WO2017021083A1 - Procédé de fabrication d'un gaz combustible et installation de production de gaz combustible comprenant un système électrolytique pour le traitement électrochimique du dioxyde de carbone - Google Patents

Procédé de fabrication d'un gaz combustible et installation de production de gaz combustible comprenant un système électrolytique pour le traitement électrochimique du dioxyde de carbone Download PDF

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Publication number
WO2017021083A1
WO2017021083A1 PCT/EP2016/065778 EP2016065778W WO2017021083A1 WO 2017021083 A1 WO2017021083 A1 WO 2017021083A1 EP 2016065778 W EP2016065778 W EP 2016065778W WO 2017021083 A1 WO2017021083 A1 WO 2017021083A1
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Prior art keywords
carbon dioxide
gas mixture
reactor
product gas
cathode
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PCT/EP2016/065778
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German (de)
English (en)
Inventor
Günter Schmid
Maximilian Fleischer
Christoph Kiener
Michael Weinhold
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Siemens Aktiengesellschaft
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Publication of WO2017021083A1 publication Critical patent/WO2017021083A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M21/00—Bioreactors or fermenters specially adapted for specific uses
    • C12M21/04—Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M43/00—Combinations of bioreactors or fermenters with other apparatus
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M43/00—Combinations of bioreactors or fermenters with other apparatus
    • C12M43/04—Bioreactors or fermenters combined with combustion devices or plants, e.g. for carbon dioxide removal
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
    • C12M47/18—Gas cleaning, e.g. scrubbers; Separation of different gases
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/02—Hydrogen or oxygen
    • C25B1/04—Hydrogen or oxygen by electrolysis of water
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis

