阅读说明：本技术 灵活性的热解系统和方法 (Flexible pyrolysis system and process ) 是由 本杰明·L·古德里奇 乔舒亚·C·沃尔特 于 2018-04-11 设计创作，主要内容包括：提供了灵活性热解系统的实例,其包括能够在超临界二氧化碳(CO<Sub>2</Sub>)气氛中热解煤的组合的至少一个反应室。该系统包括同流换热和冷凝回路,该回路从超临界CO<Sub>2</Sub>气氛中移除溶解的热解产物,并且然后回收CO<Sub>2</Sub>以在反应室中再利用。同流换热和冷凝回路包括多级同流换热器和收集器,所述多级同流换热器和收集器可以被独立地控制,以便选择性地分馏热解产物。此外,可以控制热解反应以改变产生的热解产物。(Examples of flexible pyrolysis systems are provided, including the ability to be in supercritical carbon dioxide (CO) 2 ) At least one reaction chamber for pyrolyzing a combination of coal in an atmosphere.The system includes a recuperation and condensing loop that is driven from supercritical CO 2 Removing dissolved pyrolysis products in an atmosphere and then recovering CO 2 For reuse in the reaction chamber. The recuperator and condenser circuits include multiple stages of recuperators and collectors that can be independently controlled to selectively fractionate pyrolysis products. In addition, the pyrolysis reaction can be controlled to alter the pyrolysis products produced.)

1. A method, comprising:

pyrolyzing a combination of carbonaceous feedstocks at a first temperature and a first pressure and for a first period of time to produce C₁-C₄A gas;

raising the combination to a second temperature higher than the first temperature;

pyrolyzing the combination at the second temperature and for a second period of time to produce pitch; and

extracting bitumen from said combination.

2. The method of claim 1, further comprising:

carbon fibers are made from the pitch.

3. The process of claim 1 or 2, wherein the first temperature is from 150 ℃ to 350 ℃ and the first pressure is from 7MPa to 30 MPa.

4. The method of claim 1 or 2, wherein the second temperature is from 350 ℃ to 550 ℃.

5. The method of claim 1 or 2, wherein the length of the first time period is from 1 minute to 120 minutes.

6. The process of claim 1 or 2, wherein the first time period is based on at least one C produced from the carbonaceous feedstock at the first temperature₁-C₄The amount of gas.

7. The method of claim 1 or 2, wherein the second period of time is from 1 minute to 24 hours.

8. The process of claim 1 or 2, wherein pyrolyzing the carbonaceous feedstock at the first temperature and first pressure is carried out in a first pyrolysis reaction chamber.

9. The process of claim 1 or 2, wherein pyrolyzing the carbonaceous feedstock at the second temperature is carried out in the first pyrolysis reaction chamber.

10. The method of claim 1 or 2, wherein pyrolyzing the carbonaceous feedstock at the second temperature is performed in a second pyrolysis reaction chamber different from the first pyrolysis reaction chamber.

11. The process of claim 1 or 2, wherein pyrolyzing the carbonaceous feedstock at the first temperature and first pressure is carried out in a carbon dioxide atmosphere.

12. The method of claim 1 or 2, further comprising:

monitoring one or more C's in a pyrolysis atmosphere₁-C₄The concentration of the gas.

13. The method of claim 12, wherein extracting the bitumen comprises transferring a carbon dioxide atmosphere to a separation system.

14. The method of claim 13, wherein extracting the bitumen comprises reducing at least one of a temperature or a pressure of the carbon dioxide atmosphere.

15. The method of claim 2, wherein fabricating carbon fibers from the pitch comprises extruding the pitch.

16. The method of claim 2, wherein fabricating carbon fibers from the pitch comprises preparing fibers of the pitch.

17. A method of producing bitumen from coal, comprising:

heating a combined reaction chamber containing coal to a first temperature and a first pressure in a carbon dioxide atmosphere;

maintaining the reaction chamber at the first temperature and the first pressure for a time sufficient to produce C in the atmosphere₁-C₄A first period of time for the gas;

increasing the temperature of the reaction chamber to a second temperature that is higher than the first temperature;

maintaining the reaction chamber at the second temperature for a second period of time, thereby producing at least some bitumen;

removing carbon dioxide and pitch dissolved therein from the reaction chamber after the second period of time; and

separating the pitch removed from the reaction chamber from the carbon dioxide.

18. The method of claim 17, further comprising:

fibers are made from the pitch.

19. The method of claim 17 or 18, wherein the first temperature is from 150 ℃ to 350 ℃ and the first pressure is from 7MPa to 30 MPa.

