Hydrothermal carbonisation method

Patent metadata

Field	Value
Publication number	US-12448577-B2
Application number	US-202118033507-A
Country	US
Kind code	B2
Filing date	Nov 3, 2021
Priority date	Nov 4, 2020
Publication date	Oct 21, 2025
Grant date	Oct 21, 2025

Abstract

The invention relates to a method for hydrothermal carbonisation of biomass containing organic matter, the method comprising: —injecting the biomass, a heat transfer fluid and a reagent into a reactor ( 1 ), —circulating a mixture consisting of the biomass, the heat transfer fluid and the reagent under specific pressure and temperature conditions for transforming the organic matter by hydrothermal carbonisation. The invention consists in: 1) determining the production rate of the emitted gas T e during the hydrothermal carbonisation reaction; 2) comparing the determined production rate of the emitted gas T e with a predefined value for the set gas production rate T c , and 3) adjusting at least one of the reaction control parameters chosen from among the temperature within the reactor ( 1 ), the quantity of injected reactant, and the residence time in the reactor in order to adjust the production rate of the emitted gas T e , such that the value of said production rate of the emitted gas Te tends to be equal to the value of the set gas production rate T c . The invention is applicable to treatment of biomass containing organic matter.

First claim

The invention claimed is:

1. A method for the hydrothermal carbonisation of a biomass containing organic matter, the method comprising:
injecting the biomass, a heat transfer fluid and a reagent into a reactor;
circulating in the reactor a mixture consisting of the biomass, the heat transfer fluid, and the reagent;
subjecting the mixture to specific pressure and temperature conditions in the reactor such that the organic matter in the biomass undergoes a hydrothermal carbonisation reaction in the reactor and the biomass is transformed into a carbonized biomass,
determining an emitted gas production rate Te in the reactor during the hydrothermal carbonisation reaction;
comparing the emitted gas production rate Te in the reactor to a predefined setpoint gas production rate Tc; and
adjusting at least one reaction drive parameter such that the emitted gas production rate Te in the reactor tends to be equal to or to approach the predefined setpoint gas production rate Tc, wherein the at least one reaction drive parameter is selected from the group consisting of a temperature in the reactor, an amount of the reagent injected into the reactor, and a residence time of the biomass in the reactor.

2. The method according to claim 1 , wherein the method is carried out continuously, and wherein the method further comprises:
measuring a flow rate of non-condensable gases emitted from an outlet of the reactor during the hydrothermal carbonisation reaction; and
calculating the emitted gas production rate Te based on the measurement of the flow rate of non-condensable gases emitted from the outlet of the reactor.

3. The method according to claim 2 , further comprising:
prior to or during the hydrothermal carbonisation reaction, defining the predefined setpoint gas production rate Tc as a function of a desired dryness of the biomass after the biomass has been subjected to a dehydration process performed subsequent to the hydrothermal carbonisation reaction.

4. The method according to claim 2 , further comprising:
prior to measuring the flow rate of the non-condensable gases emitted from the outlet of the reactor, passing the non-condensable gases through a condenser or other dehydration means.

5. The method according to one of claim 2 , further comprising:
adjusting the temperature in the reactor during the hydrothermal carbonisation reaction by modifying a temperature of the heat transfer fluid injected into the reactor; and/or
adjusting the residence time of the biomass in the reactor during the hydrothermal carbonisation reaction by modifying a flow rate of the biomass injected into the reactor.

6. The method according to claim 1 , wherein the reactor is sealed during the hydrothermal carbonisation reaction and the method is carried out in a batch mode, and wherein the method further comprises:
cooling the reactor to a set target temperature;
after cooling the reactor to the set target temperature, measuring a pressure prevailing in the reactor at the set target temperature; and
calculating the emitted gas production rate Te based on the measurement of the pressure prevailing in the reactor at the set target temperature.

7. The method according to claim 6 , further comprising:
adjusting the residence time of the biomass in the reactor based on a reaction time of a previous hydrothermal carbonisation reaction carried out in the reactor.

8. The method according to claim 6 , further comprising:
cooling the reactor to the set target temperature by heat exchange with another heat transfer fluid through a wall of the reactor or a coil within the reactor.

9. The method according to claim 1 , further comprising:
increasing or decreasing the amount of the reagent injected into the reactor such that the emitted gas production rate Te tends to be equal to or to approach the predefined setpoint gas production rate Tc.

10. A method for dehydrating biomass comprising:
injecting the biomass, a heat transfer fluid, and a reagent into a reactor:
circulating in the reactor a mixture consisting of the biomass, the heat transfer fluid, and the reagent;
subjecting the mixture to specific pressure and temperature conditions in the reactor such that organic matter in the biomass undergoes a hydrothermal carbonisation reaction in the reactor and the biomass is transformed into a carbonized biomass,
determining an emitted gas production rate Te in the reactor during the hydrothermal carbonisation reaction;
comparing the emitted gas production rate Te in the reactor to a predefined setpoint gas production rate Tc;
adjusting at least one reaction drive parameter such that the emitted gas production rate Te in the reactor tends to be equal to or to approach the predefined setpoint gas production rate Tc, wherein the at least one reaction drive parameter is selected from the group consisting of a temperature in the reactor, an amount of the reagent injected into the reactor, and a residence time of the biomass in the reactor; and
after the hydrothermal carbonisation reaction, mechanically dehydrating the carbonized biomass to form a dehydrated biomass.

11. The method according to claim 2 , wherein the emitted gas production rate Te is determined during the hydrothermal carbonisation reaction in the reactor, the emitted gas production rate Te is compared to the predefined setpoint gas production rate Tc during the hydrothermal carbonisation reaction in the reactor, and the at least one reaction drive parameter is adjusted in real time during the hydrothermal carbonisation reaction in the reactor.

12. The method according to claim 1 , wherein the Te is at least partly attributable to gases emitted from the organic matter during the hydrothermal carbonisation reaction.

13. The method according to claim 1 , wherein, during the hydrothermal carbonisation reaction, the organic matter undergoes hydrolysis and then decarboxylation and dehydration.

14. The method according to claim 1 , wherein the reagent comprises a catalyst configured to initiate the hydrothermal carbonisation reaction.

15. The method according to claim 14 , wherein the reagent comprises at least one acid catalyst selected from the group consisting of sulphuric acid, linear C 1 -C 6 carboxylic acids, and branched C 1 -C 6 carboxylic acids, and wherein the linear C 1 -C 6 carboxylic acids and the branched C 1 -C 6 carboxylic acids are mono-, di-, or tricarboxylic acids.

16. The method according to claim 6 , wherein the set target temperature is 75 degrees Celsius, and wherein the method further comprises:
calculating an estimated final dryness of the biomass after the carbonized biomass has been subjected to a subsequent dehydration process according to the following equation:
Ln P=f (Ln( TS /(0.0001− TS )),

where
f(x)=−03226*x+10.8734,
P is the pressure prevailing in the reactor at the set target temperature in Pa, and
TS is the final dryness of the biomass in g/L.

Assignees

• Suez Int

Inventors

• Bourdais Jean-Louis
• Choo-Kun Marlène

Classifications

• C10J2300/1861

  Heat exchange between at least two process streams · CPC title

• C10J2300/183

  Non-continuous or semi-continuous processes · CPC title

• C10J2300/1612

  CO2-separation and sequestration, i.e. long time storage · CPC title

• C10J2300/0923

  Sludge, e.g. from water treatment plant · CPC title

• C02F2209/44

  Time · CPC title