US20190062931A1 - Method and Device for the Electrochemical Utilization of Carbon Dioxide - Google Patents

Method and Device for the Electrochemical Utilization of Carbon Dioxide Download PDF

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Publication number
US20190062931A1
US20190062931A1 US16/078,863 US201716078863A US2019062931A1 US 20190062931 A1 US20190062931 A1 US 20190062931A1 US 201716078863 A US201716078863 A US 201716078863A US 2019062931 A1 US2019062931 A1 US 2019062931A1
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Prior art keywords
separation apparatus
water
gas
catholyte
carbon dioxide
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Katharina Stark
Manfred Baldauf
Marc Hanebuth
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Siemens AG
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Siemens AG
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Assigned to SIEMENS AKTIENGESELLSCHAFT reassignment SIEMENS AKTIENGESELLSCHAFT ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: BALDAUF, MANFRED, HANEBUTH, MARC, Stark, Katharina
Publication of US20190062931A1 publication Critical patent/US20190062931A1/en
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    • 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
    • C25B1/10—
    • 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
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C25B9/08—
    • 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
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
    • C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms
    • 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
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/70—Assemblies comprising two or more cells
    • C25B9/73—Assemblies comprising two or more cells of the filter-press type
    • 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

  • Various embodiments may include a method and/or an apparatus for electrochemical utilization of carbon dioxide, wherein carbon dioxide is introduced into an electrolysis cell and reduced at a cathode.
  • One of the solutions currently contemplated is conversion of electrical energy to products of value which can serve as platform chemicals or synthesis gas which comprises carbon monoxide and hydrogen.
  • One possible technique for conversion of electrical energy to products of value is electrolysis.
  • the electrolysis of water to hydrogen and oxygen is a method known in the prior art.
  • But the electrolysis of carbon dioxide to carbon monoxide has also been a subject of research for a number of years, and there are efforts to develop an electrochemical system that can reduce an amount of carbon dioxide in accordance with economic interests.
  • Some electrolysis units include a low-temperature electrolyzer in which carbon dioxide as reactant gas is metered into a cathode space with the aid of a gas diffusion electrode.
  • the carbon dioxide is reduced to carbon monoxide at a cathode of the electrochemical cell, and water is oxidized to oxygen at an anode.
  • use of an aqueous electrolyte can result not only in the formation of carbon monoxide but also in the formation of hydrogen, since the water in the aqueous electrolyte is likewise electrolyzed.
  • the cathode space and the anode space may be separated by a membrane in order to guide the product gases formed, the carbon monoxide and hydrogen on the cathode side and oxygen on the anode side, out of the electrolysis cell separately from one another in order to prevent them from contaminating one another.
  • the transport of cations, especially of hydrogen ions, through the membrane is accompanied by simultaneous transport of water molecules.
  • the aqueous electrolyte therefore loses water on the anode side, while the aqueous electrolyte on the cathode side becomes ever further diluted by water, and so the conductivity here disadvantageously falls considerably.
  • teachings of the present disclosure provide a method and an apparatus enabling sustained continuous operation of the carbon dioxide electrolyzer with sufficiently high conductivity of the electrolyte, especially of the catholyte.
  • some embodiments of the teachings herein include a method of electrochemical utilization of carbon dioxide (CO 2 ), comprising the following steps: providing an electrolysis cell ( 2 ), wherein the electrolysis cell ( 2 ) comprises a membrane ( 3 ) which separates an anode space ( 16 ) from a cathode space ( 15 ), guiding a first aqueous electrolyte as catholyte (K) into the cathode space ( 15 ) and guiding a second aqueous electrolyte as anolyte (A) into the anode space ( 16 ), reducing the carbon dioxide (CO 2 ) to a product gas (PG) comprising carbon monoxide (CO), separating the product gas (PG) from the catholyte (K) in a first separation apparatus ( 6 ), separating
  • the stripping gas used is a reactant gas (EG) comprising carbon dioxide (CO 2 ) and/or the product gas (PG) from the electrolysis cell ( 2 ).
  • EG reactant gas
  • CO 2 carbon dioxide
  • PG product gas
  • the volume flow rate of the stripping gas is increased with the aid of at least one fan unit ( 9 ).
  • the stripping gas is at least partly recycled into the electrolysis cell ( 2 ) as reactant gas (EG) after the water (W) has been separated off.
  • the stripping gas is heated up prior to entry into the second separation apparatus ( 7 ).
  • the catholyte (K) separated from excess water is recycled from the third separation apparatus ( 8 ) into the cathode space ( 15 ).
  • a fraction not exceeding one eighth of the excess water (W) is already separated from the product gas (PG) by means of a condenser downstream of the first separation apparatus ( 6 ).