20. The method of claim 17 or 18, wherein the second temperature is from 350 ℃ -550 ℃.

21. The method of claim 17 or 18, wherein the length of the first time period is from 1 minute to 120 minutes.

22. The process of claim 17 or 18, wherein the first time period is based on at least one C produced from the carbonaceous feedstock at the first temperature₁-C₄The amount of gas.

23. The method of claim 17 or 18, wherein the second time period is from 1 minute to 24 hours.

24. The method of claim 17 or 18, further comprising:

monitoring the concentration of one or more gases in the carbon dioxide atmosphere.

25. The method of claim 17 or 18, wherein removing the carbon dioxide and pitch dissolved therein from the reaction chamber comprises transferring the carbon dioxide atmosphere to a separation system.

26. The method of claim 17 or 18, wherein separating the bitumen from the carbon dioxide comprises reducing the temperature, pressure, or both of the carbon dioxide.

27. The method of claim 17 or 18, further comprising:

carbon fibers are produced using the pitch.

28. The method of claim 27, wherein producing carbon fibers using the pitch comprises extruding the pitch into fibers.

29. A system for making fibers from coal, comprising:

at least one reaction chamber capable of pyrolyzing a combination of coal in a carbon dioxide atmosphere;

a separation system configured to receive the carbon dioxide atmosphere from the reaction chamber after pyrolysis of the coal and condense pitch from the carbon dioxide into a pitch container; and

an extruder connected to the separation system, the extruder configured to receive and extrude the pitch condensed by the separation system.

30. The system of claim 29, wherein the reaction chamber is capable of heating the combination to at least 350 ℃ at a pressure from 7MPa to 30 MPa.

31. The system of claim 29 or 30, further comprising:

a heat source providing thermal energy to the reaction chamber.

32. The system of claim 29 or 30, further comprising:

a nuclear reactor providing thermal energy to the reaction chamber.

33. The system of claim 29 or 30, wherein the reaction chamber is capable of heating the carbon dioxide to a supercritical state.

34. The system of claim 29 or 30, further comprising:

a gas monitor capable of monitoring the concentration of one or more gases in the carbon dioxide atmosphere of the reaction chamber.

35. The system of claim 29 or 30, further comprising:

a valve controlling a flow of carbon dioxide from the reaction chamber to the separation system.

36. The system of claim 29 or 30, wherein the separation system comprises at least a pitch collection chamber configured to condense pitch from the carbon dioxide.

37. The system of claim 29 or 30, wherein the asphalt collection chamber is connected to the extruder.

38. A method, comprising:

reacting a carbonaceous feedstock with carbon dioxide (CO) in a supercritical state₂) Contacting at a pyrolysis temperature and pressure for a contact period of time to pyrolyze the feedstock to obtain char and supercritical CO with dissolved pyrolysis reaction products₂；

Subjecting the supercritical CO with dissolved pyrolysis reaction products₂Is separated from the char;

subjecting the supercritical CO comprising dissolved pyrolysis reaction products₂Cooling to a first stage temperature and pressure different from the pyrolysis temperature and pressure to obtain a first stage CO₂Product gas and first stage pyrolysis product condensate;

CO of the first stage₂Cooling the product gas to a second stage temperature and pressure different from the first stage temperature and pressure to obtain a second stage CO₂Product gas and second stage pyrolysis product condensate; and

reusing CO from the second stage in a subsequent pyrolysis reaction₂CO of the product gas₂At least some of.

39. The method of claim 38, further comprising:

controlling the first stage temperature and pressure to obtain a first pyrolysis reaction product in the first stage pyrolysis product condensate.

40. The method of claim 39, wherein controlling the first stage temperature further comprises:

setting the position of one or more first bypass valves to select CO entering the first recuperator₂The flow rate of the stream.

41. The method of any one of claims 38-40, further comprising:

controlling the second stage temperature and pressure to obtain a second pyrolysis reaction product in the second stage pyrolysis product condensate, the second pyrolysis reaction product being different from the first pyrolysis reaction product.

42. The method of claim 41, wherein controlling the second stage temperature further comprises:

positioning one or more second bypass valves to select CO entering the second recuperator₂The flow rate of the stream.

43. A method, comprising:

make the inlet carbon dioxide (CO) in supercritical state₂) The stream flows into a reaction chamber containing coal;

removing supercritical CO comprising dissolved pyrolysis products from the reaction chamber after a contact time₂As an outlet stream;

directing a first portion of the outlet stream through a first recuperator/collector stage to obtain a first stage CO₂An effluent stream and a first stage pyrolysis product condensate, the outlet stream being passed to the CO of the reaction chamber in the first recuperator/collector stage₂The first recuperator/collector stage comprises a recuperator followed by a condensate collector;

directing the first stage CO₂At least a portion of the effluent stream is passed through a second recuperator/collector stage to obtain a second stage CO₂An effluent stream and a second stage pyrolysis product condensate; and

by passing at least some CO₂Passing as the return stream through the first recuperator/collector stage to obtain the inlet CO₂Flow from the first stage CO₂The effluent stream or the second stage CO₂Reconditioning the at least some CO in an effluent stream₂。

44. The method of claim 43, further comprising:

directing a second portion of the outlet stream through the second recuperator/collector stage.

