The present application is in the field of electrochemistry and carbon dioxide capture. More specifically, the present application relates to an electrochemical system and method for capturing carbon dioxide, regenerating purified carbon dioxide and/or converting the captured carbon dioxide to methane.
The concentration of atmospheric carbon dioxide is rapidly increasing. From the combustion of fossil fuels, coal, oil and natural gas, increased carbon dioxide levels are threatening life across the globe. Carbon capture and regeneration is a promising strategy to reduce greenhouse effects by reducing carbon dioxide emissions. Electrochemical conversion of carbon dioxide into fuels or other value-added chemicals from exhaust streams are vital to reducing greenhouse gas emissions.
Carbon dioxide absorbents and desorption technologies are pivotal to achieving this aim. Common carbon dioxide absorbents include amines such as monoethanolamine (MEA) and alkoxide salts of sodium, lithium, and potassium. NaOH as a CO2 absorbent outperforms organic absorbents, such as MEA with a faster reaction kinetics (Gong et al., 2006; Ye et al., 2015) and a higher absorption efficiency (Peng et al., 2012). It offers higher stability, lower cost, and lower environmental impact than amine solutions (Penders-van Elk et al., 2013; Ye et al., 2015). However, the application of NaOH is facing the challenge of CO2 desorption from the capture solution. Existing commercial routes utilize Ca(OH)2 to form CaCO3 from Na2CO3, which are then incinerated at 674° C. to release CO2 (Keith et al., 2018). Other than using the complex calcium-based thermochemical cycle, bipolar membrane electrodialysis (BPMED) is an alternative with the advantage of direct use of renewable energy, avoiding high temperature conditions, phase transitions and solid handling (Sabatino et al., 2020). Valluri and Kawatra (2021) found BPMED required less energy than that required for thermal regeneration. However, the high cost of the bipolar membrane (BPM) is a major constraint.
As such, there is a need to provide improved electrochemical systems for carbon dioxide capture that would overcome at least some of the drawbacks of existing technologies, that would be cost-effective, energy-efficient and versatile.
It has been shown herein that systems of the present application provide for cost effective and efficient alternatives to the expensive BPM-based regeneration of caustic solution for CO2 capture. The processes of the present application further provide for energy efficient and versatile methods.
Accordingly, the present application includes an electrochemical system for capturing carbon dioxide from a gas stream, the system comprising: an electrochemical cell comprising an anode chamber and a cathode chamber, where the cell contains an electrolyte solution; a cathode exposed to the electrolyte solution in the cathode chamber; an anode exposed to the electrolyte solution in the anode chamber; wherein the electrochemical cell is connectable to a power supply for electrically connecting the anode and the cathode to apply a potential difference between the anode and the cathode; a proton or cation exchange membrane separating the anode chamber and the cathode chamber allowing alkali metal ions formed at the anode to diffuse through the proton or cation exchange membrane towards the cathode to react with hydroxide ions to form an alkali metal base, a collection chamber to collect the alkali metal base from the cathode chamber; a source of the gas stream comprising carbon dioxide for contacting with the alkali metal base such that the carbon dioxide reacts with the alkali metal base to form a carbonate, and thus capture the carbon dioxide from the gas stream.
The present application also includes a method for capturing carbon dioxide from a gas stream is provided, comprising: applying a potential difference between an anode and a cathode in an electrochemical cell containing an electrolytic solution such that alkali metal ions are formed in the electrolytic solution at the anode, permitting the alkali metal ions to diffuse through a proton or cation exchange membrane between the anode and the cathode, towards the cathode to react with hydroxide ions to form an alkali metal base, separating the alkali metal base from the electrolytic solution, contacting the gas stream comprising carbon dioxide with the alkali metal base such that the carbon dioxide reacts with the alkali metal base to form a carbonate, thus capturing the carbon dioxide from the gas stream.