  • an electrolysis apparatus ( 1 ) for reducing carbon dioxide (CO 2 ) to carbon monoxide (CO), comprising: an electrolysis cell ( 2 ), wherein the electrolysis cell ( 2 ) comprises a membrane ( 3 ) which separates an ( 16 ) from a cathode space ( 15 ), a first conduit ( 20 ) for guiding a first electrolyte as catholyte (K) into the cathode space ( 15 ), a second conduit ( 21 ) for guiding a second electrolyte as anolyte (A) into the anode space ( 16 ), a first separation apparatus ( 6 ) for separating a product gas (PG) comprising carbon monoxide (CO) from the catholyte (K), a second separation apparatus ( 7 ) for separating off the excess water in the catholyte (K) by means of a stripping gas, a third separation apparatus ( 8 ) for separating the water (W) from the stripping gas, and
  • the second separation apparatus ( 7 ) comprises a pervaporation unit, a falling-film evaporator or a bubble column.
  • the membrane ( 3 ) comprises an anode (A).
  • the first separation apparatus ( 6 ) is integrated into the second separation apparatus ( 7 ).
  • FIG. 1 a schematic arrangement of the electrolysis apparatus, wherein the stripping gas used is the reactant gas, according to teachings of the present disclosure
  • FIG. 2 a schematic arrangement of the electrolysis apparatus, wherein the stripping gas used is the product gas, according to teachings of the present disclosure
  • FIG. 3 a schematic arrangement of the electrolysis apparatus, wherein the stripping gas used is both the reactant gas and the product gas, according to teachings of the present disclosure.
  • Various embodiments include and/or enable electrochemical utilization of carbon dioxide.
  • Some embodiments include a method, in which, first of all, an electrolysis cell is provided, wherein the electrolysis cell comprises a membrane which separates an anode space from a cathode space. Then a first aqueous electrolyte as catholyte is guided into the cathode space, and a second aqueous electrolyte as anolyte into the anode space. The carbon dioxide is then reduced to a product gas comprising carbon monoxide in the cathode space. The product gas and the catholyte are then guided into a first separation apparatus. In the first separation apparatus, the product gas is separated from the catholyte.
  • the catholyte is then guided into a second separation apparatus.
  • the catholyte enriched with water from the anolyte during the reduction of carbon dioxide is separated from this excess water by means of a stripping gas in this second separation apparatus.
  • the water is subsequently separated from the stripping gas. This water is subsequently recycled from the third separation apparatus into the anode space.
  • an electrolysis apparatus for reducing carbon dioxide to carbon monoxide comprises an electrolysis cell, wherein the electrolysis cell comprises a membrane which separates an anode space from a cathode space. It further comprises a first conduit into the cathode space for guiding a first electrolyte as catholyte into the cathode space. It further comprises a second conduit into the anode space for guiding a second electrolyte as anolyte into the anode space.
  • the electrolysis apparatus further comprises a first separation apparatus for separating a product gas comprising carbon monoxide from the catholyte.
  • the electrolysis apparatus further comprises a third conduit from the third separation apparatus to the anode space of the electrolysis cell for recycling the water into the anode space.
  • the first separation apparatus comprises a precipitation vessel.
  • gaseous components are separated from liquid components.
  • the third separation apparatus may comprise a condenser in which the water is condensed out of the stripping gas.
  • at least two membranes in the form of membrane stacks are used in the electrolysis cell.
  • the water-diluted catholyte is separated from the excess water with the aid of a stripping gas.
  • the catholyte is thus concentrated again, which increases its conductivity. Continuous operation of the carbon dioxide electrolyzer is possible in this way. Furthermore, the operation of the carbon dioxide electrolyzer is more economically viable compared to noncontinuous operation. Dilution effects resulting from the water may be avoided, and so the conductivity of the catholyte remains at a sufficiently high level to assure continuous operation. Separation solely of water in the first separation apparatus in which the product gas is separated from the catholyte is insufficient. At an estimate, only a maximum of one eighth of the necessary amount of water is discharged from the process here. Thus, a predominant portion of the water that has gone through the membrane still remains in the catholyte.
  • a second separation apparatus enables the separating of a sufficiently large proportion of water from the catholyte to keep the conductivity of the catholyte at a sufficiently high level.
  • the third separation apparatus may provide the recovery of the water from the stripping gas in order to recycle it into the electrolysis process and especially to use it again in the anolyte space.
  • the stripping gas is also dried and can be reused in the process.
  • the stripping gas used is a reactant gas comprising carbon dioxide and/or the product gas from the electrolysis cell that likewise comprises as yet unconverted carbon dioxide. It is advantageous here to avoid the use of a further stripping gas. Carbon dioxide is thus present both in the reactant gas and in the product gas and can be used as stripping gas for the water.
  • the reactant gas or product gas as stripping gas can be recycled into the electrolysis cell after the stripping, such that any product gas components that have escaped into the gas phase are recycled back into the electrolyzer and thus may not be lost.
  • the reactant gas or product gas is used as stripping gas, no additional cooling of the catholyte downstream of the electrolysis cell or, alternatively, only a cooling apparatus with low output is needed for cooling of the catholyte from the electrolysis cell.
  • the water-saturated stripping gas leaves the second apparatus and is separated in the third apparatus, especially a gas/liquid separator, to give condensate and a gas phase. The heat from the catholyte may thus be discharged via the stripping gas and this condenser.
