BIOMASS CONVERSION SYSTEMS HAVING INTEGRATED HEAT MANAGEMENT AND METHODS FOR USE THEREOF

• US 20120151827A1
• Filed: 12/20/2011
• Published: 06/21/2012
• Est. Priority Date: 12/20/2010
• Status: Active Grant

• Current Assignee: Shell Oil Company (Shell Plc)
• Original Assignee: Shell Oil Company (Shell Plc)
• Inventors: POWELL, Joseph Broun, CHHEDA, Juben Nemchand
• Granted Patent: US 8,729,324 B2
• Time in Patent Office: Days
• US Class Current: 44/307
• CPC Class Codes: C10G 1/002 in combination with oil conversion- or refining processes
• CPC Class Codes: C10G 1/065 in the presence of a solvent
• CPC Class Codes: C10G 2300/1014 of vegetal origin
• CPC Class Codes: C10G 2300/202 Heteroatoms content, i.e. S, N, O, P
• CPC Class Codes: C10G 2300/4081 Recycling aspects
• CPC Class Codes: C10G 3/00 Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids production from non-melting solid oxygen-containing carbonaceous materials C10G1/00
• CPC Class Codes: C10G 3/40 Thermal non-catalytic treatment
• CPC Class Codes: C10G 3/52 Hydrogen in a special composition or from a special source
• CPC Class Codes: C10L 1/026 for compression ignition
• CPC Class Codes: Y02P 30/20 using bio-feedstock

Abstract

Biomass conversion systems may incorporate integrated heat management to operate more efficiently during biomass conversion. Biomass conversion systems may comprise a first fluid circulation loop comprising a hydrothermal digestion unit, and a first catalytic reduction reactor unit in fluid communication with an inlet and an outlet of the hydrothermal digestion unit; and a second fluid circulation loop comprising a reaction product take-off line in fluid communication with the first fluid circulation loop, a second catalytic reduction reactor unit in fluid communication with the reaction product take-off line, and a recycle line establishing fluid communication between the first fluid circulation loop and an outlet of the second catalytic reduction reactor unit, where the first catalytic reduction reactor unit contains at least one first catalyst and the second catalytic reduction reactor unit contains at least one second catalyst, each being capable of activating molecular hydrogen.

Claims

1. A biomass conversion system comprising:

a first fluid circulation loop comprising;

a hydrothermal digestion unit; and

a first catalytic reduction reactor unit in fluid communication with an inlet and an outlet of the hydrothermal digestion unit;

wherein the first catalytic reduction reactor unit contains at least one first catalyst that is capable of activating molecular hydrogen; and

a second fluid circulation loop comprising;

a reaction product take-off line in fluid communication with the first fluid circulation loop;

a second catalytic reduction reactor unit in fluid communication with the reaction product take-off line;

wherein the second catalytic reduction reactor unit contains at least one second catalyst that is capable of activating molecular hydrogen; and

a recycle line establishing fluid communication between the first fluid circulation loop and an outlet of the second catalytic reduction reactor unit.

2. The biomass conversion system of claim 1, wherein the first catalytic reduction reactor unit comprises a fixed bed catalytic reactor.

3. The biomass conversion system of claim 1, wherein the first fluid circulation loop lacks a purification mechanism operable for removing nitrogen compound impurities, sulfur compound impurities, or any combination thereof.

4. The biomass conversion system of claim 3, wherein the at least one first catalyst comprises a poison-tolerant catalyst.

5. The biomass conversion system of claim 3, wherein the at least one first catalyst is regenerable when poisoned with nitrogen compound impurities, sulfur compound impurities, or any combination thereof.

6. The biomass conversion system of claim 3, wherein the at least one first catalyst comprises a sulfided catalyst.

7. The biomass conversion system of claim 3, wherein the at least one second catalyst is not a poison-tolerant catalyst.

8. The biomass conversion system of claim 1, wherein the first fluid circulation loop is configured to establish countercurrent flow in the hydrothermal digestion unit.

9. The biomass conversion system of claim 1, further comprising:

a biomass feed mechanism operatively coupled to the hydrothermal digestion unit that allows a cellulosic biomass to be continuously or semi-continuously added to the hydrothermal digestion unit without the hydrothermal digestion unit being depressurized.

10. The biomass conversion system of claim 1, further comprising:

a phase separation mechanism in fluid communication with the outlet of the second catalytic reduction reactor unit.

11. The biomass conversion system of claim 1, further comprising:

a phase separation mechanism in fluid communication with an outlet of the first catalytic reduction reactor unit.

12. The biomass conversion system of claim 1, further comprising:

a flow control mechanism associated with each fluid circulation loop that allows a recycle ratio in each fluid circulation loop to be altered.

