Separation of off gases from C3 hydrocarbons in propane dehydrogenation process

Patent metadata

Field	Value
Publication number	US-10787402-B2
Application number	US-201716075004-A
Country	US
Kind code	B2
Filing date	Apr 13, 2017
Priority date	Apr 15, 2016
Publication date	Sep 29, 2020
Grant date	Sep 29, 2020

Abstract

Methods and systems for separating C3 hydrocarbons from lighter hydrocarbons, carbon monoxide, carbon dioxide, and water are provided. In certain embodiments, the methods include feeding a gaseous mixture including C1, C2, and C3 hydrocarbons and benzene solvent to the absorber column where benzene solvent selectively absorbs C3 hydrocarbons. The methods can further include removing a first stream comprising benzene solvent and absorbed C3 hydrocarbons from the absorber column, and feeding the first stream to a stripper column where benzene solvent is separated from C3 hydrocarbons, and removing a second stream comprising C3 hydrocarbons from the stripper column.

First claim

The invention claimed is:

1. A method for separating C 3 hydrocarbons from a gaseous mixture, the method comprising:
(a) feeding the gaseous mixture comprising C 1 hydrocarbons, C 2 hydrocarbons, and C 3 hydrocarbons to an absorber column;
(b) feeding benzene solvent to the absorber column, wherein benzene solvent selectively absorbs C 3 hydrocarbons;
(c) removing a first stream comprising benzene solvent and absorbed C 3 hydrocarbons from the absorber column;
(d) feeding the first stream to a stripper column where benzene solvent is separated from C 3 hydrocarbons; and
(e) removing a second stream comprising C 3 hydrocarbons from the stripper column;
wherein the benzene solvent is in concurrent contact with the gaseous mixture; and
wherein the gaseous mixture further comprises at least one member selected from the group consisting of carbon monoxide, carbon dioxide and water.

2. The method of claim 1 , wherein the gaseous mixture further comprises carbon monoxide.

3. The method of claim 1 , wherein the wherein the gaseous mixture further comprises carbon dioxide.

4. The method of claim 1 , wherein the gaseous mixture further comprises water.

5. The method of claim 1 , wherein the weight ratio of the benzene solvent fed to the absorber column to the gaseous mixture fed to the absorber column is 4:1 (ton/ton).

6. The method of claim 1 , further comprising removing a third stream comprising C 1 and C 2 hydrocarbons from the absorber column.

7. The method of claim 6 , further comprising removing a fourth stream comprising benzene solvent from the stripper column.

8. The method claim 7 , further comprising feeding the fourth stream to the absorber column.

9. The method of claim 1 , further comprising feeding the second stream to a C 3 stripper column to separate propane from propylene.

10. The method of claim 1 , wherein the weight ratio of the benzene solvent fed to the absorber column to the gaseous mixture fed to the absorber column is 3:1 (ton/ton).

11. The method of claim 1 , wherein the weight ratio of the benzene solvent fed to the absorber column to the gaseous mixture fed to the absorber column is from about 3:1 to about 4:1 (ton/ton).

12. The method of claim 1 , wherein the pressure of the absorber column is maintained at a pressure of from about 23 bar to about 24 bar.

13. The method of claim 1 , wherein the pressure of the stripper column is maintained at a pressure of from about 22 bar to about 23 bar.

14. The method of claim 1 , wherein the temperature of the top of the absorber column is maintained at a temperature of from about 7° C. to about 8° C.

15. The method of claim 1 , wherein the temperature of the bottom of the absorber column is maintained at a temperature of from about 100° C. to about 150° C.

16. The method of claim 1 , wherein the temperature of the top of the stripper column is maintained at a temperature of from about 50° C. to about 60° C.

17. The method of claim 1 , wherein the temperature of the bottom of the stripper column is maintained at a temperature of from about 220° C. to about 230° C.

18. The method of claim 1 , wherein the weight ratio of the benzene solvent fed to the absorber column to the gaseous mixture fed to the absorber column is 3.6:1 (ton/ton).

19. A method for separating C 3 hydrocarbons from a gaseous mixture, the method consisting of the steps of:
(a) feeding the gaseous mixture consisting of methane, ethane, ethylene, carbon monoxide, carbon dioxide, and C 3 hydrocarbons to an absorber column;
(b) feeding benzene solvent to the absorber column, wherein benzene solvent selectively absorbs C 3 hydrocarbons;
(c) removing a first stream comprising benzene solvent and absorbed C 3 hydrocarbons from the absorber column;
(d) feeding the first stream to a stripper column where benzene solvent is separated from C 3 hydrocarbons; and
(e) removing a second stream comprising C 3 hydrocarbons from the stripper column;
wherein the benzene solvent is in concurrent contact with the gaseous mixture;
wherein the temperature of the top of the stripper column is maintained at a temperature of 60° C.;
wherein the temperature of the bottom of the stripper column is maintained at a temperature of 230° C.;
wherein the temperature of the top of the absorber column is maintained at a temperature of 8° C.;
wherein the pressure of the absorber column is maintained at a pressure of 24 bar; and
wherein the pressure of the stripper column is maintained at a pressure of 23 bar.

20. A method for separating C 3 hydrocarbons from a gaseous mixture, the method consisting of the steps of:
(a) feeding the gaseous mixture consisting of methane, ethane, ethylene, carbon monoxide, carbon dioxide, and C 3 hydrocarbons to an absorber column;
(b) feeding benzene solvent to the absorber column, wherein benzene solvent selectively absorbs C 3 hydrocarbons;
(c) removing a first stream comprising benzene solvent and absorbed C 3 hydrocarbons from the absorber column;
(d) feeding the first stream to a stripper column where benzene solvent is separated from C 3 hydrocarbons; and
(e) removing a second stream comprising C 3 hydrocarbons from the stripper column;
wherein the benzene solvent is in concurrent contact with the gaseous mixture;
wherein the temperature of the top of the stripper column is maintained at a temperature of 50° C.
wherein the temperature of the bottom of the stripper column is maintained at a temperature of 220° C.;
wherein the temperature of the top of the absorber column is maintained at a temperature of 7° C.;
wherein the pressure of the absorber column is maintained at a pressure of 23 bar; and
wherein the pressure of the stripper column is maintained at a pressure of 22 bar.

Assignees

• Sabic Global Technologies Bv

Inventors

• Kommuri Subba Rao
• Abdelghani Mohamed Sabri

Classifications

• C07C7/04

  by distillation · CPC title

• C10G2300/4081

  Recycling aspects · CPC title

• C10G7/00

  Distillation of hydrocarbon oils · CPC title

• B01D53/1493

  Selection of liquid materials for use as absorbents · CPC title

• B01D2257/7022

  Aliphatic hydrocarbons · CPC title