METHOD OF SEPARATING LINEAR ALPHA OLEFINS

• US 20190322604A1
• Filed: 12/19/2017
• Published: 10/24/2019
• Est. Priority Date: 12/20/2016
• Status: Abandoned Application

• Current Assignee: SABIC Global Technologies BV (Government of Saudi Arabia)
• Original Assignee: SABIC Global Technologies BV (Government of Saudi Arabia)
• Inventors: Alhasmi, Khalid Mohammed, Rallapalli, Jagan
• Application Number:
  US16/471,100
• Publication Number:
  US 20190322604A1
• Time in Patent Office: Days
• CPC Class Codes: B01D 3/00 Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping evaporation in general, e.g. of liquids for gas phase reactions B01B1/005; gas chromatography B01D15/08; destructive distillation C10B; preparation of alcoholic beverages by distillation C12H6/02
• CPC Class Codes: B01D 3/143 by two or more of a fractionation, separation or rectification step
• CPC Class Codes: B01D 3/322 Reboiler specifications
• CPC Class Codes: C07C 11/02 Alkenes
• CPC Class Codes: C07C 7/04 by distillation
• CPC Class Codes: C07C 7/08 by extractive distillation

Abstract

A method of separating linear alpha olefins includes: passing a feed stream comprising linear alpha olefins through a first column; distributing a C10− fraction to a top portion of the first column; distributing a C12− fraction to a bottom portion of the first column; withdrawing the C10− fraction from the top portion of the first column; passing the C10− fraction through a second column; distributing a C8 fraction to a top portion of the second column; and distributing a C10 fraction to a bottom portion of the second column; wherein any fraction withdrawn from the top portion of the first column is further separated into greater than or equal to two fractions.

Claims

1. A method of separating linear alpha olefins, comprising:

passing a feed stream comprising linear alpha olefins through a first column;

distributing a C10−

fraction to a top portion of the first column;

distributing a C12+ fraction to a bottom portion of the first column;

withdrawing the C10−

fraction from the top portion of the first column;

passing the C10−

fraction through a second column;

distributing a C8 fraction to a top portion of the second column; and

distributing a C10 fraction to a bottom portion of the second column;

wherein any fraction withdrawn from the top portion of the first column is further separated into greater than or equal to two fractions.

2. The method of claim 1, wherein the source of the feed stream is the product of an ethylene oligomerization process.

3. The method of claim 1, wherein the source of the feed stream is the product of a C4/C6 separation column.

4. The method of claim 1, wherein the feed stream comprises C4 to C20 linear alpha olefins.

5. The method of claim 1, wherein the C10 fraction comprises decene.

6. The method of claim 5, wherein the C10 fraction comprises greater than or equal to 99% decene.

7. The method of claim 6, wherein the C10 fraction comprises greater than or equal to 99.9% decene.

8. The method of claim 1, wherein the C8 fraction comprises octene.

9. The method of claim 8, wherein the C8 fraction comprises greater than or equal to 99% octene.

10. The method of claim 9, wherein the C8 fraction comprises greater than or equal to 99.9% octene.

11. The method of claim 1, wherein the first and/or second column comprises a reboiler and/or a condenser.

12. The method of claim 11, wherein a total reboiler duty is less than or equal to 1350 kilowatts.

13. The method of claim 11, wherein a total condenser duty is less than or equal to 1300 kilowatts.

14. The method of claim 11, wherein a total reboiler duty is reduced by greater than or equal to 20% as compared to a direct method of linear alpha olefin separation.

15. The method of claim 11, wherein a total condenser duty is reduced by greater than or equal to 20% as compared to a direct method of linear alpha olefin separation.

16. The method of claim 1, wherein a total amount of energy consumed by the method is reduced by greater than or equal to 20.5% as compared to a direct method of linear alpha olefin separation.

17. The method of claim 1, wherein the feed stream comprises ethylene.

18. The method of claim 1, further comprising withdrawing the C12+ fraction from the bottom portion of the first column, withdrawing the C8 fraction from the top portion of the second column, withdrawing the C10 fraction from the bottom portion of the second column, or a combination comprising at least one of the foregoing.

19. The method of claim 1, further comprising passing the C12+ fraction through a third column.

20. A method of separating linear alpha olefins, comprising:

passing a feed stream comprising C4 to C20 linear alpha olefins through a first column, wherein the source of the feed stream is the product of an ethylene oligomerization process;

distributing a C10−

fraction to a top portion of the first column;

distributing a C12+ fraction to a bottom portion of the first column;

withdrawing the C10−

fraction from the top portion of the first column;

passing the C10−

fraction through a second column;

distributing a C8 fraction to a top portion of the second column, wherein the C8 fraction comprises greater than or equal to 99.9% octene; and

distributing a C10 fraction to a bottom portion of the second column, wherein the C10 fraction comprises greater than or equal to 99.9% decene;

wherein a total reboiler duty is less than or equal to 1350 kilowatts, wherein a total condenser duty is less than or equal to 1300 kilowatts, and wherein a total amount of energy consumed by the method is reduced by greater than or equal to 20.5% as compared to a direct method of linear alpha olefin separation,

wherein any fraction withdrawn from the top portion of the first column is further separated into greater than or equal to two fractions.