13. A method comprising:

providing a biomass conversion system comprising;

a first fluid circulation loop comprising;

a hydrothermal digestion unit; and

a first catalytic reduction reactor unit in fluid communication with an inlet and an outlet of the hydrothermal digestion unit;

wherein the first catalytic reduction reactor unit contains at least one first catalyst that is capable of activating molecular hydrogen; and

a second fluid circulation loop comprising;

a reaction product take-off line in fluid communication with the first fluid circulation loop;

a second catalytic reduction reactor unit in fluid communication with the reaction product take-off line;

wherein the second catalytic reduction reactor unit contains at least one second catalyst that is capable of activating molecular hydrogen; and

a recycle line establishing fluid communication between the first fluid circulation loop and an outlet of the second catalytic reduction reactor unit;

providing a cellulosic biomass in the hydrothermal digestion unit;

heating the cellulosic biomass in the hydrothermal digestion unit to digest at least a portion of the cellulosic biomass and form a hydrolysate comprising soluble carbohydrates within a liquor phase;

wherein at least about 70% of the heat added to the cellulosic biomass in the hydrothermal digestion unit is generated internally in the first catalytic reduction reactor unit and the second catalytic reduction reactor unit;

transferring at least a portion of the liquor phase to the first catalytic reduction reactor unit;

forming a first reaction product in the first catalytic reduction reactor unit;

recirculating at least a portion of the liquor phase to the hydrothermal digestion unit at a first flow rate; and

altering the first flow rate to increase or decrease a temperature of the liquor phase in the first fluid circulation loop.

14. The method of claim 13, wherein heating the cellulosic biomass in the hydrothermal digestion unit takes place at a pressure of at least about 30 bar.

15. The method of claim 13, wherein heating the cellulosic biomass in the hydrothermal digestion unit takes place in the presence of an organic solvent.

16. The method of claim 13, wherein the liquor phase is recirculated to the hydrothermal digestion unit such that countercurrent flow is established in the hydrothermal digestion unit.

17. The method of claim 13, wherein at least about 60% of the cellulosic biomass, on a dry basis, is digested to produce hydrolysate.

18. The method of claim 13, wherein at least about 90% of the cellulosic biomass, on a dry basis, is digested to produce hydrolysate.

19. The method of claim 13, wherein at least the at least one first catalyst comprises a poison-tolerant catalyst.

20. The method of claim 13, wherein at least the at least one first catalyst comprises a sulfided catalyst.

21. The method of claim 13, wherein the first flow rate is such that the liquor phase spends about 3 hours or less in the hydrothermal digestion unit before being transferred to the first catalytic reduction reactor unit.

22. The method of claim 13, wherein the first flow rate is such that the liquor phase is recirculated in the first fluid circulation loop at a recycle ratio of at least about 2.

23. The method of claim 13, wherein the first flow rate is such that the liquor phase is recirculated in the first fluid circulation loop at a recycle ratio of up to about 20.

24. The method of claim 13, wherein the first flow rate is such that the liquor phase is recirculated in the first fluid circulation loop at a recycle ratio ranging between about 4 and about 10.

25. The method of claim 13, wherein providing a cellulosic biomass in the hydrothermal digestion unit comprises continuously or semi-continuously adding a cellulosic biomass to the hydrothermal digestion unit without the hydrothermal digestion unit being depressurized.

26. The method of claim 25, wherein, after the cellulosic biomass is added to the hydrothermal digestion unit, the pressure in the hydrothermal digestion unit is at least about 30 bar.

27. The method of claim 13, wherein the liquor phase enters the first catalytic reduction reactor unit at a temperature ranging between about 120°

C. and about 190°

C. and exits the first catalytic reduction reactor unit at a temperature ranging between about 260°

C. and about 275°

C.

28. The method of claim 13, further comprising:

converting the first reaction product into a biofuel.

29. The method of claim 13, further comprising:

monitoring the temperature of the liquor phase in the first fluid circulation loop.

30. The method of claim 13, further comprising:

performing a phase separation of the first reaction product to form an aqueous phase and an organic phase; and

recirculating the aqueous phase to the hydrothermal digestion unit.

31. The method of claim 13, further comprising:

transferring at least a portion of the first reaction product to the second fluid circulation loop;

forming a second reaction product in the second catalytic reduction reactor unit; and

recirculating at least a portion of the second reaction product to the first fluid circulation loop at a second flow rate.

32. The method of claim 31, further comprising:

converting the second reaction product into a biofuel.

33. The method of claim 31, further comprising:

performing a phase separation of the second reaction product to form an aqueous phase and an organic phase.

34. The method of claim 33, further comprising:

recirculating at least a portion of the organic phase to the first fluid circulation loop.

35. The method of claim 31, wherein the second flow rate is such that the second reaction product is recirculated to the first fluid circulation loop at a recycle ratio of at least about 0.1.

36. The method of claim 31, wherein the second flow rate is such that the second reaction product is recirculated to the first fluid circulation loop at a recycle ratio ranging between about 0.1 and about 0.5.

37. The method of claim 31, wherein the second flow rate is such that a sufficient quantity of the second reaction product is recirculated to the first fluid circulation loop to inhibit lignins from precipitating.

38. The method of claim 31, wherein the second reaction product comprises a higher percentage of organic compounds than it does water.