EP3655564A1 - Agencement d'électrolyseur - Google Patents

Agencement d'électrolyseur

Info

Publication number
EP3655564A1
EP3655564A1 EP18780027.1A EP18780027A EP3655564A1 EP 3655564 A1 EP3655564 A1 EP 3655564A1 EP 18780027 A EP18780027 A EP 18780027A EP 3655564 A1 EP3655564 A1 EP 3655564A1
Authority
EP
European Patent Office
Prior art keywords
circuit
volume flow
anode
electrolyzer
cathode
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP18780027.1A
Other languages
German (de)
English (en)
Inventor
Marc Hanebuth
Günter Schmid
Katharina Meltzer
Dan Taroata
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Siemens AG
Original Assignee
Siemens AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Siemens AG filed Critical Siemens AG
Publication of EP3655564A1 publication Critical patent/EP3655564A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • 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
    • 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
    • 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
    • C25B9/17—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
    • C25B9/23—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms comprising ion-exchange membranes in or on which electrode material is embedded
    • 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
    • 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
    • C25B3/00—Electrolytic production of organic compounds
    • C25B3/20—Processes
    • C25B3/25—Reduction
    • 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 invention relates to an electrolyzer arrangement according to claim 1 and to a method for operating a
  • a technical challenge is to get out carbon dioxide, CO2, using over Schu Sener ⁇ gies that occur especially if more renewable energy sources are fed in the network, provide value-added products hither ⁇ .
  • One approach is the production of gaseous products of value such as carbon monoxide, CO or ethylene, C2H 4, by electrochemical reduction of carbon dioxide. This re ⁇ actions, for example, within the so-called CO2 - performed electrolyzers.
  • a typical design of C02 electrolyzers is based on aqueous electrolytes containing a conducting salt, that is, a salt that is dissolved in the electrolyte and is electrically effective.
  • the C02 electrolyzers are treated here by way of example for all electrolysis devices which have a liquid electrolyte.
  • anode space and cathode space are kept separate. This prevents that at the cathode ge ⁇ formed gaseous recyclable material can reach the anode side.
  • an image formed on the anode side gas typically oxygen reaches the Ka ⁇ Thode page. It is thus avoided a mutual Vermi ⁇ rule of the two gases. This is necessary to dangerous operating conditions, eg by the formation of explosive Gas mixtures, exclude.
  • there are other reasons to avoid mixing the gases For example, depending on the application, there are requirements for gas purities of the product gas. For example, CO, which is used in an anaerobic gas fermentation, may contain only traces of oxygen.
  • the membranes used are virtually impermeable to gases, they must be permeable to ionic charge carriers.
  • a supporting electrolyte such as potassium ⁇
  • the transport of the cations of the supporting electrolyte, such as potassium ⁇ is common to, in the foreground, that is, the potassium cation diffuses through the membrane from the anode side to the cathode side.
  • Hie ⁇ out in turn results in a difference in concentration of Ka functions between the electrolyte on the anode side and the cathode side.
  • both electrolytes can be mixed with one another in a common storage container, so that after passing through the electrolyte
  • Electrolysers the concentration equalization is ensured both on ions and the water. Since in a ⁇ individual electrolyte fluids, however, always Gasverunreinigun- gene are resulting from the electrolysis, and consist essentially of the product gas and hydrogen and oxygen concentration, this common compensation also involves certain risks. In addition, a frequently required Product purity made difficult by contamination of the product by hydrogen or by oxygen.
  • the object of the invention is to provide an electrolyzer arrangement or a method for operating an electrolyzer arrangement which are suitable for ensuring a necessary concentration compensation between an anolyte and a catholyte in the electrolyzer and thereby reducing gas contamination.
  • the object is achieved in an electrolyzer, with the features of claim 1, and in a method for operating the electrolyzer with the features of Pa ⁇ tent tapees 12th
