WO2016153341A1 - Assemblage électrodes-membrane bipolaire pour la production de combustible - Google Patents

Assemblage électrodes-membrane bipolaire pour la production de combustible Download PDF

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Publication number
WO2016153341A1
WO2016153341A1 PCT/NL2016/050189 NL2016050189W WO2016153341A1 WO 2016153341 A1 WO2016153341 A1 WO 2016153341A1 NL 2016050189 W NL2016050189 W NL 2016050189W WO 2016153341 A1 WO2016153341 A1 WO 2016153341A1
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Prior art keywords
electrode
fluid
compartment
cathode
double layer
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WO2016153341A4 (fr
WO2016153341A9 (fr
Inventor
Wilson Abele SMITH
David Arie VERMAAS
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Technische Universiteit Delft
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Technische Universiteit Delft
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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
    • 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
    • C25B1/23—Carbon monoxide or syngas
    • 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
    • C25B9/77—Assemblies comprising two or more cells of the filter-press type having diaphragms
    • 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 is in the field of forming a chemical fuel, such as by electrolysis of water thereby form- ing hydrogen.
  • the present invention is in the field of forming a chemical fuel, such as by electrolysis of water thereby forming hydrogen.
  • a chemical fuel such as by electrolysis of water thereby forming hydrogen.
  • Alternative approaches relate to forming hydro- gen also a hydrocarbon, syngas, and an alcohol may be formed. Based on readily available fluids these chemical fuels can be produced.
  • a source for e.g. the electrolysis may be solar ra ⁇ diation.
  • Electrolysis of a species as water relates to decom- position of the species (water) into its constituents (oxygen and hydrogen) by providing an electric current through said species. Thereto the species is typically in fluid form. In case of water an objective is to produce hydrogen. Electrolysis can be used to skim off excess power, such as from wind energy.
  • EP 0 459 820 A2 recites a bipolar membrane comprising a cation-exchange membrane closely adhered to an anion exchange membrane in which cation-exchange groups present at least at the adhered surface of the cation exchange membrane have been ion-exchanged with a heavy metal ion, has a water splitting current efficiency of not less then 80% and a water splitting membrane potential of not more than 2.0 V.
  • US 2007/023290 A recites an electrochemical cell comprising an ion exchange membrane having anion and cation exchange materials.
  • the membrane can have separate anion and cation exchange layers that define a heterogeneous water- splitting interface there between.
  • the mem- brane has a textured surface having a pattern of texture fea ⁇ tures comprising spaced apart peaks and valleys.
  • the mem ⁇ branes can also have an integral spacer.
  • a cartridge can be fabricated with a plurality of the membranes for insertion in a housing of the electrochemical cell.
  • the housing can also have a detachable lid that fits on the cartridge.
  • the electrochemical cell can be part of an ion controlling apparatus.
  • CN 102 912 374 A2 recites an electrochemical reduc ⁇ tion CO 2 electrolytic tank using a bipolar membrane as a diaphragm and an application of the electrochemical reduction C0 2 electrolytic tank.
  • the electrolytic tank comprises a cathode electrolysis compartment, catholyte, an anode elec- trolysis compartment, anolyte and the bipolar membrane for dividing the cathode electrolysis compartment and the anode electrolysis compartment.
  • the electrode materials of the cathode electrolysis compartment include Pb, In and Cu etc., and the catholyteis an alkaline aqueous solution; and the electrode materials of the anode electrolysis compartment include Pt and Pd etc., and the anolyte is an acidic aqueous solution containing iodate.
  • the hydroxy radicals in the cathode electrolysis compartment and the protons in the anodic electrolysis compartment are diffused to the bipolar membrane to generate water so as to form a voltage drop, so that the working voltage in the electrolytic tank is reduced.
  • the iodide ions are oxidized to generate an iodine elementary substance with low potential, small over-potential and quick dynamic process, so that the working voltage in the electrolytic tank is further reduced.
  • CO 2 is electrically reduced in a cathode compartment so as to generate small molecular fuels, such as formate, methanol, and methane; and the iodide ions are electrically oxidized to generate the elementary substance iodine in an anode compartment .
