Hydrothermal liquefaction system

Patent metadata

Field	Value
Publication number	US-11279882-B2
Application number	US-202016740339-A
Country	US
Kind code	B2
Filing date	Jan 10, 2020
Priority date	Jan 10, 2020
Publication date	Mar 22, 2022
Grant date	Mar 22, 2022

Abstract

A hydrothermal liquefaction (HTL) system can comprise a biomass slurry source, a first pump in fluid communication with the slurry source and configured to pressurize a biomass slurry stream from the slurry source to a first pressure, a first heat exchanger in fluid communication with the first pump and configured to heat a slurry stream received from the first pump to a first temperature, a second pump in fluid communication with the first heat exchanger and configured to pressurize a slurry stream received from the first heat exchanger to a second pressure higher than the first pressure, a second heat exchanger in fluid communication with the second pump and configured to heat a slurry stream received from the second pump to a second temperature higher than the first temperature, and a HTL reactor configured to produce biocrude from a slurry stream received from the second heat exchanger.

First claim

The invention claimed is:

1. A system, comprising:
a biomass slurry source;
a first pump in fluid communication with the biomass slurry source and configured to pressurize a biomass slurry stream from the biomass slurry source to a first pressure;
a first heat exchanger in fluid communication with the first pump and configured to heat a biomass slurry stream received from the first pump at the first pressure to a first temperature;
a second pump in fluid communication with the first heat exchanger and configured to pressurize a biomass slurry stream received from the first heat exchanger at the first temperature to a second pressure that is higher than the first pressure;
a second heat exchanger in fluid communication with the second pump and configured to heat a biomass slurry stream received from the second pump at the second pressure to a second temperature that is higher than the first temperature;
a hydrothermal liquefaction (HTL) reactor in fluid communication with the second heat exchanger and configured to produce a product mixture stream including biocrude from a biomass slurry stream received from the second heat exchanger;
a third heat exchanger configured to receive the product mixture stream from the HTL reactor to heat a heat transfer liquid;
wherein the second heat exchanger is in fluid communication with the third heat exchanger and configured to receive a heat transfer liquid stream from the third heat exchanger to heat the biomass slurry stream received from the second pump;
wherein the first heat exchanger is in fluid communication with the second heat exchanger and configured to receive a heat transfer liquid stream from the second heat exchanger to heat the biomass slurry stream received from the first pump; and
wherein the first heat exchanger is in fluid communication with the third heat exchanger such that a heat transfer liquid stream from the first heat exchanger flows back to the third heat exchanger.

2. The system of claim 1 , wherein:
the first pressure is from 500 psi to 1,500 psi; and
the first temperature is from 300° F. to 600° F.

3. The system of claim 2 , wherein:
the first heat exchanger comprises a shell and a plurality of tubes disposed in the shell;
an inner diameter of the tubes is from 0.5 inch to 2 inches; and
a viscosity of the biomass slurry stream received from the first pump is from 300 cP to 20,000 cP such that flow of the biomass slurry in the tubes is laminar.

4. The system of claim 3 , wherein the first pump is a slurry pump configured to pump a biomass slurry mixture comprising 15% solids to 30% solids in water.

5. The system of claim 1 , wherein:
the second pressure is 2,500 psi to 3,500 psi; and
the second temperature is 400° F. to 700° F.

6. The system of claim 5 , wherein:
the second heat exchanger comprises a shell and a plurality of tubes disposed in the shell;
an inner diameter of the tubes is from 0.25 inch to 0.5 inch; and
a viscosity of the biomass slurry stream received from the second pump is 300 cP or less such that flow of the biomass slurry in the tubes is turbulent.

7. The system of claim 5 , wherein the second pump is configured to pump abrasive slurries at a temperature of 200° F. or greater.

8. The system of claim 1 , wherein:
the third heat exchanger is configured to receive the product mixture stream from the HTL reactor at a temperature of 400° F. to 900° F.