Definitions

  • the present invention relates to a production process for a fuel gas. Moreover, the present invention relates to a plant for producing a fuel gas.
  • the gas mixture produced in bioreactors of biogas plants contains approximately 55% methane (CH 4) to the 45% carbon dioxide (C02) and various marks such as pivoting ⁇ hydrogen sulphide (H 2 S) or amines.
  • CH 4 methane
  • C02 carbon dioxide
  • various marks such as pivoting ⁇ hydrogen sulphide (H 2 S) or amines.
  • the biogas in this together ⁇ men experience thus can not be fed into the natural gas network.
  • the carbon dioxide from the biogas must be almost completely removed and the missing proportion of higher homologous Ga ⁇ se, such as ethane, propane or butane, which provide for the increase of heating or calorific value , so far has to be compensated expensive.
  • the necessary separation of the carbon dioxide from the bio ⁇ gas has the further disadvantage that by its emission into the atmosphere, a further contribution to climate damage by carbon dioxide takes place.
  • a natural carbon dioxide reduction will be beispielswei ⁇ se through photosynthesis.
  • carbon dioxide are reacted to form carbohydrates.
  • This process is not easily adaptable on an industrial scale.
  • a copy of the natural photosynthesis process with large-scale photocatalysis has not yet been sufficiently efficient. Even with less than 1%, the photosynthesis itself is not exactly efficient.
  • the present invention production process for a fuel gas comprises a first step in which a catholyte is performed in a catholyte, the catholyte as well as coals ⁇ dioxide are introduced into a cathode compartment and in Contact with a cathode are brought where at least a portion of the carbon dioxide is reduced to carbon monoxide, for this first step, an electrolysis system for carbon dioxide utilization is used.
  • a first product gas mixture, it is used in this electrolysis system produces, has which carbon monoxide and hydrogen gas ⁇ , wherein the first product gas mixture is then transferred into a reactor.
  • Her ⁇ position method for a fuel gas also includes a second step in which at least a part of the first Pro ⁇ duktgasgemisches in the reactor to a second
  • Nowgasge ⁇ is reacted mixture, which is gaseous, in particular short-chain, having hydrocarbons, in particular propane (C 3 H 8 ) and / or butane (C 4 H 10 ).
  • this second product gas mixture is then added to a supply of methane-containing gas (CH 4 ).
  • Short-chain hydrocarbons are to be understood as meaning aliphatic hydrocarbon compounds having chain lengths of up to seven carbon atoms.
  • a reactor is to be understood in particular as meaning a chemical reactor which is designed such that chemical processes can take place therein or chemical reactions can be carried out therein. It may be, for example, a stirred tank or a flow tube, which is suitable as a flow reactor. Depending on which type of reaction is to take place in the reactor, it may be a reactor which is highly heat-resistant, for example, for exothermic reactions or via which heat can be added or removed to a reaction. It may be a high-pressure reactor or the reactor may be adapted to various chambers, tubes, etc. a preferred chemical reaction sequence.
  • the production process according to the invention has the advantage of further processing carbon dioxide into a valuable material.
  • the production method comprises a preceding step in which biomethane is produced from biomass in a bioreactor.
  • a bioreactor is, for example, a fermenter to understand how it is preferably used in biogas plants.
  • the biomass is degraded in an anaerobic process in several steps to biogas and a digestate.
  • the fermenter is a container that is normally airtight and has, for example, an agitator and various measuring and control technology devices to control the process.
  • biomass of any kind is suitable.
  • waste as well as renewable raw materials are fermented in bioreactors.
  • the resulting biogas is a combustible gas. This comprises first about 55% methane (CH 4) and around 45% carbon dioxide (C0 2) and various tracks as in ⁇ game as hydrogen sulfide or amines.
  • the manufacturing process comprises a further preceding step, in the biogas produced as described, the carbon dioxide contained is withdrawn and this carbon dioxide is fed to the electrolysis system for carbon dioxide utilization.
  • the production process comprises a further preceding step: After the removal of the carbon dioxide from the biogas, the remaining biomethane is supplied to the supply of methane-containing gas. First biogas from the fermentation of biomass Ver ⁇ is generated, this biogas is then removed from the ent ⁇ preserved carbon dioxide and this Kohlenstoffdio- xid is fed to the electrolysis system for carbon dioxide utilization.