  • the present invention therefore relates to an improved process and system for generating chemical fuels, which solve one or more of the above problems and drawbacks of the prior art, providing reliable results, without jeopardizing functionality and advantages.
  • the present invention relates to a system for pro- ducing a chemical fuel according to claim 1, and a method of making said chemical fuel according to claim 13.
  • a physical double layer structure also referred to as "double layer”
  • double layer such as a bipolar membrane.
  • the double layer structure com- prises two layers directly attached to one and another.
  • Advantages of using a double layer structure with an attached electrode are; that the double layer structure provides a physical support layer for an embedded electrode, and minimizes the thickness of the electrode; the double layer struc- ture and embedded electrode have a negligible distance between the structure (or put different, are physically attached or connected to one and another; see e.g. fig.
  • the double layer structure acts as a barrier for the produced species (oxygen) at one side and the produced products (e.g., hydrogen, syngas) at another side of the structure.
  • the produced species oxygen
  • the produced products e.g., hydrogen, syngas
  • the electrodes can be positioned close together without mutual mixing of the produced gasses, which is found to further decrease ohmic losses; the double layer structure enables to use different electrolytes at either side, or to even use a gaseous phase at one side.
  • the supply of species e.g.
  • CO2 and H 2 can be tuned in all ratios, which directly influences the product selectivity;
  • the double layer structure creates an extreme pH-difference, which allows the cathode to operate in acidic conditions and the anode to operate in alkaline condi- tions;
  • the double layer in an example chemically/physically separates a base being present at one side thereof from an acid being present at another side thereof. This is found fa ⁇ vourable for common earth abundant catalysts, such as Ni- based oxygen evolution catalysts, while CO and H 2 production are promoted at low pH;
  • the anion-cation layered structure creates a strong barrier for any other ions than H + or OH " . This feature is found to minimize contamination of the cath ⁇ ode with dissolved species of the anodic compartment and therefore increases the stability of the system.
  • the present double layer structure in an example the present bipolar membrane, is typically not electrically conducting, or in an alternative having a high ohmic resistance (i.e. being an electrical insulator).
  • an area of a first element e.g. an electrode is at a negligible distance of an area of a second element e.g. a double membrane, stays at such a distance if a small force is applied to detach the elements, such as a force of two times gravity; i.e. if a first element is fixed the second element does not fall of if exposed to gravity.
  • Attachment can be achieved by e.g. forming a second element from a solution or gas on the first element, such as by chemical reaction, by deposition, by ( thermo- ) pressing the first element on the second element, by applying an adhesive, and vice versa.
  • the attachment can be established over a full area of the smaller of the two elements, or over a part thereof. Attachment may be disrupted, e.g. due to a sub-optimal attachment process, the nature of an element, incompatibility of elements, etc.
  • the present chemical fuel can in principle be any fuel that can be made from fluids by electrolysis; the fuel provides energy when it is oxidized.
  • the present system relates to a stack-like structure of various components.
  • the stack may be in any suitable form, such as a stack, a tube-like stack, etc.
  • the first electrode and first compartment are in ionic contact, hence adjacent to one and another.
  • the first electrode may in principle be any electrode capable of oxidizing the first fluid being present in the first compartment.
  • the electrode optionally is high surface/volume electrode.
  • any gaseous or liquid is indi- cated.
  • adjacent it is implied two elements that are adjacent are in direct or indirect contact with one and another
  • the first and second compart- ment are physically separated by a double layer structure, such as a bipolar membrane.
  • the double layer structure comprises two layers, a first layer adjacent to and in contact with the first fluid or first electrode, acting as an anion exchange layer (AEL) , and a second layer adjacent to and in contact with the cathode, acting as a cation exchange layer (CEL) .
  • AEL anion exchange layer
  • CEL cation exchange layer
  • the first electrode may therefore be attached to the present double layer structure, or, in an alternative, may be separated from the double layer structure by the first fluid in the first compartment.
  • a further layer may be present.
  • the AEL and CEL are typically parallel and adjacent to one and another, and in an example in contact with one and another.
