Improvements relating to coal to liquid processes

Patent metadata

Field	Value
Publication number	US-9624445-B2
Application number	US-8977406-A
Country	US
Kind code	B2
Filing date	Oct 13, 2006
Priority date	Oct 14, 2005
Publication date	Apr 18, 2017
Grant date	Apr 18, 2017

Abstract

Process for preparing a hydrocarbon product from a solid carbonaceous fuel ( 8 ), the process at least comprising the steps of: (a) supplying a solid carbonaceous fuel ( 8 ) and an oxygen containing stream ( 9 ) to a burner of a gasification reactor ( 10 ), wherein a CO 2 containing transport gas ( 30, 32 ) is used to transport the solid carbonaceous fuel ( 8 ) to the burner wherein the weight ratio of CO 2 to the carbonaceous fuel in step (a) is less than 0.5 on dry basis.; (b) partially oxidising the carbonaceous fuel in the gasification reactor, thereby obtaining a gaseous stream at least comprising CO, CO 2 , and H 2 ( 11 ); (c) removing the gaseous stream obtained in step (b) from the gasification reactor; (d) optionally shift converting ( 16 ) at least part of the gaseous stream as obtained in step (c) thereby obtaining a CO depleted stream, (e) subjecting the gaseous stream of step (c) and/or the optional CO depleted stream of step (d) to a Fischer-Tropsch reaction to obtain a hydrocarbon product ( 24 ).

First claim

What is claimed is:

1. A process for preparing a hydrocarbon product from a solid carbonaceous fuel, the process comprising the steps of:
(a) supplying a solid carbonaceous fuel and an oxygen containing stream to a burner of a gasification reactor, wherein a CO 2 containing transport gas is used to transport the solid carbonaceous fuel to the burner wherein the weight ratio of CO 2 to the carbonaceous fuel in step (a) is less than 0.3 on a dry basis;
(b) partially oxidising the carbonaceous fuel in the gasification reactor, thereby obtaining a gaseous stream comprising CO, CO 2 , and H 2 ;
(c) removing the gaseous stream obtained in step (b) from the gasification reactor;
(d) optionally shift converting at least part of the gaseous stream as obtained in step (c) thereby obtaining a CO depleted stream; and
(e) subjecting the gaseous stream of step (c) and/or the optional CO depleted stream of step (d) to a Fischer-Tropsch reaction to obtain a hydrocarbon product.

2. The process according to claim 1 , wherein the CO 2 containing stream supplied in step (a) is supplied at a velocity of less than 20 m/s.

3. The process according to claim 1 , wherein the weight ratio in step (a) is in the range from 0.12-0.2.

4. The process according to claim 1 , wherein the gaseous stream obtained in step (c) comprises from 1 to 10 mol % CO 2 on a dry basis.

5. The process according to claim 1 , wherein the solid carbonaceous fuel is coal.

6. The process according to claim 1 , wherein the process further comprises the step of subjecting the CO depleted stream as obtained in step (d) to a CO 2 recovery system thereby obtaining a CO 2 rich stream and a CO 2 poor stream and wherein the CO 2 poor stream is used in step (e).

7. The process according to claim 6 , wherein the CO 2 recovery system is a combined carbon dioxide/hydrogen sulfide removal system wherein methanol is the physical solvent.

8. The process according to claim 6 , wherein the CO 2 rich stream is at least partially used as the CO 2 containing transport gas in step (a).

9. The process according to claim 1 , wherein the H 2 /CO ratio in the gaseous stream obtained in step (b) is less than 1.

10. The process according to claim 1 , wherein the H 2 /CO ratio of the CO depleted stream is between 1.4 and 1.95.

11. The process according to claim 10 , wherein the gaseous stream obtained in step (b) is divided into at least two sub-streams, one of which undergoes step (d) to obtain a first CO depleted stream and wherein the first CO depleted stream is combined with the second sub-stream to form a second CO depleted stream.

12. The process according to claim 11 , wherein the ratio of the sub-stream which undergoes step (d) and the sub-stream which does not undergo step (d) is in the range 70:30 to 30:70 by volume.

13. A method as claimed in claim 1 , wherein up to 10% by volume of the CO depleted stream is used for hydrogen manufacture.

14. The process according to claim 1 , wherein step (e) is performed by an iron catalyzed Fischer-Tropsch synthesis reaction performed in a slurry phase reactor.

15. The process according to claim 1 , wherein step (e) is performed by a multi-stage Fischer-Tropsch process.

16. The process according to claim 15 , wherein part of the CO depleted stream is used as additional feed for the further stages in the Fischer-Tropsch process.

17. The process according to claim 1 , wherein the hydrocarbon product obtained in step (e) is subjected to a hydroprocessing step to obtain a middle distillate fuel.

18. The process according to claim 17 , wherein the hydrogen made from part of the CO depleted stream is used in the hydroprocessing step.

19. The process according to claim 1 , wherein the weight ratio in step (a) is in the range from 0.14-0.29.

20. The process according to claim 1 , wherein the weight ratio in step (a) is less than 0.2.

21. The process according to claim 1 , wherein the weight ratio in step (a) is less than or equal to 0.14.

Assignees

• Van Den Berg Robert Erwin
• Van Montfort Johannes Margaretha Anna Joan
• Scheerman Jacobus Hendrikus
• Schilder Johannes Gerardus Maria
• Shell Oil Co

Inventors

• Van Den Berg Robert Erwin
• Van Montfort Johannes Margaretha Anna Joan
• Scheerman Jacobus Hendrikus
• Schilder Johannes Gerardus Maria

Classifications

• C10J2300/1807

  Recycle loops, e.g. gas, solids, heating medium, water · CPC title

• C10K3/06

  by mixing with gases · CPC title

• C10J2300/0903

  Feed preparation · CPC title

• C10J3/506

  for entrained flow gasifiers · CPC title

• C10J2300/0943

  Coke · CPC title