Accordingly, the present application further includes an electrochemical system for capturing carbon dioxide from a gas stream and generating methane, the system comprising: an electrochemical cell comprising an anode chamber and a cathode chamber, where the cell contains an electrolyte solution; a cathode exposed to the electrolyte solution in the cathode chamber; an anode exposed to the electrolyte solution in the anode chamber; a power supply electrically connected to the anode and the cathode configured to apply a potential difference between the anode and the cathode; a proton or cation exchange membrane separating the anode chamber and the cathode chamber allowing alkali metal ions formed at the anode to diffuse through the proton or cation exchange membrane towards the cathode to react with hydroxide ions to form an alkali metal base, a collection chamber to collect the alkali metal base from the cathode chamber; a source of the gas stream comprising carbon dioxide for contacting with the alkali metal base such that the carbon dioxide reacts with the alkali metal base to form a carbonate, and thus capture the carbon dioxide from the gas stream, a deoxygenation unit to remove dissolved oxygen from the carbonate solution to produce a deoxygenated carbonate solution, and a biomethane production module configured to receive the deoxygenated carbonate solution, the biomethane production module comprising biocatalysts to react with the carbonate to produce methane.
The present application also includes a method for generating methane by capturing carbon dioxide from a gas stream is provided, the method comprising: applying a potential difference between an anode and a cathode in an electrochemical cell containing an electrolytic solution such that alkali metal ions are formed in the electrolytic solution at the anode, permitting the alkali metal ions to diffuse through a proton or cation exchange membrane between the anode and the cathode, towards the cathode to react with hydroxide ions to form an alkali metal base, separating the alkali metal base from the electrolytic solution, contacting the gas stream comprising carbon dioxide with the alkali metal base such that the carbon dioxide reacts with the alkali metal base to form a carbonate, thus capturing the carbon dioxide from the gas stream; deoxygenating the carbonate with an aerobic bacterium, transferring the carbonate to biocatalysts for generating methane.
Other features and advantages of the present application will become apparent from the following detailed description. It should be understood, however, that the detailed description and the specific examples, while indicating embodiments of the application, are given by way of illustration only and the scope of the claims should not be limited by these embodiments, but should be given the broadest interpretation consistent with the description as a whole.
The embodiments of the application will now be described in greater detail with reference to the attached drawings in which:
Unless otherwise indicated, the definitions and embodiments described in this and other sections are intended to be applicable to all embodiments and aspects of the present application herein described for which they are suitable as would be understood by a person skilled in the art.
The terms “about”, “substantially” and “approximately” as used herein mean a reasonable amount of deviation of the modified term such that the end result is not significantly changed. These terms of degree should be construed as including a deviation of at least ±5% of the modified term if this deviation would not negate the meaning of the word it modifies or unless the context suggests otherwise to a person skilled in the art.
The systems of the application have been shown to serve as a cost effective and efficient alternative to the expensive BPM-based regeneration of caustic solution for CO2 capture.
Accordingly, the present application includes an electrochemical system for capturing carbon dioxide from a gas stream, the system comprising: an electrochemical cell comprising an anode chamber and a cathode chamber, where the cell contains an electrolyte solution; an air cathode exposed to the electrolyte solution in the cathode chamber; an anode exposed to the electrolyte solution in the anode chamber; a power supply electrically connected to the anode and the cathode configured to apply a potential difference between the anode and the cathode; a proton or cation exchange membrane separating the anode chamber and the cathode chamber allowing alkali metal ions formed at the anode to diffuse through the proton or cation exchange membrane towards the cathode to react with hydroxide ions to form an alkali metal base, a collecting chamber to collect the alkali metal base from the cathode chamber; a source of the gas stream comprising carbon dioxide for contacting with the alkali metal base such that the carbon dioxide reacts with the alkali metal base to form a carbonate, and thus capture the carbon dioxide from the gas stream.