  • the volume flow rate of the stripping gas is increased with the aid of at least one fan unit.
  • a fan unit may increase the volume flow rate, and so the volume flow rate of the reactant gas and/or the product gas is increased such that this volume flow alone as stripping gas separates the water from the catholyte in a sufficient amount.
  • the fan unit is typically disposed in a conduit that guides the stripping gas. The fan is may be arranged such that a portion of the carbon dioxide in the reactant gas or product gas is removed and circulated. The fan unit is thus within this mass transfer cycle.
  • the stripping gas is at least partly recycled into the electrolysis cell as reactant gas after the water has been separated off.
  • components that have also been transferred into the gas phase during the stripping but are products of value are recycled into the electrolysis cell.
  • Both the components of the product gas and those of the reactant gas can be recycled into the electrolysis cell as reactant gas.
  • Such a measure can increase the selectivity of carbon dioxide electrolyzers with regard to carbon monoxide and suppress the side reaction for formation of hydrogen. In some embodiments, this also avoids the loss of, for example, carbon monoxide or carbon dioxide which is used as reactant.
  • the stripping gas is heated up prior to entry into the second separation apparatus. This is helpful especially when the temperature of the catholyte downstream of the electrolysis cell is insufficiently high to preheat the stripping gas such that the water is transferred from the catholyte to the stripping gas.
  • the catholyte separated from excess water is recycled from the third separation apparatus into the cathode space. In some embodiments, the catholyte is thus reused, and so the continuous supply of new additional catholyte into the electrolysis cell is avoided.
  • a fraction not exceeding one eighth of the excess water is already separated by means of a condenser from the product gas which is guided out of the first separation apparatus.
  • This water can be recycled into the anode space.
  • the gas phase also comprises water as well as the product gas. It is thus possible to reduce the amount of stripping gas required in the second separation apparatus. It is possible either for an additional condenser to be disposed in the product gas conduit downstream of the first separation apparatus or for the product gas comprising the water to be guided into a condenser downstream of the second separation apparatus. In this case, the two streams, the product gas stream and the water-laden stripping gas, are guided separately and in parallel through the condenser, such that there is no mass transfer.
  • the second separation apparatus is a pervaporation unit, a falling-film evaporator or a bubble column.
  • a bubble column may be suitable when solely the product gas is used as stripping gas.
  • the first separation apparatus and the second separation apparatus have been combined.
  • the product gas is separated out and a portion of the water is stripped out of the catholyte at the same time. This construction dispenses with components in the apparatus, which contributes to the simplicity of the apparatus and saves energy.
  • the pervaporation unit is advantageous when both product gas and reactant gas are used for stripping of the water out of the catholyte.
  • the pervaporation unit provides a large area for contact between the stripping gas and the catholyte can be provided in a relatively small design volume.
  • the electrolysis there is transport of cations, especially protons, and simultaneous transport of water through the membrane 3 .
  • Three to ten molecules of water are transferred from the anode space 16 into the cathode space 15 for every cation.
  • the anolyte A loses water W
  • the catholyte K is diluted over time.
  • the conductivity of the catholyte K is distinctly reduced by the dilution with water W, which increases ohmic potential drops.
  • the water has to be separated from the catholyte K.
  • the three working examples show how the water W can be effectively separated.
  • FIG. 1 shows, in schematic form, an electrolysis apparatus having an electrolysis cell 2 .
  • the electrolysis apparatus comprises a membrane 3 , wherein the membrane 3 separates a cathode space 15 from an anode space 16 . It further comprises an anode 4 and a cathode 5 . In this configuration, the anode 4 has been applied to the membrane 3 . This reduces the necessary amount of anolyte A in the anode space 16 .
  • the cathode 5 may comprise a gas diffusion electrode.
  • the electrolysis apparatus 1 comprises a first separation apparatus 6 .
  • the fourth conduit 23 leads from the cathode space 15 into the first separation apparatus 6 .
  • the catholyte K, the product gas PG and water W are guided within the fourth conduit 23 .
  • the first separation apparatus 6 may comprise a precipitation apparatus.
  • the gaseous product gas PG is separated here from the catholyte K and water W.
  • the tenth conduit 29 then guides the product gas PG out of the electrolysis apparatus 1 .
  • the seventh conduit 26 guides the catholyte K separated off in the first separation apparatus 6 and the water KW into the second separation apparatus 7 .
  • the second separation apparatus 7 is configured as a falling-film evaporator.
  • the sixth conduit 25 branching off from the fifth conduit 24 , guides the reactant gas EG into the second separation apparatus 7 .
  • the reactant gas EG functions here as stripping gas.
  • the reactant gas EG is laden with water W in the second separation apparatus and then leaves the second separation apparatus 7 via the eighth conduit 27 .
  • Moist components are first condensed out of the reactant gas EG in a heat exchanger 11 .
  • third separation apparatus 8 especially a gas-liquid separator, water W is now separated from the reactant gas EG.
  • the water W is recycled via the third conduit 22 to the anode space 16 .
  • the reactant gas EG is guided in the ninth conduit 28 from the third separation apparatus 8 to the fifth reactant gas-guiding conduit 24 .
