Solids circulation system and method for capture and conversion of reactive solids having fluidized bed containing hollow engineered particles

• US 9,920,268 B2
• Filed: 11/09/2016
• Issued: 03/20/2018
• Est. Priority Date: 11/05/2010
• Status: Active Grant

• Current Assignee: Thermochem Recovery International, Inc.
• Original Assignee: Thermochem Recovery International, Inc.
• Inventors: Chandran, Ravi, Zenz, Jonathan A., Newport, Dave G., Whitney, Hamilton Sean Michael
• Primary Examiner(s): CHANDLER, KAITY V
• Application Number:
  US15/347,138
• Publication Number:
  US 20170058221A1
• Time in Patent Office: 496 Days
• CPC Class Codes: B01J 2208/00132 Tubes
• CPC Class Codes: B01J 2208/00398 inside the reactor bed
• CPC Class Codes: B01J 2208/00415 electric resistance heaters
• CPC Class Codes: B01J 2208/00752 Feeding
• CPC Class Codes: B01J 2208/00761 Discharging
• CPC Class Codes: B01J 8/004 by means of a nozzle
• CPC Class Codes: B01J 8/0055 using cyclones
• CPC Class Codes: B01J 8/26 with two or more fluidised beds, e.g. reactor and regeneration installations
• CPC Class Codes: B01J 8/388 externally, i.e. the particles leaving the vessel and subsequently re-entering it
• CPC Class Codes: C01B 3/02 Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
• CPC Class Codes: C10J 2200/09 Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
• CPC Class Codes: C10J 2300/0916 Biomass
• CPC Class Codes: C10J 2300/093 Coal
• CPC Class Codes: C10J 2300/094 Char
• CPC Class Codes: C10J 2300/0946 Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
• CPC Class Codes: C10J 2300/0959 Oxygen
• CPC Class Codes: C10J 2300/0976 as steam
• CPC Class Codes: C10J 2300/0983 Additives
• CPC Class Codes: C10J 2300/0986 Catalysts
• CPC Class Codes: C10J 2300/1246 by external or indirect heating
• CPC Class Codes: C10J 2300/1261 : by pulse burners
• CPC Class Codes: C10J 2300/1625 : with solids treatment
• CPC Class Codes: C10J 2300/1637 : Char combustion
• CPC Class Codes: C10J 2300/1687 : with steam generation
• CPC Class Codes: C10J 2300/1807 : Recycle loops, e.g. gas, solids, heating medium, water
• CPC Class Codes: C10J 2300/1838 : Autothermal gasification by injection of oxygen or steam
• CPC Class Codes: C10J 2300/1846 : Partial oxidation, i.e. injection of air or oxygen only
• CPC Class Codes: C10J 2300/1853 : Steam reforming, i.e. injection of steam only
• CPC Class Codes: C10J 2300/1892 : with one stream being water/steam
• CPC Class Codes: C10J 3/466 : Entrained flow processes
• CPC Class Codes: C10J 3/48 : Apparatus; Plants
• CPC Class Codes: C10J 3/482 : Gasifiers with stationary fluidised bed
• CPC Class Codes: C10J 3/485 : Entrained flow gasifiers
• CPC Class Codes: C10J 3/721 : Multistage gasification, e.g. plural parallel or serial gasification stages
• CPC Class Codes: C10J 3/723 : Controlling or regulating the gasification process
• CPC Class Codes: C10K 1/026 : by centrifugal forces cyclones B04C
• CPC Class Codes: Y02P 20/129 : Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
• CPC Class Codes: Y02P 20/145 : the feedstock being materials of biological origin

Abstract

A solids circulation system receives a gas stream containing char or other reacting solids from a first reactor. The solids circulation system includes a cyclone configured to receive the gas stream from the first reactor, a dipleg from the cyclone to a second reactor, and a riser from the second reactor which merges with the gas stream received by the cyclone. The second reactor has a dense fluid bed and converts the received materials to gaseous products. A conveying fluid transports a portion of the bed media from the second reactor through the riser to mix with the gas stream prior to cyclone entry. The bed media helps manipulate the solids that is received by the cyclone to facilitate flow of solids down the dipleg into the second reactor. The second reactor provides additional residence time, mixing and gas-solid contact for efficient conversion of char or reacting solids.

Claims

1. A system for processing a carbonaceous feedstock to create a final product gas stream containing both carbon monoxide and hydrogen, comprising:

(a) a first reactor (500) having a fluidized bed and configured to receive a feedstock and steam, and output a syngas stream (600) via a first conduit (602), the syngas stream (600) comprising syngas, char, condensable organic compounds and aromatic hydrocarbons;

(b) a second conduit (612) connected to the first conduit (602), the second conduit (612) configured to receive a portion of said syngas stream (600) as a first-stage product gas stream (610);

(c) a second reactor (100) having a fluidized bed and configured to receive char from the syngas stream (600) and an oxygen containing gas, the second reactor configured to operate under conditions sufficient to convert the char into a second-stage product gas stream (910) containing at least carbon monoxide;

wherein;

the second reactor and the second conduit (612) are connected such that the second-stage product gas stream (910) is merged with the first-stage product gas stream (610) to form the final product gas stream (950); and

the fluidized bed in the second reactor (100) contains hollow engineered particles, the hollow engineered particles being one or more from the group consisting of alumina, zirconia, sand, olivine sand, limestone, dolomite and metal catalyst.