45. The method of claim 43 or 44, further comprising:

maintaining the reaction chamber at a temperature sufficient to maintain the reaction chamber at a temperature sufficient to remove the impuritiesCO in the reaction chamber₂Maintaining a pyrolysis temperature and pressure in a supercritical state, thereby pyrolyzing the coal to obtain char and supercritical CO comprising dissolved pyrolysis products₂。

46. The method of claim 43 or 44, wherein the inlet CO₂The temperature of the stream is from 300 ℃ to 600 ℃ and the pressure is from 7MPa to 30 MPa.

47. The method of claim 45, further comprising:

subjecting the CO to₂And at least a portion of the dissolved pyrolysis product stream flows through a third recuperator/collector stage to obtain third stage CO₂An effluent stream and a third stage pyrolysis product condensate.

48. The method of claim 47, further comprising:

subjecting the CO to₂And at least a portion of the dissolved pyrolysis product stream flows through a fourth recuperator/collector stage to obtain a fourth stage CO₂An effluent stream and a fourth stage pyrolysis product condensate.

49. The method of claim 48, further comprising:

subjecting the CO to₂And at least a portion of the dissolved pyrolysis product stream flows through a fifth recuperator/collector stage to obtain a fifth stage CO₂An effluent stream and a fifth stage pyrolysis product condensate.

50. A method according to claim 49, wherein the first, second, third, fourth and fifth recuperator/collector stages operate at different temperatures.

51. The method of claim 43 or 44, further comprising:

the different temperatures of the recuperator/collector stages are controlled by setting the position of one or more bypass valves.

52. A system for pyrolyzing coal, comprising:

at least one reaction chamber capable of being exposed to supercritical carbon dioxide (CO)₂) Pyrolyzing a combination of coal in an atmosphere;

a recuperation and condensing loop from the supercritical CO₂Removing at least some of the dissolved pyrolysis products in an atmosphere, and then recovering CO₂For re-use in the reaction chamber.

53. The system of claim 52, further comprising wherein the reaction chamber is capable of heating the combination to at least 350 ℃ at a pressure from 7MPa to 30 MPa.

54. The system of claim 52 or 53, further comprising:

a heat source that heats the CO₂Atmosphere to the CO before delivery to the reaction chamber₂The atmosphere provides thermal energy.

55. The system of claim 54, further comprising:

wherein the heat source is a nuclear reactor.

56. The system of claim 52 or 53, wherein the recuperator and condenser loop comprises one or more recuperator/collector stages, each recuperator/collector stage having a heat exchanger and a condensate collector connected to receive heat from the reaction chamber as CO₂CO of a process stream₂Atmosphere of heat from the CO₂Transfer of process stream to CO₂Return flow, and from cooled CO₂The process stream is condensed and the pyrolysis products are collected.

57. The system of claim 56, further comprising:

an additive injection system to inject one or more additives to the CO₂Return flow or in the reaction chamber.

58. The system of claim 56, further comprising:

a bypass system comprising more than one process stream bypass valve that bypasses the CO₂Distributing the flow of the process stream to the one or more recuperator/collector stages; and

a controller controlling the more than one process stream bypass valve to control the CO₂Flow of a process stream to the one or more recuperator/collector stages.

59. The system of claim 58, further comprising:

wherein the bypass system further comprises more than one return flow bypass valve that bypasses the CO₂The flow of the return stream is distributed to the one or more recuperator/collector stages; and

wherein the controller controls the more than one return flow bypass valve to control the CO₂Returning flow to the one or more recuperator/collector stages.

60. The system of any one of claims 59, wherein the controller controls the CO passing through the recuperator/condenser stage by way of the bypass system₂Process stream and said CO₂The flow of the return stream controls the condensate fraction collected by at least one of the recuperator/condenser stages.

61. The system of claim 60, wherein the controller controls the condensate fraction collected by at least one of the recuperator/condenser stages based on a predetermined target.

62. The system of claim 60, wherein the controller controls the condensate fraction collected by at least one of the recuperator/condenser stages based on information received from one or more temperature sensors that monitor temperature at one or more points in the recuperator and condenser loop.