Integrated process for producing anode grade coke

Patent metadata

Field	Value
Publication number	US-9909068-B2
Application number	US-201615219730-A
Country	US
Kind code	B2
Filing date	Jul 26, 2016
Priority date	Aug 4, 2015
Publication date	Mar 6, 2018
Grant date	Mar 6, 2018

Abstract

The invention relates to processes for producing anode grade coke from whole crude oil. The invention is accomplished by first deasphalting a feedstock, followed by processing resulting DAO and asphalt fractions. The DAO fraction is hydrotreated or hydrocracked, resulting in removal of sulfur and hydrocarbons, which boil at temperatures over 370° C., and gasifying the asphalt portion in one embodiment. This embodiment includes subjecting hydrotreated and/or unconverted DAO fractions to delayed coking. In an alternate embodiment, rather than gasifying the asphalt portion, it is subjected to delayed coking in a separate reaction chamber. Any coke produced via delayed coking can be gasified.

First claim

The invention claimed is:

1. A method for producing anode grade coke, comprising:
(i) solvent deasphalting a hydrocarbon feedstock to produce an asphalt fraction and a deasphalted oil (DAO) fraction, in a first reaction chamber;
(ii) processing said DAO fraction and asphalt fraction in separate, second, third, and fourth reaction chambers;
(iii) hydrocracking said DAO fraction in said second reaction chamber at a pressure of from 100-200 bars, a temperature of from 350° C. to 450° C., an LHSV of from 0.1 to 4.0 h −1 , and a hydrogen:DAO ratio of from 500-2,500 SLt/Lt to remove sulfur and nitrogen therefrom and to distill any hydrocarbons contained in said DAO which have a boiling point over 370° C.;
(iv) subjecting any hydrotreated or unconverted DAO fraction to delayed coking in a third chamber, and
(v) gasifying said asphalt fraction via combining it with oxygen and steam, in said fourth reaction chamber, to produce hydrogen therefrom.

2. The method of claim 1 , further comprising gasifying any coke produced in step (iv).

3. The method of claim 1 , comprising introducing any hydrogen produced in said third reaction chamber into said second reaction chamber.

4. The method of claim 1 , wherein said hydrocarbon feedstock is crude oil and said solvent deasphalting comprises mixing said crude oil with a paraffinic solvent containing C 3 -C 7 carbon atoms, at a temperature and a pressure below critical temperature and critical pressure of said solvent.

5. The method of claim 4 , wherein said solvent comprises n-butane and isobutane.

6. The method of claim 1 , further comprising contacting said hydrocarbon feedstock with a solid adsorbent.

7. The method of claim 1 , wherein said hydrocarbon feedstock is crude oil and said solvent deasphalting comprises mixing said crude oil and solvent at a temperature and pressure below the critical temperature and critical pressure of said solvent.

8. The method of claim 4 , wherein said crude oil and solvent are combined at a weight ratio of from 10:1 to 200:1 w/w.

9. The method of claim 1 , comprising hydrocracking said DAO in a series of multiple chambers.

10. The method of claim 1 , wherein said second reaction chamber is a fixed bed, ebullated bed, or slurry bed chamber.

11. The method of claim 1 , comprising hydrocracking said DAO in the presence of a catalyst, which contains from 2-40 wt % active metal, a pore volume of from 0.33-1.50 cc/gm, a surface area of 250-450 m 2 /g, and an average pore diameter of at least 50 Angstroms.

12. The method of claim 11 , wherein said active metal is a Group VI, VII, or VIIIB metal.

13. The method of claim 11 , wherein said active metal comprises Co, Ni, W, or Mo.

14. The method of claim 11 , wherein said catalyst is presented on a support.

15. The method of claim 14 , wherein said support comprises alumina, silica, or a zeolite.

16. The method of claim 15 , wherein said support is a zeolite with FAU, MOR, BEA or MFI topology.

17. The method of claim 16 , wherein said zeolite has been modified by treatment with at least one of steam, ammonia, or acid, and contains at least one transition metal.

18. The method of claim 17 , wherein said at least one transition metal is Zn or Ti.

19. The method of claim 1 , comprising gasifying said asphalt fraction at a temperature of from 900° C. to 1700° C., and a pressure of from 20 bars to 100 bars.

20. The method of claim 1 , further comprising adjusting the amount of asphalt and at least one of oxygen and steam in said fourth reaction chamber to provide a stoichiometric balance therebetween which results in partial combustion of said asphalt.

21. The method of claim 19 , wherein said stoichiometric ratio based on the oxygen:carbon ratio is from 0.2:1:0 to 10:0.2 by weight.

22. The method of claim 19 , comprising introducing asphalt and steam to said fourth reaction chamber in a ratio of from 0.1 to 1.0 to 10:0.1 based upon weight of carbon in said crude oil.

23. A process for producing anode grade coke, comprising:
(i) solvent deasphalting a hydrocarbon feedstock to produce an asphalt fraction and a deasphalted oil (DAO) fraction, in a first reaction chamber,
(ii) processing said DAO fraction and asphalt fraction in separate, second, third, and fourth reaction chambers;
(iii) hydrocracking said DAO fraction in said second reaction chamber at a pressure of from 100-200 bars, a temperature of from 350° C. to 450° C., an LHSV of from 0.1 to 4.0 h −1 , and a hydrogen:DAO ratio of from 500-2,500 SLt/Lt to remove sulfur and nitrogen therefrom and to distillate any hydrocarbons contained in said DAO which have a boiling point over 370° C.;
(iv) subjecting any hydrotreated or unconverted DAO fraction to delayed coking in a third chamber, and either
(v) oxidizing said asphalt fraction in said fourth reaction chamber, to produce higher grade asphalt or
(vi) subjecting said asphalt fraction to delayed coking in said third reaction chamber to produce fuel grade coke.

Assignees

• Saudi Arabian Oil Co

Inventors

• Koseoglu Omer Refa

Classifications

• C10G45/02

  to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing · CPC title

• C10G25/00

  Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents · CPC title

• C10G9/005

  Coking (in order to produce liquid products mainly) · CPC title

• C10B55/00 Primary

  Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material (cracking oils C10G) · CPC title

• C10G2300/1055

  Diesel having a boiling range of about 230 - 330 °C · CPC title