  • a fan unit 9 is present in the ninth conduit 28 .
  • this fan unit 9 increases the volume flow rate of the reactant gas EG, such that the reactant gas EG separates a sufficient amount of water W from the catholyte K.
  • the anode gas AG is also separated from the anolyte A in a fourth separation apparatus 10 .
  • the carbon dioxide CO 2 which is the main component of the reactant gas EG is reduced to carbon monoxide CO.
  • the product gas PG may comprise carbon monoxide CO and unreduced carbon dioxide CO 2 .
  • Oxygen O 2 is produced as anode gas AG at the anode A.
  • Catholytes used may include aqueous solutions of potassium sulfate, potassium hydrogencarbonate, and/or potassium phosphate. It is also possible to use further sulfates, hydrogencarbonates and phosphates. Mixtures of these substances are also possible. In general, conductivity of the aqueous catholyte must be at a maximum without precipitation of salts.
  • these aqueous solutions are present with salt concentrations of 0.5 mol/L to 1 mol/L.
  • salt concentrations 0.5 mol/L to 1 mol/L.
  • water is used as anolyte.
  • FIG. 2 shows one embodiment with an electrolysis apparatus 1 in which the product gas PG is used for stripping of the water W out of the catholyte K.
  • the electrolysis apparatus 1 comprises an electrolysis apparatus 2 comprising a membrane 3 , an anode 4 , a cathode 5 , and an anode space 16 separated from the cathode space 15 by the membrane 3 .
  • the reactant gas EG is guided into the electrolysis cell 2 via a fifth conduit 24 .
  • the reactant gas EG comprises carbon dioxide CO 2 which is reduced to carbon monoxide CO in the cathode space 15 .
  • the catholyte K that has been enriched with water W leaves the electrolysis cell 2 for the second separation apparatus 7 together with the product gas PG comprising carbon dioxide CO and unreduced carbon dioxide CO 2 via the fourth conduit 23 .
  • the first separation apparatus 6 and the second separation apparatus 7 are combined in one apparatus.
  • the second separation apparatus 7 comprises a bubble column.
  • the product gas PG comprising carbon monoxide CO and carbon dioxide CO 2 is guided here by means of the fourteenth conduit 33 into the second separation apparatus 7 .
  • the product gas PG is enriched with water W therein and leaves the second separation apparatus 7 via the eighth conduit 27 .
  • the product gas PG and the water W are then guided through a first heat exchanger 11 , where a fraction of water W is already condensed.
  • the two phases are then separated from one another in the third separation apparatus 8 .
  • the water W is recycled via the third conduit 22 into the anode space 16 .
  • the product gas PG is partly conducted out of the system via the tenth conduit 29 .
  • a second fraction is recycled to the second separation apparatus 7 via the fourteenth conduit 33 .
  • a fan unit 9 is introduced into the fourteenth conduit 33 .
  • the stripping gas is present in a sufficient amount to separate the excess water W from the catholyte K.
  • the catholyte K can then be recycled into the cathode space 15 via the first conduit 20 .
  • the pump 13 ensures the transport of the catholyte K.
  • the oxygen gas formed at the anode, anode gas AG is guided via the eleventh conduit 30 into the fourth separation apparatus 10 .
  • the anode gas AG oxygen is separated from the anolyte A.
  • the anolyte A is recycled into the anode space 16 via a twelfth conduit 31 .
  • the anode gas AG oxygen leaves the electrolysis apparatus 1 via a thirteenth conduit 32 .
  • FIG. 3 shows an electrolysis apparatus 1 in which the stripping gas used is both the product gas PG and the reactant gas EG.
  • the second separation apparatus 7 in that case is a pervaporation unit.
  • the electrolysis cell 2 comprises, as already set out in the first two examples, a membrane 3 , an anode 4 , a cathode 5 , an anode space 16 and a cathode space 15 .
  • the catholyte K that has been enriched with water W during the electrolysis of carbon dioxide CO 2 to carbon monoxide CO is guided via the fourth conduit 23 into the first separation apparatus 6 .
  • the product gas is discharged therein via the tenth conduit 29 .
  • the catholyte K and the water W leave the first separation apparatus 6 via the seventh conduit 26 and reach the second separation apparatus 7 .
  • the reactant gas EG and a portion of the product gas PG which has been recycled via the fourteenth conduit 33 are guided into the pervaporation unit into the second separation apparatus 7 , the pervaporation unit.
  • the water W is now transferred from the catholyte K through the membrane into the reactant gas and product gas EG, PG.
  • the reactant gas and product gas EG, PG and the water W are now guided through the fifteenth conduit 34 at first via a first heat exchanger 11 and then, in the third separation apparatus 8 , liquid components are separated from gas components.
  • the water W is recycled via the third conduit 22 into the anode space 16 .
  • the reactant gas and the product gas EG, PG are recycled via the sixteenth conduit 35 into the cathode space 15 .
  • the anolyte is cooled to such an extent that it is recycled into the anode space 16 at a temperature of 20° C. to 95° C. More preferably, it is recycled into the anode space 16 at a temperature of 70° C.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
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  • Inorganic Chemistry (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
US16/078,863 2016-02-24 2017-02-20 Method and Device for the Electrochemical Utilization of Carbon Dioxide Abandoned US20190062931A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102016202840.5A DE102016202840A1 (de) 2016-02-24 2016-02-24 Verfahren und Vorrichtung zur elektrochemischen Nutzung von Kohlenstoffdioxid
DE102016202840.5 2016-02-24
PCT/EP2017/053742 WO2017144395A1 (de) 2016-02-24 2017-02-20 Verfahren und vorrichtung zur elektrochemischen nutzung von kohlenstoffdioxid