  • the electrolyzer according to the invention according to claim 1 comprises at least one electrolysis cell, which in turn comprises two electrodes, namely an anode and a cathode. Je ⁇ de of the two electrodes is in communication with a so-called electrode space.
  • the electrode space is adapted to be filled with a liquid electrolyte.
  • the two electrode spaces are separated by a membrane, wherein both electrodes comprise a conveying device for conveying the electrolyte in each case in a circuit, a cathode circuit and an anode circuit.
  • the invention is characterized in that outside the electrolytic cell, a conveying device for conveying a secondary volume flow between the cathode circuit and the anode circuit is provided outside the electrolytic cell.
  • anode circuit and the cathode circuit is in each case understood to be a device, in particular a pipeline ⁇ device, understood in particular to a pumping device which is adapted to have formed therein an appropriate electrolyte is circulated or recirculated.
  • each case one collecting container is provided for each of the two circuits.
  • the collecting container is subdivided into at least two sub-containers, wherein a first sub-container communicates with the cathode circuit and a second sub-container communicates with the anode circuit and the secondary volume flow is between the first sub-container and the second sub-container.
  • a compensation of the electrolytes, so the anolyte and the catholyte outside of the electrolytic cell in two separate containers via a defined secondary flow, for example through a pipe with a targeted flow, which is controlled by a pump, is particularly useful because the electrolyte collected in this sub-tank is and the volume flow can be well regulated.
  • a second conveying device for generating a second secondary volume flow between the two circuits is provided. This takes place in the opposite direction to the first secondary flow.
  • This may be expedient if, for example, water and cations are passed from a first to a second sub-container through the first sub-volume flow, and an equalization of anions can take place in the second sub-volume flow.
  • the conveying device between the two circuits for generating the second secondary flow in the form of a membrane module ⁇ staltet.
  • the membrane module prefferably be both a constituent part of the cathode circulation and a component of the
  • Anodenniklaufes is.
  • a membrane also as between the two electrode chambers, arranged, which is available as a replacement area for the dissolved ions to Ver ⁇ addition. These are cations and anions.
  • the membrane between the electrode spaces is preferably a cation-permeable membrane.
  • This is in contrast to a porous membrane to den nourish gases from the individual electrical occurring there during the electrolysis to keep vonei ⁇ Nander separately.
  • cations such as potassium, which is part of the conducting salt, to migrate through the membrane.
  • an increased concentration balance between the catholyte and the anolyte outside the electrolysis cell is necessary.
  • Ver ⁇ application of a cation permeable membrane of the secondary flow is preferably carried out from the cathode to the anode circulation circuit ⁇ run.
  • Another aspect of the invention is a method having the features of claim 12 which is suitable for operating an electrolyzer assembly.
  • the electrolysis uranium order on an electrolytic cell comprising the re ⁇ rum two electrodes, namely an anode and a Thode Ka.
  • the electrodes each have an electrode space through which a liquid electrolyte with a conductive salt dissolved therein is conveyed into a respective circuit, namely a cathode circuit and an anode circuit. Since ⁇ at the electrode spaces and thus also contained therein electrolytes are separated by a membrane.
  • the invention is characterized in that the electrolyte is conveyed from one circuit to the second circuit in a secondary volume flow.
  • the method has the same advantages already be ⁇ wag the electrolysis arrangement are discussed.
  • the secondary volume flow is designed such that it has at least 0.01% at most 10%, preferably between 0.1% and 1% of the larger of the two main volume flows, ie either the volume flow of the cathode circuit or of the anode circuit.
  • secondary flow both in terms of the method and with respect to the electrolyzer arrangement, a stream of molecules and ions is understood.
  • the secondary volume flow can take place in corresponding pipelines, hoses or channels, in the form of a stream of the electrolyte, in particular an aqueous base with conductive salt or the corresponding ions contained therein.
  • it can also take the form of a diffusion through a membrane.