In some embodiments, the system of the application comprises an electrochemical system with a three-phased air cathode and proton exchange membrane assembly (ACPEM) or a three-phased air cathode and cation exchange membrane assembly (ACCEM) for cost-effective caustic regeneration, in which H+ are continuously generated through anodic reaction and accumulated in the anode chamber, whereas the alkali metal cations cross the PEM or CEM to form the alkali metal base with OH-resulting from proton consuming cathodic reactions. The system generates pH differences between electrodes via hindering proton or cation transfer through PEM or CEM leveraging the abundant alkali metal cations in the CO2 capture solution. This design can incorporate either an abiotic anode (oxygen evolution reaction) or a biotic anode (acetate oxidation reaction).
In some embodiments, the cathode has a flow inlet and a flow outlet. In some embodiments, the cathode flow inlet is configured to receive the electrolyte solution and the cathode flow outlet is configured to transfer the alkali metal base generated away from the cathode towards the collecting chamber.
In some embodiments, the anode has a flow inlet and flow outlet. The anode flow inlet may be configured to receive the electrolyte solution or the captured CO2 solution that subsequently reacts with H+ to release the carbon dioxide. The anode flow outlet may be configured to allow release of the processed electrolyte solution or captured CO2 solution. Built up carbon dioxide in the anode headspace is released to a carbon reservoir or to a further processing unit.
In some embodiments, the anode is an abiotic anode wherein an oxygen evolution reaction takes place. In some embodiments, the anode is a biotic anode wherein an acetate oxidation reaction is catalyzed by respiring microorganisms takes place within the anode chamber. In some embodiments, the microorganisms may include Geobacter spp. or Shewanella spp. In some embodiments, the acetate ions are sourced from volatile fatty acids in a separate acetate reactor before being transferred to the anode. In some embodiments, the fatty acids in the acetate reactor react with carbonate to release carbon dioxide and form salts comprising sodium acetate. In some embodiments, the salts are directed to a ACPEM, ACCEM or BEMP. In some embodiments, the acetate ions are sourced from carbohydrate rich waste. In some embodiments, the acetate ions are sourced from a combination of fermentation and anaerobic digestion processes in a cost-effective manner. In some embodiments, the acetate ions are sourced from forestry and crop waste, wherein the combination of fermentation and anaerobic digestion processes generate acids while allowing residual material to be easily dried and compressed as pellets. In some embodiments, the acetate ions are sourced from wastewater from Fischer-Tropsch reaction, biomass pyrolysis, sugar processing, potato processing, etc. In some embodiments, the acetate ions are sourced from ethanol production to help reduce the carbon intensities of fuel ethanol. In some embodiments, the acetate ions are sourced from potato processing, fruit processing, or paper mill industry waste. In some embodiments, the acetate ions formed in the acetate reactor are subjected to deoxygenation before being transferred to the anode. In some embodiments, the acetate ions formed in the acetate reactor are transferred to a deoxygenation system before being transferred to the anode.
In some embodiments, the solution in the anode chamber has a pH from about 5 to about 7, or about 6 to about 7, or about 7.
In some embodiments, the solution in the cathode chamber has a pH of about 12 to about 14, or about 13 to about 14, or about 14.
In some embodiments, the cathode is an air cathode. In some embodiments, the air cathode is based on a carbon support such as carbon felt, activated carbon, black carbon, carbon cloth, or VULCAN carbon support having high porosity to facilitate air, water, and electrode interactions. In some embodiments, the carbon support is a nitrogen doped carbon support with a catalyst comprising Pt, Fe or Co. In some embodiments, the air cathode comprises an embedded current collector that increases power generation of fuel cells by decreasing cathodic charge transfer impedance. In some embodiments, the embedded current collector is made of an acid and alkaline resistant material comprising titanium or stainless steel.
In some embodiments, the cathode comprises a film including MnO2 deposited onto carbon felt. In some embodiments, the film is deposited via electrodeposition techniques.
In some embodiments, the cathode is a hydrogen evolution cathode. In some embodiments, the hydrogen evolution reaction is catalyzed by Pt.
