Systems and methods for enhancing the extractive section operability and modifying solvent heat recovery cycle in the separation of C4 mixtures

Patent metadata

Field	Value
Publication number	US-12404222-B2
Application number	US-202117760103-A
Country	US
Kind code	B2
Filing date	Jan 26, 2021
Priority date	Feb 6, 2020
Publication date	Sep 2, 2025
Grant date	Sep 2, 2025

Abstract

A system and a method for separating C 4 and recovering 1,3-butadiene are disclosed. The system includes a main washer column, a rectifier column for separating a bottom stream from the main washer column, an after washer column for purifying 1,3-butadiene from a side stream of the rectifier column comprising acetylenes and butadienes, a degasser column for separating a bottom stream from the rectifier column to produce a lean solvent stream. The lean solvent stream comprises primarily the solvent and about 8.3% water used in the main washer column and after washer column. A reboiler for the rectifier column includes one or more heat exchange units. At least one of the heat exchange units of the reboiler for the rectifier column uses steam as heating medium.

First claim

The invention claimed is:

1. A method of separating a mixture of C 4 hydrocarbons and a solvent, the method comprising:
separating the mixture of C 4 hydrocarbons and the solvent in a rectifier column to produce a top stream comprising at least some C 4 hydrocarbons and a bottom stream comprising (a) primarily the solvent and (b) some C 4 hydrocarbons;
separating the bottom stream in a degasser column to produce a lean solvent stream comprising primarily the solvent;

wherein a reboiler for the rectifier column comprises four or more heat exchangers in series, wherein at least three of the heat exchangers are operated using the lean solvent stream as a heating medium, and wherein a last heat exchanger of the four or more heat exchangers in series is operated using low pressure steam as a heating medium;
wherein the degasser column is operated at an overhead boiling temperature range of 85 to 100° C.; and
wherein the method further comprises steps of:
flowing the lean solvent stream to at least one of the four or more heat exchangers as a heating medium for the reboiler to heat a rectifier feed stream to produce a first cooled lean solvent stream and a heated rectifier feed stream; and
flowing the low pressure steam to the last heat exchanger of the four or more heat exchangers as a heating medium to heat the reboiler to heat the heated rectifier feed stream and produce a further heated rectifier feed stream.

2. The method of claim 1 , wherein the mixture of C 4 hydrocarbons and the solvent is produced by a step of separating, in a main washer column, a C 4 hydrocarbon feed stream via extractive distillation to produce (i) a first overhead stream comprising 1-butene, 2-butene, isobutylene, isobutane, n-butane, or combinations thereof, and (ii) the mixture of C 4 hydrocarbons and the solvent comprising primarily a mixture of 1,3-butadiene, the solvent, and C 4 hydrocarbons other than 1,3-butadiene.

3. The method of claim 1 , wherein the separating of the mixture of C 4 hydrocarbons and the solvent in the rectifier column further produces a first side stream comprising 1,3-butadiene and acetylenes.

4. The method of claim 3 , further comprising separating the first side stream in an after washer column to produce a crude butadiene stream comprising primarily 1,3-butadiene.

5. The method of claim 1 , wherein the separating of the bottom stream in the degasser column further produces a second side stream comprising acetylene.

6. The method of claim 5 , further comprising separating the second side stream in an acetylene column to produce a purified acetylene stream.

7. The method claim 1 , wherein the first cooled lean solvent stream is provided as a heating medium to one or more of: i) a reboiler of a propyne column for purifying propyne from the crude butadiene stream, ii) a reboiler of a refining column for purifying 1,3-butadiene from the crude butadiene stream, and/or iii) a feed evaporator for the main washer column.

8. The method of claim 7 , wherein the first cooled lean solvent stream is provided as a heating medium to all of the reboiler of the propyne column, the reboiler of the refining column, and the feed evaporator for the main washer column, such the first cooled lean solvent stream flows through the reboiler of the propyne column, the reboiler of the refining column, and the feed evaporator for the main washer column in series.

9. The method of claim 1 , wherein the temperature of the reboiler for the rectifier column is in a range of 100 to 125° C.

10. The method of claim 1 , wherein the separating of the bottom stream in the degasser column further produces a second overhead stream comprising C 4 hydrocarbons.

11. The method of claim 10 , wherein the second overhead stream is flowed to the rectifier column.

12. The method of claim 1 , wherein the C 4 hydrocarbons in the mixture of C 4 hydrocarbons and the solvent comprise 1-butene, 2-butene, n-butane, isobutane, isobutylene, 1,3-butadiene, or combinations thereof.

13. The method of claim 1 , wherein the solvent comprises N-methyl-2-pyrrolidone and 8.3 wt. % water.

14. The method of claim 1 , wherein the rectifier column is operated at an overhead boiling temperature range of 55 to 75° C., a reboiler temperature range of 100 to 125° C., and an operating pressure of 4.5 to 5.5 bara.

15. The method of claim 1 , wherein the degasser column is operated at a reboiler temperature range of 145 to 155° C.

16. The method of claim 2 , wherein the degasser column is operated at a reboiler temperature range of 145 to 155° C.

17. A method of separating a mixture of C 4 hydrocarbons and a solvent, the method comprising: separating the mixture of C 4 hydrocarbons and the solvent in a rectifier column to produce a top stream comprising at least some C 4 hydrocarbons and a bottom stream comprising (a) primarily the solvent and (b) some C 4 hydrocarbons; separating the bottom stream in a degasser column to produce a lean solvent stream comprising primarily the solvent;
wherein a reboiler for the rectifier column comprises four or more heat exchangers, wherein at least three of the heat exchangers are operated using the lean solvent stream as a heating medium, and wherein a last heat exchanger of the four or more heat exchangers in series is operated using low pressure steam as a heating medium;
wherein the rectifier column is operated at an overhead boiling temperature range of 55 to 75° C.; and
wherein the method further comprises steps of:
flowing the lean solvent stream to at least one of the four or more heat exchangers as a heating medium for the reboiler to heat a rectifier feed stream to produce a first cooled lean solvent stream and a heated rectifier feed stream; and
flowing the low pressure steam to the last heat exchanger of the four or more heat exchangers as a heating medium to heat the reboiler to heat the heated rectifier feed stream and produce a further heated rectifier feed stream.

Assignees

• Sabic Global Technologies Bv

Inventors

• Alshehri Ahmad Mahdi
• Abdelghani Mohammed Sabri
• Alzenaidi Ahmed

Classifications

• C07C11/24

  Acetylene (production of acetylene gas by wet methods C10H) · CPC title

• C07C11/22

  containing carbon-to-carbon triple bonds · CPC title

• C07C11/167

  1, 3-Butadiene · CPC title

• C07C9/10

  with four carbon atoms · CPC title

• B01D3/40

  Extractive distillation · CPC title