  • the term secondary volumetric flow device is understood to mean any device which is suitable for providing said stream of molecules and ions. This includes, on the one hand, in particular a corresponding pump, but also a corresponding line or channel, which on the basis of
  • delivery device also includes a membrane which causes ions to be transferred from one cycle to the other cycle.
  • a gas separation container to be provided in the cathode circuit and / or in the anode circuit, and a connection line of at least one of the gas discharge containers be provided. Separation container is provided to Eduktzu Crystalvoriques. This allows the anode gas and / or cathode gas as ⁇ derum process reasons a starting gas may represent the actual electrolysis process be recycled. This positively influences the cost-effectiveness of the process.
  • FIG. 1 electrolyzer arrangement with a secondary volume flow between anode circuit and cathode circuit
  • FIG. 2 electrolyzer arrangement as in FIG. 1 with additional separation vessels
  • FIG. 3 shows an electrolyzer arrangement with two possibilities for the representation of devices for a secondary volume flow with two collecting containers
  • FIG. 4 shows an electrolyzer arrangement with two possibilities for the representation of devices for a secondary volume flow
  • Figure 5 is a schematic representation of an electrolyzer, with two headers in the foreground and
  • FIG. 6 shows a membrane module
  • an electrolyzer assembly 2 is shown schematically having an electrolytic cell 4, in which an electrolyte 5 is arranged.
  • the electrolysis cell 4 has two electrodes, a cathode 7, which is designed in this case in the form of a gas-permeable electrode and an anode 6.
  • the two electrodes, namely the anode 6 and the cathode 7, each adjoin an electrode space, wherein under an electrode space 8 for the anode 6 and an electrode space 9 for the cathode 7 differs.
  • Both electrode chambers 8, 9 are separated from each other by a membrane 10.
  • the electrolyte 5 which is referred to depending on the location in the electrolytic cell 4 as anolyte 38 when it is present in the electrode chamber 8 of the anode 6 and which is referred to as the catholyte 40 when in the electrode chamber 9 of the cathode is present.
  • the electrolyte 5 or 38 and 40 is not stationary in the electric ⁇ denriz 8 and 9, but it is in a circuit 14, 15.
  • conveyors 12 and 13 are provided, each for an anode circuit 14 and a cathode circuit 15 provide the corresponding volume flow of electrolyte 5 or 38 and 40.
  • the electrolyte 5 is moved along the respective circuit 14 (anode circuit) and 15 (cathode circuit).
  • Betrach ⁇ is now exemplarily tet the cathode circuit 15, so the catholyte is pumped 40 from the electrode chamber 9, the cathode 7 on the drawing provided with the reference line 15 by the conveyor. 13
  • uranium assembly further exists a reactant supply 42, through which a reactant, for example Kohlendio ⁇ dioxide is introduced into the electrolytic cell 4, and a process duktab effet 44.
  • a reactant for example Kohlendio ⁇ dioxide
  • a process duktab effet 44 During the electrolysis, in which at the Ka ⁇ Thode 7 and at the anode 6 electric current is applied, in this example, the carbon dioxide to carbon monoxide redu ⁇ graces, which comes out via the product discharge 44 from the electrolysis ⁇ cell 4 again.
  • both protons and the cations of a conducting salt dissolved in the electrolyte 5, for example potassium migrate through the membrane 10, which in this embodiment is in the form of a cation-permeable membrane.
  • the anolyte 38 and the catholyte 40 have different concentrations of cations, in particular cations of the conductive salt, with increasing electrolysis activity. To a degree of about 2% difference, this can be tolerated, starting from a certain concentration difference the cost- effectiveness and profitability of the electrolysis ⁇ process no longer guaranteed. For this reason, it is expedient to carry out a continuous exchange between the anolyte 38 and the catholyte 40.
  • a single collection vessel is used in a simple form which is both part of the circuit 14, the anode circuit and the cathode circuit 15.
  • a secondary volume flow 20 takes place, which takes place via a secondary volume flow device 18. Due to the secondary volume flow, there is an exchange of concentration between the anode circuit and the cathode circuit or vice versa.
  • the direction in which the secondary flow rate depends depends on the respective process control.