In some embodiments, the electrolyte solution is an aqueous solution of the formula XnY wherein X is Na+, K+, or Li+, Y is SO42−, CO32−, HCO3−, and n is 1 or 2 or a combination thereof.
In some embodiments, the power supply is electrically connected to the anode and the cathode configured to apply a potential difference between the anode and the cathode. In some embodiments, the power supply is an external electric source or is recycled from a component of the system. In some embodiments, the power supply is recycled when the anode of the ACPEM or ACCEM with biotic anode is configured to be connected to the cathode of a BPMED; and the cathode of the ACPEM or ACCEM with biotic anode is configured to be connected to the anode of a BPMED. In some embodiments, the potential difference is from about −0.9V to about 0.75V, or about −0.85V to about 0.7V, or about −0.8V to about 0.65V, or about −0.75 to about 0.6V, or about −0.7V to about 0.55V.
In some embodiments, the proton or cation exchange membrane is selected from pure polymer membranes and composite membranes. The proton or cation exchange membrane may be a semipermeable membrane comprising perfluorinated sulfonic acid ionomer structures. The PEM/CEM may be selected from Nafion®, Flemion®, Aciplex®, Pemion®, Cemion®, Fumapern®, Fujifilm® as well as sulfonated poly (ether ether) (SPEEK) and PVA-Nafion-borosilicate.
In some embodiments, the alkali metal ion is Na+, K+, Li+ or combinations thereof.
In some embodiments, the gas stream is sourced from the combustion of fossil fuels, coal, oil and/or natural gas, for example from an energy production process.
In some embodiments, the gas stream is air, exhaust gas, flue gas produced during the combustion of fossil fuels, coal, oil and/or natural gas for energy production.
In some embodiments, the collecting chamber is an external container used to collect the generated alkali metal base solution. In some embodiments, the collecting chamber is configured to allow the liquid to be directed in or out of the ACPEM, ACCEM or BEMP using a transferrer. In some embodiments, the transferrer operates by mechanical action or gravity. In some embodiments, the alkali metal base in the collecting chamber is transferred to a gas contactor housed in a carbon capture unit to contact the gas stream comprising carbon dioxide such that the carbon dioxide reacts with the alkali metal base to form a carbonate, and thus capture the carbon dioxide from the gas stream. In some embodiments, the carbonates formed therein are stored in a carbon reservoir for further processing. In some embodiments, further processing comprises CO2 release, deoxygenation, combinations thereof or any systems requiring a CO2 input. In some embodiments, the carbon capture unit is a system configured to allow efficient gas-liquid contact, i.e. contact between the gas stream and the alkali metal base solution.
In some embodiments, CO2 release is carried out by returning the carbonates solution to the anode chamber to react with the H+ generated at the anode, and thus release the CO2. In some embodiments, the released CO2 is directed to a gas processing system comprising a carbon dioxide storage container for optionally dewatering, purification and/or purity analysis before being compressed for transportation, utilization, or storage.
In some embodiments, the system further comprises a transferrer for bringing the alkali metal base from the collecting chamber to a gas contactor of a carbon capture unit configured to bring the gas stream in contact with the alkali metal base. In some embodiments, the transferrer may also bring captured carbon dioxide in the form of carbonate that is generated in a ACPEM or ACCEM biotic anode system to a deoxygenation system and/or subsequently to the anode to react the carbonate with hydrogen ions and release carbon dioxide. In some embodiments, the transferrer may bring the captured carbon dioxide to a further processing system selected from purification and compression processes. In some embodiments, the transferrer operates by mechanical action or gravity. In some embodiments, the transferrer is selected from a peristatic pump, a pressure driven flow control pump, a diaphragm pump, a centrifugal pump or combinations thereof. In some embodiments, the transferrer is operatively connected at each stage of the system for transferring the respective solutions/products to a next stage. In some embodiments, fluid communication between each stage of the system is provided by suitable tubes or pipes, or the like.