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EP (1) EP3384069B1 (pl)
CN (1) CN108699709A (pl)
AU (1) AU2017224279B2 (pl)
DE (1) DE102016202840A1 (pl)
DK (1) DK3384069T3 (pl)
ES (1) ES2751906T3 (pl)
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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11417901B2 (en) 2018-12-18 2022-08-16 Twelve Benefit Corporation Electrolyzer and method of use
US11512403B2 (en) 2018-01-22 2022-11-29 Twelve Benefit Corporation System and method for carbon dioxide reactor control
US11578415B2 (en) * 2018-11-28 2023-02-14 Twelve Benefit Corporation Electrolyzer and method of use
US11939284B2 (en) 2022-08-12 2024-03-26 Twelve Benefit Corporation Acetic acid production

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102017216710A1 (de) * 2017-09-21 2019-03-21 Siemens Aktiengesellschaft Elektrolyseuranordnung
DE102019211620A1 (de) * 2019-08-02 2021-02-04 Siemens Aktiengesellschaft Anlage und Verfahren zur elektrochemischen Nutzung von Kohlenstoffdioxid
CN110344071B (zh) * 2019-08-14 2020-11-17 碳能科技（北京）有限公司 电还原co2装置和方法
DE102019123858A1 (de) 2019-09-05 2021-03-11 Thyssenkrupp Uhde Chlorine Engineers Gmbh Kreuzflusswasserelektrolyse
DE102020005254A1 (de) * 2020-08-27 2022-03-03 Linde Gmbh Verfahren und Anlage zur Herstellung von Kohlenstoffmonoxid
CN112725823B (zh) * 2020-12-07 2021-11-19 大连理工大学 一种高效利用电能进行煤氧化和二氧化碳还原的耦合工艺