  • the secondary flow rate is preferably at most 10% of the volume of electrolyte flows in Katho ⁇ thinking rice marker 15, or in the anode circuit 14, minimum low flow rate is 0.01% of the electrolyte volume flow, in particular, the interval in which the Crowvolu ⁇ volume flow 20 moving between 0.1% and 1% of Elektrolytvolu ⁇ volume flows.
  • the cathode circuit 15 has ei ⁇ NEN collection container 23 in which the catholyte 40 is trans- ferred and the anode circuit 14 comprises a collection container 22 into which the anolyte is brought 38th
  • Both Sam ⁇ mel matterser 23 and 22 are generally separated from each other, but also they have, in another Substituted ⁇ staltungsform a device 18 which is used to produce egg nes addition to volume flow twentieth
  • This device 18 is shown very schematically in Figure 3, it may for example be configured in the form of an overflow channel, in which a small amount, can move containers through a defined pitch or a defi ⁇ ned gradient from one container to the other collective term. It can also be caused by a corresponding, not shown here pipeline or a corresponding hose, a secondary volume flow 20 between the containers 22 and 23, which is effected for example by gravity or a pressure difference.
  • FIG 5 shows a device 18 for generating the sub-volume stream 20 is shown which he ⁇ follows in the form of pipes, in which a pump is integrated 30th It may also be expedient ge ⁇ Gurss Figure 5 to a Konzentrationsaus- equal between the anolyte 38 and to ensure the catholyte 40 in terms of the anions, that a second secondary flow 26 is provided by a second conveyor device 24, for example in the Pumping device 30 according to FIG 5 is generated. It is also expedient that the two sub-containers 22, 23 contain agitators 27, which ensure a uniform mixing of the electrolyte 38, 40 in the respective containers 22 and 23. It is of course also possible to achieve a good mixing within the sub-tank without active stirring devices, eg. B. by a suitable flow guidance.
  • the second secondary volume flow then serves to compensate for anions which take place between the container 22 and the container 23 via the second secondary volume flow 26.
  • a further possibility of a secondary flow to erzeu ⁇ gene is in the form of a membrane module 28, in which a diaphragm 29 is arranged (cf. FIG. 3 and 4). Both the cathode circuit 15 and the anode circuit 14 pass through this membrane module 28 according to FIG. 3.
  • the membrane module 28 has, in addition to the membrane 29, two module chambers, a first module chamber 46 through which the anode circuit 14 extends and a second module chamber 47 the Katho ⁇ den Vietnameselauf 15 takes place.
  • the catholyte 40 is thus located in the module chamber 47, and the anolyte 38 is located in the module chamber 46.
  • the membrane 29 provides an exchange face for the dissolved ions in the electrolytes 38 and 40, namely for cations and for anions.
  • the task is porous membranes that are as thin as possible, be ⁇ particularly well suited. These bring a relatively low transport resistance, so that relatively small Memb ⁇ ran lake are sufficient.
  • the transport in porous membranes (permeation) is caused by two different mechanisms, an externally forced transport through pores, ie a purely convective transport, or a transport due to diffusion of a dissolved component.
  • the transport mechanism of the ions through the porous membrane corresponds to the diffusion, which proceeds without energy consumption.
  • the so-called drag water can also be forced in principle by convection through the membrane by applying a small differential pressure.
  • the required size of the porous membrane 29 can be determined via the maximum expected mass flow rate of cations within the electrolysis cell by simultaneously defining a maximum tolerable concentration difference between anolyte 38 and catholyte 40 (for example 0.2 mol / L).
  • a maximum tolerable concentration difference between anolyte 38 and catholyte 40 for example 0.2 mol / L.
  • Electrolysis cell surface of the membrane 10 is is min ⁇ least one hundredth 10. Particularly advantageous from the membrane surface of the membrane has a ratio of 1:20 between the membrane 29 and membrane 10 to about 1: 5 between the membrane 29 and membrane 10 degrees.
  • water can also be transported through the porous membrane 29 in that a small differential pressure prevails within the membrane module 28. This is preferably less than 100 mbar.
  • the catholyte 40 does not contain any oxygen which contaminates the catholyte product gas.
  • starting gas such as carbon dioxide through the anolyte 38 (at ⁇ play as carbon monoxide, methane or hydrogen) neither product gas.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)