Without being bound to theory, the versatility of the system of the application allows it to work in conjunction with other systems requiring a CO2 input, such as a bioelectrochemical methane production (BEMP) module, wherein the captured CO2 solution in the form of carbonates can be introduced to BEMP after pH monitoring and deoxygenation. In some embodiments, the pH is monitored with a pH meter or the like, to determine the reaction end point. The introduction of CO2 in bicarbonate form to BEMP may present at least one of four (4) advantages: 1) realization of direct synergy between carbon capture and BEMP.
In some embodiments, before the carbonate solution generated from CO2 capture can be applied to a biotic anode or a BEMP, the dissolved oxygen level may need to be reduced to protect oxygen sensitive anode respiring bacteria and methanogens. In some embodiments, a biological deoxygenation unit is designed and incorporated in the system of the application. In some embodiments, the deoxygenation unit takes advantage of Halomonas alkaliphila, an aerobic bacterium with high XHCO3/X2CO3 tolerance (where X is alkali metal cation), to consume dissolved oxygen in the capture solution.
In some embodiments, the deoxygenation unit comprises carbonate tolerant aerobic bacterium including Halomonas alkaliphila or other carbonate tolerant bacteria.
Overall, the ACPEM/ACCEM of the present application with an abiotic or biotic anode may serve as an alternative to the expensive BPM-based regeneration of caustic solution for CO2 capture, in which low-cost PEM/CEM and MnO2 coated carbon felt replace expensive BPM and associated catalysts. Without being bound to theory, the air cathode instead of hydrogen evolution cathode allow lower onset voltage and energy consumption. When using a biotic anode, volatile fatty acids (VFA) generated from carbohydrate rich waste can be incorporated to regenerate the caustic solution, release captured and generated CO2, and generate current/voltage to support other energy consuming processes. Coupling CO2 capture coupled with BEMP via direct reduction of bicarbonate provides a synergic solution to both technologies. The combined process of ACPEM/ACCEM of the present application with biotic anode and BEMP was achieved, coupling CO2 capture and biomethane production with superior pH management, biocatalyst efficiency, and product mixture (CO2 and CH4) separation to traditional anaerobic digestion. Lastly, a cost-effective biological deoxygenation unit may be incorporated to protect oxygen sensitive methanogens and anode respiring microbes in the downstream processes.
The present application further provides methods and uses of an electrochemical system to capture carbon dioxide, regenerate a purified stream of carbon dioxide and/or couple captured carbon dioxide as carbonates to a module to produce purified methane, syngas, formic acid, and combinations thereof.
Accordingly, the present application includes a method for capturing carbon dioxide from a gas stream, the method comprising: generating an alkali metal base in an electrochemical cell comprising an anode chamber and a cathode chamber, where the cell contains an electrolyte solution; an air cathode exposed to the electrolyte solution in the cathode chamber; an anode exposed to the electrolyte solution in the anode chamber, and a proton/cation exchange membrane separating the anode chamber and the cathode chamber, by applying a potential difference between the anode and the cathode such that alkali metal ions are formed at the anode and diffuse through the proton/cation exchange membrane towards the cathode to react with hydroxide ions to form the alkali metal base, transferring the alkali metal base from the cathode chamber to a collecting chamber; contacting the gas stream comprising carbon dioxide with the alkali metal base such that the carbon dioxide reacts with the alkali metal base to form a carbonate, thus capturing the carbon dioxide from the gas stream.
In some embodiments, the transferring of the alkali metal base from the cathode chamber to the collecting chamber is carried out by a transferrer.
In some embodiments, the method further comprises storing the generated carbonate solution in a carbon reservoir container. In some embodiments, the method further comprises transferring the carbonate solution to the anode chamber to be reacted with H+ and release the carbon dioxide. In some embodiments, the method further comprises transferring the carbonate solution to an external container housing volatile fatty acids wherein the acids react with carbonate to release carbon dioxide. In some embodiments, the method further comprises transferring the carbonate solution to a deoxygenation unit. In some embodiments, the method further comprises transferring the carbonate solution or deoxygenated carbonate solution to a further processing unit. In some embodiments, the further processing unit comprises purifying or compressing the carbonate solution.