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2289898A (en) * 1994-06-04 1995-12-06 Atomic Energy Authority Uk Reducing contamination of the anolyte in electrochemical oxidation of matter using nitric acid containing silver ions as the electrolyte
US20140131217A1 (en) * 2011-05-31 2014-05-15 Clean Chemistry, Llc Electrochemical reactor and process

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002302784A (ja) * 2001-01-30 2002-10-18 Fuji Electric Co Ltd 固体高分子電解質膜を用いた水電解装置とその運転方法
US8845878B2 (en) * 2010-07-29 2014-09-30 Liquid Light, Inc. Reducing carbon dioxide to products
JP5437968B2 (ja) * 2010-10-14 2014-03-12 本田技研工業株式会社 水電解システム
US8821709B2 (en) * 2012-07-26 2014-09-02 Liquid Light, Inc. System and method for oxidizing organic compounds while reducing carbon dioxide
JP2015168836A (ja) * 2014-03-05 2015-09-28 株式会社神鋼環境ソリューション 水素酸素発生装置

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2289898A (en) * 1994-06-04 1995-12-06 Atomic Energy Authority Uk Reducing contamination of the anolyte in electrochemical oxidation of matter using nitric acid containing silver ions as the electrolyte
US20140131217A1 (en) * 2011-05-31 2014-05-15 Clean Chemistry, Llc Electrochemical reactor and process

Cited By (5)

* 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
US11578415B2 (en) * 2018-11-28 2023-02-14 Twelve Benefit Corporation Electrolyzer and method of use
US11417901B2 (en) 2018-12-18 2022-08-16 Twelve Benefit Corporation Electrolyzer and method of use
US11888191B2 (en) 2018-12-18 2024-01-30 Twelve Benefit Corporation Electrolyzer and method of use
US11939284B2 (en) 2022-08-12 2024-03-26 Twelve Benefit Corporation Acetic acid production

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DE102016202840A1 (de) 2017-08-24
ES2751906T3 (es) 2020-04-02
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AU2017224279A1 (en) 2018-08-02

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