Abstract

La présente invention concerne un agencement d'électrolyseur muni d'au moins une cellule d'électrolyse qui comprend deux électrodes, à savoir une anode et une cathode, chacune des deux électrodes étant en contact avec une chambre d'électrode devant être remplie avec un électrolyte liquide, les deux chambres d'électrodes étant séparées par une membrane et pour les deux électrodes, il est prévu respectivement un dispositif de transport pour transporter l'électrolyte dans respectivement un circuit, un circuit de cathode et un circuit d'anode, à travers la chambre d'électrode à l'aide d'au moins un récipient de recueil par circuit, de nouveau dans la chambre d'électrode. L'invention est caractérisée en ce qu'il est prévu, en dehors de la cellule d'électrolyse, un dispositif pour transporter un courant de volume secondaire entre le circuit de cathode et le circuit d'anode.
EP18780027.1A 2017-09-21 2018-09-13 Agencement d'électrolyseur Withdrawn EP3655564A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102017216710.6A DE102017216710A1 (de) 2017-09-21 2017-09-21 Elektrolyseuranordnung
PCT/EP2018/074697 WO2019057593A1 (fr) 2017-09-21 2018-09-13 Agencement d'électrolyseur

Publications (1)

Publication Number Publication Date
EP3655564A1 true EP3655564A1 (fr) 2020-05-27

Family

ID=63720633

Family Applications (1)

Application Number Title Priority Date Filing Date
EP18780027.1A Withdrawn EP3655564A1 (fr) 2017-09-21 2018-09-13 Agencement d'électrolyseur

Country Status (6)

Country Link
US (1) US20200263311A1 (fr)
EP (1) EP3655564A1 (fr)
CN (1) CN111133131A (fr)
AU (1) AU2018335098A1 (fr)
DE (1) DE102017216710A1 (fr)
WO (1) WO2019057593A1 (fr)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3722462A1 (fr) * 2019-04-08 2020-10-14 Siemens Aktiengesellschaft Installation et procédé d'accumulation d'énergie électrique
DE102019123858A1 (de) * 2019-09-05 2021-03-11 Thyssenkrupp Uhde Chlorine Engineers Gmbh Kreuzflusswasserelektrolyse
CN112981438A (zh) * 2021-02-02 2021-06-18 碳能科技（北京）有限公司 Co2电解制合成气系统
CN117883974B (zh) * 2024-03-15 2024-06-18 中南大学 模块化膜隔离碳解吸装置、碳捕集系统、方法及应用

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19736350C1 (de) * 1997-08-21 1999-08-05 Atotech Deutschland Gmbh Verfahren zur Konzentrationsregulierung von Stoffen in Elektrolyten und Vorrichtung zur Durchführung des Verfahrens
MX2011001153A (es) * 2008-07-29 2011-09-15 Trustwater Ltd Dispositivo electroquimico.
DE102015003911A1 (de) * 2015-03-27 2016-09-29 Eilenburger Elektrolyse- Und Umwelttechnik Gmbh Verfahren zur Desinfektion von Schwimmbecken-, Trink- und Gebrauchswasser sowie zur Herstellung eines Desinfektionsmittelkonzentrats
DE102015212503A1 (de) * 2015-07-03 2017-01-05 Siemens Aktiengesellschaft Reduktionsverfahren und Elektrolysesystem zur elektrochemischen Kohlenstoffdioxid-Verwertung
DE102016200858A1 (de) * 2016-01-21 2017-07-27 Siemens Aktiengesellschaft Elektrolysesystem und Verfahren zur elektrochemischen Ethylenoxiderzeugung
DE102016202840A1 (de) * 2016-02-24 2017-08-24 Siemens Aktiengesellschaft Verfahren und Vorrichtung zur elektrochemischen Nutzung von Kohlenstoffdioxid

Also Published As

Publication number Publication date
AU2018335098A1 (en) 2020-03-12
US20200263311A1 (en) 2020-08-20
WO2019057593A1 (fr) 2019-03-28
DE102017216710A1 (de) 2019-03-21
CN111133131A (zh) 2020-05-08

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