  • biomethane a combustible gas mixture which has at least 96 mol% methane (CH 4 ).
  • CH 4 methane
  • Ge ⁇ meinhin is spoken of biomethane, even if the Biomethangasgemisch still traces such as hydrogen sulfide (H 2 S), but which are quantitatively below 0.01 mol%, predominantly in the ppm range. Where ppm is parts per million and 1 ppm is 0.0001%.
  • This variant of the manufacturing process has the advantage of being able to completely extract fuel gas from biomass.
  • the extraction of the carbon dioxide from the biogas can, for example, via an amine scrubbing, by means of aminoethanol compounds or amino acids or alternatively via a
  • the electrical energy for the carbon dioxide electrolysis for example, from renewable
  • the carbon dioxide utilization can be operated in times in which electric current from volatile energy sources is available or, for example, the carbon dioxide electrolysis can be coupled even at times of Stromüberschreibs, regardless of which source. Preferably, the entire Where necessary, renewable energy sources.
  • the manufacturing method in the first step is operated or the electrolysis system ⁇ is turned so that the first product gas mixture beside Kohlenstoffmo- monoxide and hydrogen gas and a proportion of Kohlenstoffdio- oxide of at least 0.1 vol .-% by weight.
  • the proportion of carbon dioxide in the first product gas mixture is at least 1% by volume, advantageously between 1% by volume and 5% by volume, preferably at least 3% by volume.
  • the Synthesegasge- would be mixed down to the ppm range free of carbon dioxide.
  • the Rectisol process for example, a physical sour gas scrubbing, supplies purified synthesis gas mixtures whose residual carbon dioxide content is between 2 ppm by volume and 3% by volume.
  • the components of the first ⁇ Ferngasgemi ⁇ ULTRASONIC are generated in a common electrolysis step.
  • the current density at the cathode and / or the pressure and / or the temperature in the cathode space are used as control parameters for the composition of the first product gas mixture.
  • the temperature is preferably varied between 5 ° C and 130 ° C, the pressure between atmospheric pressure and 40bar.
  • the joint production has the advantage that only one only peo ⁇ ger electrolyzer is needed the advantage.
  • aqueous electrolytes at atmospheric pressure and room temperature, a maximum of 3 g carbon dioxide dissolve per 1000 g solution, ie 0.3 percent by weight. If the electrolyzer is operated at (too) high current density, the additional competition reduction reaction Conversion of water to hydrogen gas at the cathode instead.
  • the current density forms a Regelparame ⁇ ter for the production of the desired carbon monoxide-water serstoff-gas mixture.
  • the control parameters are selected so that in the first product gas mixture is also still a carbon dioxide content.
  • carbon monoxide and hydrogen can be produced in different electrolysis steps , or in different electrolysis units, and combined in the desired composition to produce the first product gas mixture.
  • the division into two electrolysis ⁇ steps provides the advantage to adjust the electrolysers optimally to the respective reduction reaction and to exit from the system for the folic gerea excess carbon monoxide or hydrogen ⁇ gas before they are combined for the first product gas mixture in order to use this otherwise.
  • This alternative is of particular advantage for large-scale plants where less attention is paid to investment costs but much more emphasis is placed on energy efficiency. Because especially for the reduction reaction to hydrogen gas in the carbon dioxide electrolyzer energy-consuming high overvoltage is needed.
  • the second step of the Heinrichsver ⁇ driving a Fischer-Tropsch synthesis is driven by means of which at least a portion of the product gas mixture is reacted in the reactor in a second product gas mixture, which then comprises gaseous hydrocarbons, in particular propane and / or butane.
  • this second product gas mixture can be supplied to the methane reservoir, for example directly, that is to say without an intermediate step for purification.
  • a Fischer-Tropsch reactor is typically introduced ⁇ sets.
  • Fischer-Tropsch synthesis sometimes referred to as Fischer-Tropsch processes, refers to a large-scale coal liquefaction process.
  • a reactor suitable for the Fischer-Tropsch process thus has a feed for the coal or the synthesis gas, a steam outlet, a gas outlet, which preferably passes directly to a gas scrubber, a water jacket for cooling, a drive for a distributor as well as a rotary grate and an ash sluice.
