Fast pyrolysis of biomass in an autothermally operating reactor

Patent metadata

Field	Value
Publication number	US-10851037-B2
Application number	US-201715798056-A
Country	US
Kind code	B2
Filing date	Oct 30, 2017
Priority date	Oct 31, 2016
Publication date	Dec 1, 2020
Grant date	Dec 1, 2020

Abstract

The present invention is directed to a pyrolysis method. The method involves providing a biomass and subjecting the biomass, in a reactor operating under conditions of parasitic heat loss of less than 1% of the biomass' chemical energy content, to partial oxidation where, during steady state operation of the reactor, oxygen is provided to the reactor in sufficient quantity to achieve an equivalence ratio of 0.06 to 0.15 to release sufficient energy to support endothermic pyrolysis reactions and produce condensable organic compounds as the major portion of the pyrolysis products.

First claim

What is claimed:

1. A pyrolysis method comprising:
providing a biomass and
subjecting said biomass, in a reactor operating at a heat loss of less than 1% of the biomass' chemical energy content, to partial oxidation where, during steady state operation of the reactor, oxygen is provided to the reactor in sufficient quantity to achieve an equivalence ratio of 0.06 to 0.15 to release sufficient energy to support endothermic pyrolysis reactions and produce pyrolysis products comprising condensable organic compounds, wherein the condensable organic compounds are the major portion of the pyrolysis products and the major portion comprises at least about 50% of the total pyrolysis products.

2. The method of claim 1 , wherein said subjecting is effective to increase the level of biomass throughput in the reactor, during steady state operation, by a value proportional to more than the reactor's diameter squared, as compared to when said subjecting is carried out in the absence of partial oxidation.

3. The method of claim 2 , wherein said subjecting is effective to increase the level of biomass throughput in the reactor, during steady state operation, by a value proportional to up to and optionally including, the reactor's diameter cubed, as compared to when said subjecting is carried out in the absence of partial oxidation.

4. The method of claim 1 , wherein the condensable organic compounds have a residence time in the reactor of 2-5 seconds.

5. The method of claim 1 , wherein said subjecting is carried out in a well-mixed reactor.

6. The method of claim 5 , wherein the well-mixed reactor is a fluidized bed reactor.

7. The method of claim 1 , wherein the production of condensable organic compounds is achieved with little or no loss in bio-oil yield or quantity compared to when oxygen is not provided to the reactor.

8. The method of claim 1 , wherein the major portion of the pyrolysis products comprises bio-oil.

9. The method of claim 1 , wherein the reactor is insulated and constructed to reduce the reactor's intrinsic surface area to volume ratio.

10. The method of claim 1 , wherein the biomass is selected from the group consisting of forest and mill residues, agricultural crops and wastes, wood and wood wastes, grasses, manure, livestock operation residues, trees and plants, and municipal and industrial wastes.

11. The method of claim 1 , wherein said subjecting is carried out at a temperature of 400 to 600° C.

12. The method of claim 1 , wherein the partial oxidation is carried out with air or air/nitrogen mixtures.

13. The method of claim 1 further comprising:
recovering said condensable organic compounds after said subjecting.

14. The method of claim 13 , wherein the recovered condensable organic compounds contain 5 to 15 wt % pyrolytic sugars.

15. The method of claim 13 , wherein the recovered condensable organic compounds contain 45 to 60 wt % phenolics.

16. The method of claim 1 further comprising:
recovering biochar produced in the reactor after said subjecting.

17. The method of claim 1 , wherein the reactor is provided with a heater to enable the reactor to reach steady state operation and enable the reactor to operate adiabatically during such steady state operation.

18. The method of claim 1 , wherein said subjecting produces condensable organic compounds and said method further comprises:
cooling the condensable organic compounds in a first stage comprising a condenser having passages for the condensable organic compounds separated by a heat conducting wall from passages for a coolant, wherein the coolant in the condenser of the first stage is maintained at a substantially constant temperature, set at a temperature in the range of 75 to 130° C., to condense a first liquid fraction of liquefied bio-oil constituents in the condenser of the first stage and
collecting the first liquid fraction of liquefied bio-oil constituents from the condenser of the first stage.

19. The method of claim 18 further comprising:
recovering a first bio-oil vapor fraction from the condenser of the first stage and
removing aerosols from the first bio-oil vapor fraction in a second stage as a second liquid fraction of liquefied bio-oil constituents.

20. The method of claim 19 further comprising:
recovering a second bio-oil vapor fraction after said removing aerosols;
cooling the second bio-oil vapor fraction in a third stage comprising a condenser having passages for the second bio-oil vapor fraction separated by a heat conducting wall from passages for a coolant, wherein the coolant in the condenser of the third stage is maintained at a substantially constant temperature, set at a temperature above the dew point of water, to condense a third liquid fraction of liquefied bio-oil constituents in the condenser of the third stage; and
collecting the third liquid fraction of liquefied bio-oil constituents from the condenser of the third stage.

21. The method of claim 20 further comprising:
recovering a third bio-oil vapor fraction from the third stage and
removing aerosols from the third bio-oil vapor fraction in a fourth stage as a fourth liquid fraction of liquefied bio-oil constituents.

22. The method of claim 21 further comprising:
recovering a fourth bio-oil vapor fraction after said removing aerosols from the third bio-oil vapor fraction;
cooling the fourth bio-oil vapor fraction in a condenser of a fifth stage having passages for the fourth bio-oil vapor separated by a heat conducting wall from passages for a coolant, wherein the coolant in the condenser of the fifth stage is maintained at a substantially constant temperature, with a temperature set sufficiently low to condense substantially all water vapor from the fourth bio-oil vapor as a fifth liquid fraction of liquefied bio-oil constituents in the condenser of the fifth stage; and
collecting the fifth liquid fraction of liquefied bio-oil constituents from the condenser of the fifth stage.

23. The method of claim 1 , wherein said subjecting produces condensable organic compounds and said method further comprises:
cooling the condensable organic compounds in a liquid scrubbing system to condense a first liquid fraction of liquefied bio-oil constituents and
collecting the first liquid fraction of liquefied bio-oil constituents from the liquid scrubbing system.

Assignees

• Univ Iowa State Res Found Inc

Inventors

• Brown Robert C
• Polin Joseph P
• Whitmer Lysle E

Classifications

• C13K1/02 Primary

  obtained by saccharification of cellulosic materials (manufacture of fodder A23K10/32) · CPC title

• C10B53/02

  of cellulose-containing material (production of pyroligneous acid C10C5/00) · CPC title

• C10C5/00

  Production of pyroligneous acid {distillation of wood, dry distillation of organic waste}(carbonisation of wood C10B) · CPC title

• C11B1/04

  of vegetable raw material {(C11B1/025 takes precedence)} · CPC title

• C10K1/028

  by electrostatic precipitation (separating dispersed particles from gases or vapour by electrostatic effect in general B03C3/00) · CPC title