PRODUCTION OF HYDROCARBONS

• US 20120228148A1
• Filed: 11/04/2010
• Published: 09/13/2012
• Est. Priority Date: 11/04/2009
• Status: Active Grant

• Current Assignee: FFGF Limited
• Original Assignee: FFGF Limited
• Inventors: Wolfowitz, Steven Alan
• Granted Patent: US 9,469,910 B2
• Time in Patent Office: Days
• US Class Current: 205/462
• CPC Class Codes: C25B 15/08 Supplying or removing reactants or electrolytes; Regeneration of electrolytes
• CPC Class Codes: C25B 3/25 Reduction
• CPC Class Codes: C25B 9/00 Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
• CPC Class Codes: C25B 9/19 with diaphragms

Abstract

This invention relates to a method for the production of hydrocarbons from carbon dioxide and water, using electrolysis and two separate reaction vessels. A first reaction vessel (14) contains a positive electrode and a liquid electrolytic medium comprising water and ionized material. A second reaction vessel (12) contains a negative electrode and a liquid electrolytic medium comprising a mixture of water and carbon dioxide. The reaction vessels are connected with connection means which allow ions to pass between the electrolytic media of the first and second reaction vessels. A direct electrical current is applied to the positive electrode and the negative electrode to produce hydrocarbons (typically methane); and oxygen.

Claims

1. A method for the production of hydrocarbons from carbon dioxide and water includes the steps of:

(e) providing a first reaction vessel (14) containing a positive electrode and a liquid electrolytic medium comprising water and ionizing material;

(f) providing a second reaction vessel (12) containing a negative electrode and a liquid electrolytic medium comprising a mixture of water and carbon dioxide;

(g) connecting the first and second reaction vessels with connection means which allows electrons and/or ions to pass between the electrolytic media of the first and second reaction vessels;

(h) applying a direct electrical current to the positive electrode and the negative electrode to;

cause electrons to flow from the cathode to the anode, through the electrolytic media in the reaction vessels (12) and (14);

form hydrocarbons in the reaction vessel (12).

2. The method as claimed in claim 1, wherein the hydrocarbons includes methane.

3. The method as claimed in claim 1, wherein oxygen is formed in the reaction vessel (14).

4. The method as claimed in claim 1, wherein hydrocarbons are recovered from the second reaction vessel (12).

5. The method as claimed in claim 3, wherein oxygen is recovered from the first reaction vessel (14).

6. The method as claimed in claim 1, wherein the reaction vessels (12) and (14) are operated at the same internal pressure.

7. The method as claimed in claim 1, wherein the reaction vessels (12) and (14) are operated at different temperatures.

8. The method as claimed in claim 1, wherein the connection means is a liquid electrolytic medium.

9. The method as claimed in claim 1, wherein the connection means includes a membrane which allows electrons to pass through, and possibly some ions, but not atoms.

10. The method as claimed in claim 1, wherein the connection means is defined by one or more tube/s.

11. The method as claimed in claim 10, wherein the tube/s is/are capillary tube/s.

12. The method as claimed in claim 1, wherein the connection means is provided with stopper means.

13. The method as claimed in claim 12, wherein the stopper means is a valve or valves.

14. The method as claimed in claim 10, wherein the ratio of internal diameter to length of the/each tube is from 0.00001:

1 to 0.1;

1.

15. The method as claimed in claim 14, wherein the ratio of internal diameter to length of the/each tube is from 0.00001:

1 to 0.001;

1

16. The method as claimed in claim 1, wherein the positive electrode in the first reaction vessel (14) is in the form of a hollow microporous cylinder which is closed at one end and which is made of Pt.

17. The method as claimed in claim 1, wherein the negative electrode in the second reaction vessel (12) is in the form of a hollow microporous cylinder which is closed at one end and which is made from a CuPt amalgam or Pt.

18. The method as claimed in claim 1, wherein the electrolytic media in the first (14) and second reaction (12) vessels is kept in a liquid state by operating the vessels (12) and (14) under a suitable pressure and temperature conditions.

19. The method as claimed in claim 1, wherein the first (14) and second reaction (12) vessels are operated at a pressure of above 5.1 atm.

20. The method as claimed in claim 19, wherein the first (14) and second reaction (12) vessels are operated at a pressure of from 5.1 to 1000 atm.

21. The method as claimed in claim 20, wherein the first (14) and second reaction (12) vessels are operated at a pressure of from 10 atm to 400 atm.

22. The method as claimed in claim 21, wherein the first (14) and second reaction (12) vessels are operated at a pressure of from 10 to 200 atm.