  • a variety of Kataly ⁇ catalysts is used. The most commonly used are based on the transition metal cobalt, iron, nickel and ruthenium.
  • the carriers used are porous metal oxides with large specific surface areas such as kieselguhr, aluminum oxide, zeolites and titanium dioxide.
  • the present synthesis step is not concerned with the production of long-chain hydrocarbons or methanol but is of particular interest for the short-chain hydrocarbons, it is possible to work with less suitable or poisoned catalysts, as arise when the carbon dioxide content of the synthesis gas mixture is too high more than 3 vol .-% is present.
  • the production process can be operated, for example, even at higher capacity so that in the same system used an excess of liquefied gases is generated, which are then not supplied to the methane, son ⁇ countries separately discharged, stored or stealver ⁇ can be evaluated.
  • the invention has the further advantage that to further utilize exhaust carbon dioxide equal ⁇ time resulting from biogas production in order to avoid the emission into the atmosphere, and this while essential important gen materials for fuel gas production to further process.
  • Zinc, palladium and gallium cathodes almost exclusively reduced to carbon monoxide, formed on a Kupferka ⁇ method, a variety of hydrocarbons as reaction products.
  • the table shows Faraday efficiencies [%] of products produced by carbon dioxide reduction on various metal electrodes. The values given apply to a 0.1 M potassium bicarbonate solution as electrolyte and current densities below 10 mA / cm 2 .
  • silver-containing and / or copper-containing cathodes and / or catalysts are preferably used in the electrolysis system.
  • the catholyte preferably has water in the first step.
  • the reactor is operated in the second step of the method according to the invention so that the second product gas mixture in addition to propane and / or butane also has ethane and / or pentane.
  • the simultaneous generation of several different higher homologs of methane is advantageous for the most accurate adaptation of the fuel gas composition to each currently fed into the natural gas network fuel gas relationship ⁇ widening the number of possible catalysts.
  • the invention also includes a plant for producing a fuel gas, which has an electrolysis system for carbon dioxide utilization.
  • This electrolysis system comprises an electrolyzer with an anode in an anode chamber, a cathode in a cathode compartment, said cathode compartment comprising at least one access for carbon dioxide and is ⁇ staltet to bring the, OBTAINED carbon dioxide in contact with the cathode, where it at least partially to Koh is reduced lenmonoxid, the plant having a first gas ⁇ line, which is connected to the electrolyzer and configured, a first product gas mixture from the cathode Lyt Vietnameselauf the electrolyzer and refer to a Re ⁇ actor.
  • the plant comprises a reactor which is designed to implement the first product gas mixture in a second product gas mixture and the system includes a methane reservoir, which is connected via a second gas line to the reactor, that the second envisiongasge ⁇ mixed are fed to the methane reservoir can.
  • the invention embodied in this way has the advantage that carbon dioxide can be utilized electrochemically and can be converted into recyclables which upgrade methane in a methane reservoir to a fuel gas.
  • the methane reservoir can be connected to a bioreactor so that it can be fed from the bioreactor with biomethane. This has the advantage that in addition to the carbon dioxide utilization for the production of fuel gas biomethane can be obtained from biomass and can be further processed to Biobrenngas.
  • the methane reservoir can be connected to a synthesis reactor so that it can be fed from the synthesis reactor with synthetically produced methane.
  • a Fischer-Tropsch reactor is preferred as the reac tor ⁇ used.
  • the system described can be modified by one or more additional ⁇ Liche reactors so that in addition to the fuel gas for feeding into the natural gas network or alternatively other products can be produced.
  • the previously easiest way to use biogas is the ⁇ sen direct electricity through an internal combustion engine and generator. Higher profits have so far been achieved by being cached and only at times of high electricity prices a recuperation took place.
  • the use in the natural gas network is actually the most sensible option, because it saves fossil resources.
  • Figure 1 shows an arrangement of a biogas plant with a
