System and method for biological methane gas generation and removal of carbon dioxide therefrom

Patent metadata

Field	Value
Publication number	US-12415976-B2
Application number	US-202017137956-A
Country	US
Kind code	B2
Filing date	Dec 30, 2020
Priority date	Dec 30, 2020
Publication date	Sep 16, 2025
Grant date	Sep 16, 2025

Abstract

A system for biological methane production and removing carbon dioxide from the methane comprises (a) a primary anaerobic digester adapted and arranged to generate a gaseous mixture comprising methane and carbon dioxide from organic materials; (b) an electrochemical reactor comprising at least one reactor cell including an anode spaced from a cathode by a porous ion exchange resin wafer with a cation exchange membrane between the anode and the resin wafer and a bipolar ion exchange membrane between the cathode and the resin wafer; the electrochemical reactor being adapted and arranged to capture gaseous carbon dioxide within the resin wafer as aqueous bicarbonate, and to electrochemically generate hydrogen gas at the cathode; and (c) a hydrogenotrophic methanogenesis bioreactor adapted and arranged to convert the bicarbonate and hydrogen from the electrochemical reactor to methane. An electrochemical reactor and a method for producing methane with reduced carbon dioxide content also are described.

First claim

The embodiments of the invention in which an exclusive property or privilege is claimed are defined as follows:

1. A system for biologically generating methane and removing carbon dioxide therefrom, the system comprising:
(a) a primary anaerobic digester adapted and arranged to generate a gaseous mixture comprising methane and carbon dioxide from organic materials;
(b) an electrochemical reactor; and
(c) a hydrogenotrophic methanogenesis bioreactor adapted and arranged to convert the bicarbonate and hydrogen from the electrochemical reactor to methane;
wherein:
the electrochemical reactor comprises a plurality reactor cells in a stack with each reactor cell including:
an anode;
a cathode spaced from the anode;
a single porous ion exchange resin wafer between the anode and the cathode, wherein the ion exchange resin wafer consists of a basic ion exchange resin wafer;
a cation exchange membrane adjacent to the anode between the anode and the resin wafer, wherein the cation exchange membrane is adjacent to both the anode and the resin wafer; and
a bipolar ion exchange membrane between the cathode and the resin wafer, wherein the bipolar exchange membrane is adjacent to both the cathode and the resin wafer;
wherein:
the cathode of each adjacent reactor cell is separated from the anode of the nearest adjacent cell by an electrical insulator;
the reactor cells are in fluid communication with each other in series so that liquid and gas flow through each resin wafer sequentially; and
the electrochemical reactor includes a hydrogen transfer line to direct hydrogen gas from the cathodes out of the electrochemical reactor;
the electrochemical reactor is adapted and arranged to capture gaseous carbon dioxide within the resin wafer as aqueous bicarbonate, and to electrochemically generate hydrogen gas at the cathodes when an aqueous liquid and a carbon dioxide-containing gas are flowing through the reactor cells, and a voltage is applied across the anode and the cathode of each reactor cell;
the primary anaerobic digester includes a gas transfer line in fluid communication with an inlet end of the electrochemical reactor adapted and arranged to receive gas and liquid into pores of the resin wafer;
the electrochemical reactor further includes a first gas vent line; an outlet operably connected to a liquid transfer line in fluid communication with the hydrogenotrophic methanogenesis bioreactor; and a hydrogen transfer line providing fluid communication between the hydrogenotrophic methanogenesis bioreactor and a region adjacent the cathode where hydrogen is generated during use; and
the hydrogenotrophic methanogenesis bioreactor comprises: a liquid recycle line in fluid communication with the inlet end of the electrochemical reactor adapted and arranged to direct fluid flow through the electrochemical reactor; and a second gas vent line;
wherein in use, the electrochemical reactor is filled with an aqueous fluid; the gaseous mixture containing methane and carbon dioxide is formed from the organic materials in the primary anaerobic digester; and the gaseous mixture is transferred from the primary anaerobic digester via the gas transfer line into the inlet end of the electrochemical reactor to flow through the resin wafer while a voltage is applied across the cathode and the anode; the carbon dioxide from the gaseous mixture is electrochemically converted to bicarbonate in the aqueous fluid within electrochemical reactor; hydrogen is electrochemically generated at the cathode; the methane from the gaseous mixture and the aqueous fluid both flow through the resin wafer, and carbon dioxide-depleted methane is vented through the first gas vent line and stored for later use; the aqueous fluid containing the bicarbonate flows through the liquid transfer line into the hydrogenotrophic methanogenesis bioreactor, and the hydrogen generated at the cathode flows through the hydrogen transfer line into the hydrogenotrophic methanogenesis bioreactor, where the bicarbonate and hydrogen are biologically converted to methane; the methane generated in the hydrogenotrophic methanogenesis bioreactor is vented through the second gas vent line and collected for later use; and aqueous fluid is recycled back into the inlet end of the electrochemical reactor from the hydrogenotrophic methanogenesis bioreactor through the liquid recycle line.