23. The method as claimed in claim 1, wherein the reaction vessels (12) and 14) are operated at different temperatures.

24. The method as claimed in claim 1, wherein the first reaction vessel (14) is operated at a temperature of 20°

C. to 200°

C.

25. The method as claimed claim 24, wherein the first reaction vessel (14) is operated at a temperature of 20°

C. to 200°

C.

26. The method as claimed claim 25, wherein the first reaction vessel (14) is operated at a temperature of from 20°

C. to 30°

C.

27. The method as claimed in claim 1, wherein the second reaction vessel (12) is operated at a temperature of −

50°

C. to 200°

C.

28. The method as claimed in claim 27, wherein the second reaction vessel (12) is operated at a temperature of −

10°

C. to 70°

C.

29. The method as claimed in claim 1, wherein the first reaction vessel (14) is operated at ambient temperature (10°

C. to 30°

C.).

30. The method as claimed in claim 29, wherein the temperature of the second reaction vessel is controlled to a desired temperature.

31. The method as claimed in claim 30, wherein the desired temperature is from −

50°

C. to 10°

C.

32. The method as claimed in claim 30, wherein the desired temperature is from 10°

C. to 200°

C.

33. The method as claimed in claim 1, wherein the voltage applied across the positive electrode and the negative electrode is from −

0.5v to −

20v.

34. The method as claimed in claim 33, wherein the voltage applied across the positive electrode and the negative electrode is from −

0.5v to −

10v.

35. The method as claimed in claim 34, wherein the voltage applied across the positive electrode and the negative electrode is from −

0.5v to −

6v.

36. The method as claimed in claim 35, wherein the voltage applied across the positive electrode and the negative electrode is from −

0.5v to −

3v.

37. The method as claimed in claim 1, wherein the direct current applied across the positive electrode and the negative electrode is from 50 to 500 mA.

38. The method as claimed in claim 37, wherein the direct current applied across the positive electrode and the negative electrode is from 100 to 200 mA.

39. The method as claimed in claim 1, wherein the positive electrode and the negative electrode are a grid of multiple electrodes wired in parallel and the direct current applied across the electrodes is 0.1 to 10 amp.

40. The method as claimed in claim 1, wherein carbon dioxide and water in the second reaction vessel (12) are mixed at a volumetric ratio of 1:

1 to 1;

2 or in stoichiometric (or greater) proportions according to the formula;

CO₂+2H₂O→

CH₄+20₂.

41. The method as claimed in claim 1, wherein carbon dioxide, water and carbon monoxide are separated from the electrolytic medium of the second reaction vessel (20), and recycled to the second reaction vessel (12).

42. The method as claimed in claim 1, wherein water is separated from the electrolytic medium of the first reaction vessel (14) and recycled to the second reaction vessel (12).

43. An apparatus for the production of hydrocarbons from carbon dioxide and water, the apparatus comprising:

a first reaction vessel (14) for containing water in the liquid phase;

a second reaction vessel (12) for containing a mixture of carbon dioxide and water in the liquid phase;

a positive electrode located within the first reaction vessel (14);

a negative electrode located within the second reaction vessel (12);

and connection means connecting electrolytic media in the first and second reaction vessels (14) and (12).

44. The apparatus as claimed in claim 43, wherein the connection means is a liquid electrolytic medium.

45. The apparatus as claimed in claim 44, wherein the connection means includes a membrane which allows electrons to pass through, and possibly some ions, but not atoms.

46. The apparatus as claimed in claim 43, wherein the connection means is defined by one or more tube/s.

47. The apparatus as claimed in claim 46, wherein the tube/s is/are capillary tube/s.

48. The apparatus as claimed in claim 43, wherein the connection means is provided with stopper means.

49. The apparatus as claimed in claim 48, wherein the stopper means is a valve or valves.

50. The apparatus as claimed in claim 46, wherein the ratio of internal diameter to length of the/each tube is from 0.00001:

1 to 0.1;

1.

51. The apparatus as claimed in claim 50, wherein the ratio of internal diameter to length of the/each tube is from 0.00001:

1 to 0.001;

1.

52. The apparatus as claimed in claim 43, including a high pressure intensifier for equalizing the pressures in both reaction vessels (12) and (14).

53. The apparatus as claimed in claim 52, wherein the high pressure intensifier is pressurized with CO₂, and pressurizes the second reaction vessel (12) directly with CO₂, and a high pressure accumulator is provided for pressurizing the first reaction vessel (14) with H₂O.