The following non-limiting examples are illustrative of the present application.
In principle, ACPEM/ACCEM utilizes the abundant Na+ (e.g. 4 M in abiotic anode) in the anode chamber to compete with scarce protons (H+) (e.g. 10−7 M at neutral pH) for the PEM/CEM. The competition hinders the crossover of H+ through the PEM. H+ continuously generated through anodic reaction is then accumulated in the anode chamber, whereas Na+ cross the PEM/CEM to form NaOH with OH− resulting from proton/cation consuming cathodic reactions. The end-result is higher pH at the cathode and lower pH at the anode. In this design, instead of using a hydrogen evolution reaction, which is typically used in BPMED at the cathode, an air cathode is utilized to provide a thermodynamically favorable conditions coupling with either an abiotic oxygen evolution reaction or a biotic acetate oxidation reaction in the anode chamber. When compared with the work of Bouwman et al. (2018), which generates NaOH along with their reduced products (e.g. methanol and formic acid) at the cathode, this design avoids the downstream separation of products and the regenerated caustic solution.
As illustrated in
Further illustrated in
The ACPEM/ACCEM assembly can be integrated with either an abiotic anode catalyzing oxygen evolution reaction or a biotic anode catalyzing acetate oxidation. When compared with BPMED, which needs at least 0.83 V across a BPM at which water dissociation takes place when starting from a 1 M salt solution, ACPEM combined with an abiotic anode requires lower onset voltage from a thermodynamic point of view. When using a biotic anode, the reactions are spontaneous with electricity output.
Without wishing to be bound to theory, PEM/CEM facilitated the transport of both Na+ and H+. When using 1 M Na2SO4 and 1 M Na2CO3 as the electrolyte, the concentration ratio of Na+/H+ was 4×107. This large concentration difference limited the transportation of H+ through the PEM/CEM, which leads to acidification of the anode solution. In this design, as the anode can become an acidic environment, an oxygen evolution reaction catalyst that is acid tolerant was employed. An exemplary choice is a cost-effective and stable manganese oxybromide (Mn7.5O10Br3) catalyst (Pan et al., 2022). The accumulated H+ will react with Na2CO3 generated from CO2 capture to allow the release of CO2 (
As shown in
In the CO2 regeneration process, the constituents of the CO2·H2O/HCO3−/CO32− buffer system shifts with pH values. Higher pH values led to the presence of higher concentration of HCO3− and reduced the percentage of CO2 released (
where:
pKa H
During the CO2 regeneration process, the headspace had much higher CO2 concentration than air (˜60%), leading to a high pCO
ACPEM/ACCEM with a biotic anode utilizes acetate oxidation reaction catalyzed by anode respiring microorganisms (e.g., Geobacter spp. and Shewanella spp.). These microbes use the electrode as the electron accepter of their acetate oxidation reaction to complete the electrochemical reaction (
A carbohydrate rich organic waste source such as those from sugarcane processing, potato processing, fruit processing and/or the paper mill industry is subjected to fermentation to produce volatile fatty acids (VFAs, e.g., acetic acid) solutions. Other sources of VFAs and their precursors include Fisher-Tropsch reaction water, pyroligneous acid, agricultural waste and waste from sustainable forestry management. Such solutions acidified Na2CO3 solution from the CO2 capture process and allowed the release of CO2. The primary content in the resulting solution was acetate, after dilution to a suitable concentration (˜200 mM) that serves as an excellent fuel (carbon and energy source) for the anode respiring microbes (e.g., Geobacter spp.). Following the mechanisms illustrated in