  • Figure 2 shows a three-chamber construction of a Elektrolysezel ⁇ le with gas diffusion electrode
  • FIG. 3 shows a PEM structure (polymer electrolyte membrane) of an electrolysis cell
  • FIG. 4 shows a greatly enlarged illustration of a gas diffusion electrode (GDE).
  • GDE gas diffusion electrode
  • Figure 1 schematically shows an example of a system in which,, is generated in addition to a Kohlestoffdio- xidreduktionshim biogas as described, which are then provided with ⁇ means of the higher homologous, the evaluation of the Kohlenstoffdioxidver-, on a fuel gas with Einspei ⁇ sequency is upgraded.
  • a power plant K reg is initially displayed sym ⁇ bolisch, which is preferably produced from an electrical regenerati ⁇ ven energy source such as solar, wind, water power or current I.
  • This current I is made available, for example, at least to the electrolysis system 1. Additionally or alternatively, excess current from another source can also be used.
  • the electrolysis system 1 comprises a voltage source U for the electrolyzer comprising an anode A in an anode space AR, a cathode K in a cathode space KR, and two separate electrolyte circuits, an anolyte circuit AK passing through the anode space AR, such as a catholyte circuit KK through the cathode space KR runs.
  • Anolyte and catholyte side are connected to each other via a membrane M, which runs between the anode AR and cathode chamber KR.
  • a membrane M which runs between the anode AR and cathode chamber KR.
  • Pump P but possibly also several pumps P equipped in the course, which ensure a continuous flow of electrolyte through the electrolysis chambers AR, KR.
  • Electrolysis educts to the electrodes A, K introduced and
  • Electrolysis products discharged from the electrolyzer Ka ⁇ tholyt Vietnameselauf KK also a Edukteinlass EE and be ⁇ vorzugt a substrate reservoir ER is provided through which the carbon dioxide CO 2 in the electrolyte can be metered.
  • the electrolysis products and by-products can the
  • Circuits AK, KK are taken. For this purpose, for example Gasabscheidebecken GA in both circuits AK, KK are provided.
  • a by-product is withdrawn via a product outlet NPA, which can be, for example, oxygen gas O 2 or chlorine gas Cl 2 , depending on which electrolyte and which anode material is used.
  • a product mixture is the product outlet PA preferably taken which carbon monoxide CO, What ⁇ hydrogen gas H 2, and for example also a small residual percentage unveriretem carbon dioxide CO 2 contains.
  • Product gas mixture from the KAT catalytic cycle is then indicated by means of a successive arrow to a Fischer-Tropsch reactor 2.
  • the Fischer-Tropsch reactor 2 has at least one steam outlet DA and a product outlet for gaseous products PA.
  • the product gas mixture from the CO 2 electrolyzer 1 is introduced into the Fischer-Tropsch reactor 2 via a synthesis gas inlet SGE.
  • propane and butane are preferably produced.
  • Steam inlet and outlet DE, DA can also be used for heat regulation or alternatively for cooling. For example, any excess heat from other steps can be used.
  • the gas product produced in the Fischer-Tropsch reactor 2 now contains at least propane and butane.
  • the product gas from the Fischer-Tropsch reactor 2 which contains Bu tan C 4 H 10 and propane C 3 H 8 and ethane C 2 H 6
  • a gas mixture is generated, that in about the 55% methane CH 4 , about 45% carbon ⁇ dioxide gas CO2 and various traces, such as hydrogen sulfide H2 S has.
  • This product mixture can not yet be fed into the natural gas grid.
  • the carbon dioxide CO2 has to be removed from it, which can be carried out, for example, by amine scrubbing with aminoethanol compounds and amino acids or, alternatively, by pressure swing absorption with water and methanol.
  • the thus separated carbon dioxide is then Koh ⁇ lenstoffdioxid-recovery unit, namely, supplied to the electrolysis system ⁇ . 1
  • Natural gas 36 ... 50 50,0,13 39, 819 35, 883 9, 968
  • FIG 4 an enlarged schematic Dar ⁇ position of the gas diffusion electrode GDE is still shown, as it is used in the figure 2 used: From a gas reservoir GR behind the porous cathode K, the carbon dioxide CO 2 pushes into the catholyte in the cathode space KR under elevated pressure. Arrows indicate the flow direction of the catholyte in the cathode space KR.
  • the carbon dioxide CO 2 is introduced into the gas diffusion electrode GDE via a carbon dioxide inlet CO 2 -E.
  • a laboratory monitor preferably works in a pressure range of 2 bar.
  • the carbon dioxide CO 2 is eg fed into the electrolyzer 1 after a pressure swing absorption. This can be operated for example as alkali electrolyzer.