2. The system of claim 1 , wherein the primary anaerobic digester comprises:
(i) an acidogenesis reactor adapted and arranged to biologically convert organic waste and wastewater to soluble volatile fatty acids (VFA), methane, carbon dioxide, and hydrogen; and
(ii) an acetoclastic methanogenesis reactor adapted and arranged to biologically convert the VFA to carbon dioxide and methane;
wherein the gas transfer line is in fluid communication with both the acidogenesis reactor and the acetoclastic methanogenesis reactor; and the acidogenesis reactor is in fluid communication with the acetoclastic methanogenesis reactor via a liquid feed line; and
wherein in use, VFA, carbon dioxide, hydrogen and methane are generated in the acidogenesis reactor; VFA-containing liquid from the acidogenesis reactor is fed into the acetoclastic methanogenesis reactor via the liquid feed line; methane and carbon dioxide are generated in the acetoclastic methanogenesis reactor, and carbon dioxide, methane, and hydrogen are transferred from the acidogenesis reactor and the acetoclastic methanogenesis reactor into the inlet end of electrochemical reactor through the gas transfer line.

3. The system of claim 1 , wherein each of the reactor cells comprises at least one porous gas and liquid flow distributor in contact with the resin wafer thereof; the flow distributor being adapted and arranged to laterally distribute gas and liquid within pores thereof prior to entering the resin wafer of the electrochemical reactor.

4. The system of claim 3 , wherein the at least one porous gas and liquid flow distributor includes interconnected pores having an average pore size in the range of about 100 to about 600 micrometers, and is adapted and arranged to laterally distribute the liquid and gas bubbles having an average diameter in the range of about 100 to about 600 micrometers throughout the flow distributor and into the resin wafer of the electrochemical reactor.

5. The system of claim 1 , wherein the electrochemical reactor comprises at least one porous gas and liquid flow distributor in contact with at least one of the resin wafers in the stack; and the at least one porous gas and liquid flow distributor is adapted and arranged to distribute gas within the liquid flowing through the resin wafers of the electrochemical reactor.

6. The system of claim 5 , wherein the at least one porous gas and liquid flow distributor includes interconnected pores having an average pore size in the range of about 100 to about 600 micrometers, and is adapted and arranged to laterally distribute the liquid and gas bubbles having an average diameter in the range of about 100 to about 600 micrometers throughout the flow distributor and into the resin wafers of the electrochemical reactor.

7. The system of claim 1 , wherein each wafer has a thickness in the range of about 1 to about 20 mm.

8. The system of claim 1 , wherein the electrochemical reactor comprises 2 to about 50 reactor cells.

9. An electrochemical reactor for capturing carbon dioxide as bicarbonate and generating hydrogen; the reactor comprising a plurality reactor cells in a stack with each reactor cell including:
(a) an anode;
(b) a cathode spaced from the anode;
(c) a single porous ion exchange resin wafer between the anode and the cathode, wherein the ion exchange resin wafer consists of a basic ion exchange

Assignees

• Uchicago Argonne Llc

Inventors

• Lin Yupo J

Classifications

• B01D61/485

  Specific features relating to the ion-exchange material · CPC title

• B01D61/466

  comprising the membrane sequence BC or CB · CPC title

• B01D61/445

  with bipolar membranes; Water splitting · CPC title

• B01D2053/221

  Devices · CPC title

• B01D2273/10

  Allowing a continuous bypass of at least part of the flow, e.g. of secondary air, vents · CPC title