In another embodiment, an electrochemical cell, comprising an anode chamber comprising an anode, an anode outflow container and a cathode chamber comprising a cathode, is connected to an electrical load or battery that is electrically connected to the anode and the cathode through electrical wires to apply a potential difference between the anode and the cathode. The cathode comprises an embedded current collector that increases power generation of fuel cells by decreasing cathodic charge transfer impedance. A proton/cation exchange membrane separates the anode chamber and the cathode chamber that allows alkali metal ions formed at the anode to diffuse through the proton/cation exchange membrane towards the cathode to react with hydroxide ions to form alkali metal base. A water container supplies a small stream of water through a first flow controller and first silicone tube to the inlet of the cathode chamber to carry resulting alkali metal base to a NaOH solution container that is transferred by a pump to the carbon capture unit. Carbon dioxide is captured in a carbon capture unit by reacting with the NaOH to form carbonates that are then directed towards a Na2CO3/NaHCO3 solution container. The carbonates are directed to a neutralization reactor to react with an organic acid solution, particularly acetic acid, to produce the first stream of CO2 that is detected by a CO2 sensor. The pH of the waste sodium acetate solution is monitored with a pH sensor. The first stream of CO2, which is from air capture, is then transferred to a CO2 storage container. The neutralized sodium acetate solution is deoxygenated with a deoxygenation unit when necessary. A dissolved oxygen sensor is equipped with the deoxygenation unit. The (deoxygenated) sodium acetate solution is transferred through a second flow controller and a second silicone tube back to the anode chamber of the electrochemical cell to be oxidized by anode respiring microorganisms and to react with the H+ ions to release the second stream of CO2. The second stream of CO2 is biogenic and from acetate oxidation. A CO2 sensor detects carbon dioxide released at the anode that is subsequently transferred to CO2 gas storage container. Additional flow controllers may be incorporated herein to control liquid phase flow, for example organic acid solution and the neutralized sodium acetate solution as would be understood by a person skilled in the art.
The hydrogen ions that are used to release the first stream of CO2 can be from organic acid (e.g., acetic acid) sourced from carbohydrate rich waste streams from pulp and paper processing, Fischer-Tropsch reaction, biomass pyrolysis, sugar processing, potato processing etc. This leads to waste reduction from these industries, while providing high purity CO2 capture from both air capture and acetate oxidation. The captured CO2 can be sequestrated for emission reduction credits or utilized for beverage making, concrete curing, dry ice production, and aviation fuel synthesis, etc. Overall, this approach allows valorization of waste streams into values for the industries. It can also be sourced from ethanol production. After conversion a fraction of ethanol to acetic acid to drive emission reduction from CO2 removed from both air capture and acetate oxidation, the carbon intensity scores of the remaining ethanol-based fuel products can be significantly reduced to boost their values.
Following the neutralization, the primary component in the resulting solution was acetate, after dilution to a suitable concentration (˜200 mM) that serves as an excellent fuel (carbon and energy source) for the anode respiring microbes (e.g., Geobacter spp.). Following the mechanisms illustrated in
Acetate itself is oxidized into CO2 anaerobically at the anode by the anode aspiring microorganisms, which allows a second CO2 stream to be evolved and captured. This increases the total quantity of CO2 captured per cycle. The generated H+in the anode is of lower concentration compared to the conditions in ACPEM/ACCEM with abiotic anode, which is buffered against both the CH3COO−/CH3COOH and HCO3−/H2CO3 buffer systems, maintaining a pH around 6.5. At slightly acidic conditions, a larger portion of the produced CO2 from the acetate oxidation reaction can be released and harvested through the off-gas collection. Additionally, rough vacuum can be applied to extract more CO2 that is dissolved in the solution by leveraging Henry's law. In the testing conditions, a power output of 2.25 w/m2 was observed, which drove the generation of 247 L of 1M NaOH solution per kwh. The captured CO2 from both streams were found with purity >97%. Steady performance was observed for 3 months of operation.