2. The system according to claim 1, further comprising:

a restriction orifice (660) configured to reduce a pressure of said first-stage product gas stream (610), prior to being merged with the second-stage product gas stream (910).

3. The system according to claim 2, further comprising:

a first cyclone (300) configured to receive the syngas stream (600) via the first conduit (602);

wherein;

the second conduit (612) is connected to the first conduit (602) via the first cyclone (300); and

the restriction orifice (660) is placed downstream of the first cyclone (300).

4. The system according to claim 3, further comprising:

a second cyclone (700) having an input connected to a freeboard region (160) of the second reactor (100); and

a third cyclone (900) configured to receive a solids-laden second-stage product gas (710) from the second cyclone (700) and output the second-stage product gas stream (910);

wherein;

the third cyclone (900) is connected to the second conduit (612) such that the second-stage product gas stream (910) is merged with the first-stage product gas stream (610) to form the final product gas stream (950).

5. The system according to claim 4, wherein:

the second cyclone (700) is external to the second reactor (100); and

an output of the second cyclone (700) is connected to the second reactor (100) to recycle one or more of char and bed solids captured by the second cyclone (700).

6. The system according to claim 1, further comprising:

a first riser (200) connected to the second reactor (100) and configured to convey bed solids in a direction away from the second reactor (100);

a first separation device (300) connected to the first reactor (500) and to the first riser (200); and

a dipleg (400) having a first end connected to the first separation device (300) and a second end connected to the second reactor (100).

7. The system according to claim 6, wherein:

the first riser (200) conveys the bed solids (120) towards said syngas stream (600);

the first separation device (300) is configured to receive a mixture of said bed solids (120) conveyed through the first riser (200) and said syngas stream (600), and separate said mixture into an intermediate solids mixture (650) and the first-stage product gas stream (610); and

the dipleg (400) conveys the intermediate solids mixture (650) from the first separation device (300) to a dense fluid bed (110) of the second reactor (100).

8. The system according to claim 7, further comprising:

a gas-solids flow regulator (2000) interposed between a dipleg first section (402) connected to the first separation device (300) and a dipleg second section (404) connected to the second reactor (100);

wherein;

the gas-solids flow regulator (2000) is provided with a fluidization media inlet (2130) configured to receive a fluidization media.

9. The system according to claim 6, wherein:

the dipleg (400) and the riser (200) enter the second reactor (100) at locations that are circumferentially spaced apart from one another by at least 90 degrees.

10. The system according to claim 6, wherein:

the first riser (200) comprises a conveying fluid inlet (240) which extends into the second reactor (100) and terminates in a conveying fluid injector (242) configured to inject a conveying fluid into a riser entrance section (210, 210a) at a point within the second reactor (100).

11. The system according to claim 10, wherein:

the conveying fluid injector (242) comprises a bent tip which is configured to inject conveying fluid into the riser inlet (250) at a lowermost portion of the riser entrance section.

12. The system according to claim 11, wherein:

the first riser (200) comprises an upwardly inclined riser entrance section (210) connected to the second reactor (100) and a vertical riser pipe (220) which is angled relative to the riser entrance section; and

the conveying fluid inlet extends along the upwardly inclined riser entrance section.

13. The system according to claim 1, further comprising:

at least one heating conduit (170) protruding into the second reactor to heat the fluidized bed, upon startup.

14. The system according to claim 1, further comprising:

(d) a cooling pipe (180) protruding into the fluidized bed in the second reactor (100) to control bed operating temperature, the cooling pipe being connected to a source of elevated pressure steam as a coolant;

wherein;

the second reactor is configured to operate such that the cooling pipe superheats the elevated pressure steam.

15. The system according to claim 1, wherein the fluidized bed in the second reactor (100) has a bulk density ranging from about 10 pounds per cubic foot to about 60 pounds per cubic foot.

16. A method of processing a carbonaceous feedstock to create a final product gas stream containing both carbon monoxide and hydrogen, comprising:

(a) introducing a carbonaceous feedstock and steam into a first reactor having a fluidized bed;

(b) reacting the carbonaceous feedstock and steam to thereby produce a syngas stream comprising syngas, char, condensable organic compounds and aromatic hydrocarbons;

(c) separating out a first stage product gas stream from the syngas stream;

(d) introducing char from the syngas gas stream, and an oxygen containing gas, into a second reactor having a fluidized bed containing hollow engineered particles, the hollow engineered particles being one or more from the group consisting of alumina, zirconia, sand, olivine sand, limestone, dolomite and metal catalyst;

(e) operating the second reactor under conditions sufficient to convert the char introduced into the second reactor to produce a second-stage product gas stream containing at least carbon monoxide; and

(f) combining said first-stage product gas stream and said second-stage product gas stream to form the final product gas stream.