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Abstract

L'invention concerne une installation de biogaz équipée d'un système électrolytique, par exemple un électrolyseur (1), comprenant une anode (A), une cathode (K), et une membrane (M) qui sépare les circuits d'anolyte et de catholyte (AK, KK). L'effluent de dioxyde de carbone (CO2) généré lors de la production de biogaz est recyclé afin qu'il ne soit pas diffusé dans l'atmosphère. Le dioxyde de carbone (CO2) est transformé au moyen de l'électrolyseur (1) et, par exemple, d'un réacteur (2) raccordé à l'électrolyseur, en substances hautement utiles pour la production de gaz combustible, qui sont ensuite ajoutées au biogaz et augmentent sensiblement la capacité calorifique de celui-ci.
PCT/EP2016/065778 2015-07-31 2016-07-05 Procédé de fabrication d'un gaz combustible et installation de production de gaz combustible comprenant un système électrolytique pour le traitement électrochimique du dioxyde de carbone WO2017021083A1 (fr)

Applications Claiming Priority (2)

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DE102015214592.1A DE102015214592A1 (de) 2015-07-31 2015-07-31 Herstellungsverfahren für ein Brenngas und Anlage zur Herstellung eines Brenngases mit einem Elektrolysesystem zur elektrochemischen Kohlenstoffdioxid-Verwertung
DE102015214592.1 2015-07-31

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112593252A (zh) * 2019-09-17 2021-04-02 株式会社东芝 电化学反应装置和有价物质制造系统
US11512403B2 (en) 2018-01-22 2022-11-29 Twelve Benefit Corporation System and method for carbon dioxide reactor control
US11859477B2 (en) 2019-07-02 2024-01-02 Totalenergies Se Hydrocarbon extraction using solar energy
US11939284B2 (en) 2022-08-12 2024-03-26 Twelve Benefit Corporation Acetic acid production

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4668349A (en) * 1986-10-24 1987-05-26 The Standard Oil Company Acid promoted electrocatalytic reduction of carbon dioxide by square planar transition metal complexes
DE10148600A1 (de) * 2001-10-02 2003-04-10 Bayer Ag Einbau einer Gasdiffusionselektrode in einen Elektrolyseur
WO2012110257A1 (fr) * 2011-02-17 2012-08-23 Alexander Krajete Système et procédé pour stocker de l'énergie sous forme de méthane
DE102012105658A1 (de) * 2012-06-28 2014-01-02 MicrobEnergy GmbH Energieversorgungseinheit
DE102013001689A1 (de) * 2013-01-31 2014-07-31 Waldemar E. Reule Verfahren zur Erzeugung von Biomethan
DE102013219681A1 (de) * 2013-09-30 2015-04-02 Marek Fulde Verfahren und System zur Speicherung von elektrischer Energie

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AU2010357037B2 (en) * 2010-07-09 2014-01-16 Haldor Topsoe A/S Process for converting biogas to a gas rich in methane
DE102013224202A1 (de) * 2013-11-27 2015-05-28 Siemens Aktiengesellschaft Elektrolysezelle und Verfahren zur Erzeugung chemischer Produkte mittels einer Elektrolysezelle

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4668349A (en) * 1986-10-24 1987-05-26 The Standard Oil Company Acid promoted electrocatalytic reduction of carbon dioxide by square planar transition metal complexes
DE10148600A1 (de) * 2001-10-02 2003-04-10 Bayer Ag Einbau einer Gasdiffusionselektrode in einen Elektrolyseur
WO2012110257A1 (fr) * 2011-02-17 2012-08-23 Alexander Krajete Système et procédé pour stocker de l'énergie sous forme de méthane
DE102012105658A1 (de) * 2012-06-28 2014-01-02 MicrobEnergy GmbH Energieversorgungseinheit
DE102013001689A1 (de) * 2013-01-31 2014-07-31 Waldemar E. Reule Verfahren zur Erzeugung von Biomethan
DE102013219681A1 (de) * 2013-09-30 2015-04-02 Marek Fulde Verfahren und System zur Speicherung von elektrischer Energie

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
"Modern Aspects of Electrochemistry", 2008, SPRINGER, pages: 89 - 189
JOHN A. KEITH ET AL: "Elucidation of the Selectivity of Proton-Dependent Electrocatalytic CO 2 Reduction by fac -Re(bpy)(CO) 3 Cl", JOURNAL OF THE AMERICAN CHEMICAL SOCIETY, vol. 135, no. 42, 23 October 2013 (2013-10-23), US, pages 15823 - 15829, XP055257154, ISSN: 0002-7863, DOI: 10.1021/ja406456g *

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11512403B2 (en) 2018-01-22 2022-11-29 Twelve Benefit Corporation System and method for carbon dioxide reactor control
US11859477B2 (en) 2019-07-02 2024-01-02 Totalenergies Se Hydrocarbon extraction using solar energy
CN112593252A (zh) * 2019-09-17 2021-04-02 株式会社东芝 电化学反应装置和有价物质制造系统
US11939284B2 (en) 2022-08-12 2024-03-26 Twelve Benefit Corporation Acetic acid production

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