking the first overhead stream as a liquid stream.

16. The hydroprocessing process of claim 12 wherein the first bottoms stream comprises a higher concentration of heavy naphtha than the first overhead stream.

17. A hydroprocessing process comprising:

hydrocracking a diesel feed stream, having a T5 between about 150°

C. (302°

F.) and about 200°

C. (392°

F.) and a T95 between about 343°

C. (650°

F.) and about 399°

C. (750°

F.) using the TBP distillation method, in a hydrocracking reactor with a hydrogen stream over hydrocracking catalyst to provide a hydrocracked stream;

separating said hydroprocessed effluent stream in a separator to provide a vaporous hydrocracked stream and a liquid hydrocracked stream;

fractionating the liquid hydrocracked stream in a first fractionation column to provide a first overhead stream comprising LPG and light naphtha and a first bottoms stream comprising heavy naphtha and kerosene;

fractionating the first overhead stream in a second fractionation column to provide a second overhead stream comprising LPG and a second bottoms stream comprising light naphtha; and

fractionating the first bottoms stream in a third fractionation column to provide a third overhead stream comprising heavy naphtha and a second bottoms stream comprising kerosene.

18. The hydroprocessing process of claim 17 wherein said third bottoms stream has a T5 between about 177°

C. (350°

F.) and about 204°

C. (400°

F.) and a T95 between about 266°

C. (510°

F.) and about 371°

C. (700°

F.) using the ASTM D-86 distillation method.

19. The hydroprocessing process of claim 17 wherein said third overhead stream has a T5 between about 99°

C. (210°

F.) and about 110°

C. (230°

F.) and a T95 between about 154°

C. (310°

F.) and about 171°

C. (340°

F.) using the ASTM D-86 distillation method.

20. The hydroprocessing process of claim 17 further comprising heat exchanging the first bottoms stream with a boilup stream taken from the second bottoms stream to reboil the boilup stream and return it to the second fractionation column.