17. The method according to claim 16, comprising:

operating the second reactor at a temperature of about 650°

C. to about 1,200°

C., and in a substoichiometric mode, to produce the second-stage product gas stream from the char.

18. The method according to claim 16, wherein:

the fluidized bed of the first reactor is a bubbling bed type; and

the fluidized bed of the second reactor is one from the group consisting of a circulating bed type, a turbulent bed type and a bubbling bed type.

19. The method according to claim 18, further comprising:

monitoring a fluid bed level of the second reactor.

20. The method according to claim 16, further comprising:

adding sorbents to the second reactor to capture sulfur contaminants.

21. The method according to claim 16, further comprising:

capturing tars present in the final product gas stream and injecting them back into the second reactor.

22. The method according to claim 16, wherein the final product gas stream has a hydrogen to carbon monoxide molar ratio of about 2.0.

23. The method according to claim 16, comprising:

in step (a), introducing one or more from the group consisting of biomass, refuse derived fuel, coal, and black liquor, as the carbonaceous feedstock.

24. The method according to claim 16, further comprising:

providing the final product gas stream to a heat recovery steam generator (HRSG); and

producing biofuel from gaseous output of the HRSG.

25. The method according to claim 16, further comprising indirectly heating the first reactor via heating conduits.

26. The method according to claim 16, comprising:

in step (g), combining the first-stage product gas stream and the second-stage product gas stream downstream of a restriction orifice to form the final product gas stream.

27. The method according to claim 16, comprising:

operating the first reactor at a carbon conversion target of less than 98% carbon conversion.

28. The method according to claim 16, wherein:

the char transferred to the second reactor has a diameter of less than 50 microns.

29. The method according to claim 16, wherein:

the char transferred to the second reactor has a density of less than 12 pounds per cubic foot.

30. The method according to claim 16, wherein:

the char transferred to the second reactor corresponds to Geldart Group C particle classification.

31. The method according to claim 16, wherein:

the second reactor has a freeboard zone with multiple fluid addition stages; and

the method further comprising adding one or more of air, enriched air, oxygen and steam to the fluid addition stages.

32. The method according to claim 16, comprising:

in the second reactor, exothermically reacting the oxygen containing gas with tars to produce carbon monoxide and carbon dioxide.

33. The method according to claim 16, comprising:

in the second reactor, exothermically reacting the oxygen containing gas with carbon monoxide to produce carbon dioxide according to the reaction equation;

CO+½

O2→

CO2+Heat.

34. The method according to claim 33, comprising:

in the second reactor, endothermically reacting carbon dioxide with the char to produce additional carbon monoxide according to the reaction equation;

CO2+C+Heat→

2CO.

35. The method according to claim 16, further comprising:

introducing steam to the second reactor, in addition to the char and the oxygen containing gas.

36. The method according to claim 35, comprising:

in the second reactor, endothermically reacting steam with the char to produce methane and carbon dioxide according to the gasification reaction equation;

H₂O+C+Heat→

½

CH4+½

CO2.

37. The method according to claim 36, further comprising:

in the second reactor, endothermically reacting carbon dioxide with the char to produce carbon monoxide according to the reaction equation;

CO2+C+Heat→

2CO.

38. The method according to claim 35, comprising:

in the second reactor, endothermically reacting steam with the char to produce hydrogen and additional carbon monoxide according to the steam reforming reaction equation;

H₂O+C+Heat→

H2+CO.

39. The method according to claim 38, comprising:

in the second reactor, exothermically reacting hydrogen with the char to produce methane through according to the hydrogasification reaction equation;

C+2H2→

CH4+Heat.

40. The method according to claim 38, comprising:

in the second reactor, exothermically reacting carbon monoxide with hydrogen to produce methane and steam according to the methanation reaction equation;

CO+3H2→

CH4+H₂O+Heat.

41. The method according to claim 38, comprising:

in the second reactor, exothermically reacting the oxygen containing gas with hydrogen to produce steam according to the reaction equation;

H₂+½

O2→

H₂O+Heat.

42. The method according to claim 16, further comprising:

introducing carbon dioxide to the second reactor, in addition to the char and the oxygen containing gas.

43. The method according to claim 42, further comprising:

in the second reactor, endothermically reacting carbon dioxide with the char to produce carbon monoxide according to the reaction equation;

CO2+C+Heat→

2CO.

44. The method according to claim 16, comprising:

in the second reactor, exothermically reacting the oxygen containing gas with the char to produce carbon monoxide and carbon dioxide according to the reaction equation;

C+xO2→

yCO+(x−

y/2)CO2+Heat,

wherein x and y represent stoichiometric amounts.

45. The method according to claim 44, further comprising:

in the second reactor, endothermically reacting carbon dioxide with the char to produce additional carbon monoxide according to the reaction equation;

CO2+C+Heat→

2CO.

46. The method according to claim 16, wherein the fluidized bed in the second reactor has a bulk density ranging from about 10 pounds per cubic foot to about 60 pounds per cubic foot.