9. A method, comprising:
pressurizing a biomass slurry stream from a biomass slurry source to a first pressure;
in a first heat exchanger, heating the biomass slurry stream at the first pressure to a first temperature;
pressurizing the biomass slurry stream at the first temperature to a second pressure that is greater than the first pressure;
in a second heat exchanger, heating the biomass slurry stream at the second pressure to a second temperature that is greater than the first temperature;
flowing the biomass slurry stream at the second pressure and the second temperature from the second heat exchanger through a hydrothermal liquefaction (HTL) reactor to produce a product mixture stream including biocrude;
flowing the product mixture stream from the HTL reactor through a third heat exchanger configured to heat a heat transfer liquid;
flowing the heat transfer liquid from the third heat exchanger through the second heat exchanger to heat the biomass slurry stream to the second temperature; and
flowing the heat transfer liquid from the second heat exchanger through the first heat exchanger to heat the biomass slurry stream to the first temperature, and from the first heat exchanger back to the third heat exchanger.

10. The method of claim 9 , wherein pressurizing the biomass slurry stream to the first pressure further comprises pressurizing the biomass slurry stream to a first pressure of 500 psi to 1,500 psi with a slurry pump.

11. The method of claim 10 , wherein heating the biomass slurry stream to the first temperature further comprises flowing the biomass slurry stream through the first heat exchanger at the first pressure to heat the biomass slurry stream to a temperature of 300° F. to 600° F.

12. The method of claim 11 , wherein:
the first heat exchanger comprises a shell and a plurality of tubes disposed in the shell;
an inner diameter of the tubes is from 0.5 inch to 2 inches; and
heating the biomass slurry stream further comprises flowing the biomass slurry stream through the tubes of the first heat exchanger to heat the biomass slurry stream from ambient temperature to a temperature of 300° F. to 600° F. such that a viscosity of the biomass slurry stream is reduced to 300 cP or less in the first heat exchanger.

13. The method of claim 12 , wherein pressurizing the biomass slurry stream at the first temperature to the second pressure further comprises pressurizing the biomass slurry stream to a second pressure of 2,500 psi to 3,500 psi.

14. The method of claim 13 , wherein heating the biomass slurry stream to the second temperature further comprises flowing the biomass slurry stream through the second heat exchanger at the second pressure to heat the biomass slurry stream to a second temperature of 400° F. to 700° F.

15. The method of claim 14 , wherein:
the second heat exchanger comprises a shell and a plurality of tubes disposed in the shell;
an inner diameter of the tubes is from 0.25 inch to 0.5 inch; and
flowing the biomass slurry stream through the second heat exchanger further comprises flowing the biomass slurry stream at a viscosity of 300 cP or less such that flow of the biomass slurry stream in the tubes is turbulent.

16. The method of claim 9 , wherein the first heat exchanger comprises a shell and a plurality of tubes disposed in the shell, and the plurality of tubes and the shell of the first heat exchanger are configured to handle liquids at or below the first pressure.

17. The method of claim 9 , further comprising:
pressurizing the heat transfer liquid with a third pump prior to flowing the heat transfer liquid through the third heat exchanger; and
prior to flowing the heat transfer liquid through the second heat exchanger, heating the heat transfer liquid with a heater.

18. The method of claim 17 , wherein:
the third heat exchanger is configured to heat the heat transfer liquid to a temperature of 600° F. to 750° F.; and
the heater is configured to heat the heat transfer liquid to a temperature of 700° F. to 800° F.

19. The method of claim 9 , wherein the biomass slurry stream from the second heat exchanger flows directly t

Assignees

• Battelle Memorial Institute

Inventors

• Thorson Michael R
• Snowden-Swan Lesley J
• Schmidt Andrew J
• Hart Todd R
• Billing Justin M
• Anderson Daniel B
• Hallen Richard T

Classifications

• C10G3/40

  Thermal non-catalytic treatment · CPC title

• C10L2290/46

  Compressors or pumps · CPC title

• C10L2290/06

  Heat exchange, direct or indirect · CPC title

• C10L9/086

  Hydrothermal carbonization · CPC title

• C02F2301/024

  Turbulent · CPC title