The BEMP as well as biological methane synthesis have been both traditionally operated with gaseous CO2. However, as illustrated in
Without being bound to theory, this operational route also has the advantages of 1) bypassing the kinetic limiting step of the mass transfer of gaseous CO2 to the liquid phase (Simon et al., 2018); 2) higher effective CO2 concentration (buffered in bicarbonate form) leading to reduced Gibbs free energy for CO2 reduction; and 3) bicarbonate serving as cost-effective buffer and improving conductivity for a bioelectrochemical system (Fan et al., 2007; Wang et al., 2022).
The involvement of Na2CO3/NaHCO3 demands the biocatalysts (methanogens) to be moderately Na+ tolerant. Table 1 summarizes the methanogens capable of adapting to a Na2CO3/NaHCO3 based BEMP. Among these species, Methanococcus maripaludis (mesophilic), Methanobthermobacter marburgenesis, Methanothermococcus okinawensis (thermophilic), and Methanotorris igneus (hyperthermophilic) are the most potent producers generating methane at the highest rates. These strains can be spiked to the mixed culture to allow effective methane generation. The concentration of Na2CO3/NaHCO3 added to the system varies according to the physiology of the biocatalysts, while at least a level of 200 mM is recommended.
The Na2CO3/NaHCO3 based BEMP is suitable to work in conjunction with ACPEM/ACCEM and biotic anode-based CO2 capture (
Without wishing to be bound to theory, although the theoretical cell voltage of this pair of reactions is −0.24V−(−0.28V)=0.04V (>0), the reaction is not spontaneous, due to the overpotentials in the system. Therefore, an external power source such as ACPEM/ACCEM and biotic anode, or power from the grid can be used to drive the reaction. Acetoclastic methanogenesis and hydrogen evolution reactions also occurred in this BEMP. The equilibriums of these reactions reached at various applied voltage/current levels and PH levels. A slightly alkaline condition (pH=7.5-8) is maintained to allow most of the generated CO2 to stay in the bicarbonate form and release a high purity CH4 (>90%). The resulting bicarbonate solution can be recycled through the CO2 regeneration/pH adjustment process (
Methanobacterium
aahusense
alcaliphilum
beijingense
ferruginis
kanagiense
lacus
movilense
Methanobrevibacter
boviskoreani
millerae
Methanobthermobacter
crinale
thermoauto-
trophicus
thermoflexus
Methanocaldococcus
fervens
bathoardescens
Methanotorris
formicicus
Methanococcus
vannielii
voltae
aeolicus
Methanothermococcus
thermolitho-
trophicus
Methanofollis
formosanus
liminatans
Methanogenium
frigidum
marinum
Methanolaciania
petrolearia
For the carbon capture solution to be an effective feedstock for BEMP, significant reduction of dissolved oxygen level in the CO2 capture solution is crucial (
As both anode respiring microbes and methanogens are sensitive to oxygen toxicity, dissolved oxygen in the carbon capture solution should be significantly reduced. A deoxygenation unit was placed after the mixing of VFAs with Na2CO3 as shown in
The mixing speed was not found as a significant factor on the oxygen consumption and final DO. Static operation showed satisfactory performance while saving energy cost. pH values of 8 and 9 showed more promising outcomes than pH 10. Higher tube numbers lead to improved operational outcomes.
While the applicant's teachings described herein are in conjunction with various embodiments for illustrative purposes, it is not intended that the applicant's teachings be limited to such embodiments as the embodiments described herein are intended to be examples. On the contrary, the applicant's teachings described and illustrated herein encompass various alternatives, modifications, and equivalents, without departing from the embodiments described herein, the general scope of which is defined in the appended claims.
The present application is a continuation-in-part of PCT/CA2024/050385 filed Mar. 27, 2024, which claims the benefit of priority of U.S. Provisional Patent Application No. 63/455,646, which was filed Mar. 30, 2023, the contents of which are incorporated herein by reference in their entirety.
Number | Date | Country | |
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63455646 | Mar 2023 | US |
Number | Date | Country | |
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Parent | PCT/CA2024/050385 | Mar 2024 | WO |
Child | 18904990 | US |