  • a bipolar membrane is used.
  • the double layer acts as a barrier at least for oxidized species.
  • a bipolar membrane is typically applied in the production of acid and base.
  • a bipolar membrane has been used for microbial fuel cells and fuel cells, which processes are different from the present tech- nology.
  • the water is not being dissociated when using it in a fuel cell, but instead H + and OH " recombine to water in this case.
  • H + and OH recombine to water in this case.
  • This is considered an important difference, not only because the process is opposite in goal (e.g. making water versus the present splitting water) , but also because water will be accumulated in the interfacial layer in the bipolar membrane, which causes blistering and high electrical resistance of the membrane; hence the bipolar membrane is not suitable in this respect.
  • the bipolar membrane remains stable.
  • a bipolar membrane has been reported for fuel production, but in both cases there was no electrode attached to the membrane. In both cases, an aqueous solution was applied at both sides of the bipolar membrane.
  • the present system further comprises a second elec- trode, which is attached to the CEL, that is in ionic contact with said layer and adjacent to said layer.
  • the first electrode is typically the anode, whereas the second electrode is typically the cathode.
  • the compartment Adjacent to the second electrode a second compart ⁇ ment for reduction is present, the compartment comprising a second fluid for reduction in cation exchange contact with the second electrode.
  • the second electrode and second compartment are in ionic contact, hence adjacent to one and another.
  • the second electrode may in principle be any electrode capable of reducing the second fluid being present in the second compartment.
  • a power source in electrical contact with the first and second electrode is provided.
  • the power source can retrieve its power in principle from any electrical power source; if a DC source is used preferably a transformer is provided.
  • chemical fuels can be generated using electrochemical reduction and oxidation.
  • the most common example thereof is the oxidation and reduction of water, where hydrogen and oxygen are evolved.
  • CO2 can be reduced, together with water oxidation, to obtain carbon monoxide.
  • the combination of these reactions can yield hydrocarbons, which can be used as fuel.
  • the present system provides a stable and selective reaction at high rate, using e.g. a system with a bipolar membrane and an embedded electrode in this membrane.
  • a possible design of such a system 100 is described in Fig. 1.
  • the present invention provides design flexibility. Several variations on the present system can be created. In particular, the use of tubular membranes, with a gas phase inside the tube, is considered.
  • the tube may be cylindrical (circular cross-section ⁇ , polygonal cross-sectional, such as square, rectangular, triangular, hexa-angular, oval, etc. It provides the following advantages:
  • the tube provides a relatively short average distance for an arbitrary molecule/atom in the fluid to the electrode
  • porous carbon graphite
  • the tube allows selection of a larger or smaller area for the cathode compared to the anode, respectively. This is considered beneficial if one of the two electrodes is limiting for the process selected.
  • a limited number of tubes provides the possibility of hav- ing a solar panel behind the system, even when the bipolar membranes and cathodes are not transparent. Only a part of the light is interrupted by the tubes, while light can freely pass at the positions where no tube interrupts the light.
  • the present invention relates in a first aspect to a system for producing a chemical fuel according to claim 1.
  • the first fluid is an aqueous solution, such as comprising a hydroxide, or a gas .
  • the double layer is a bipolar membrane.
  • the second fluid is a gas, such as hydrogen, carbon monoxide, carbon dioxide, and combinations thereof.
  • the first fluid provides hydrogen ions, in order to make a chemical fuel thereof .
  • the second fluid provides a carbon dioxide molecule.
  • the power source is a PV-source, such as a PV-element attached to the first electrode (adjacent to the first liquid) and/or a PV-element attached to the second electrode.
  • a PV-source such as a PV-element attached to the first electrode (adjacent to the first liquid) and/or a PV-element attached to the second electrode.
  • the double layer is curved, such as a tube, wherein the anion exchange layer is on a convex side of the double layer and the cation exchange layer is on a concave side of the double layer.
  • the concave side is filled with a porous material, such as with carbon.
  • a first electrode (70) comprises Ni or NiFe.
  • the present system provides herewith as further advantage that good affordable materials as Ni and Fe can be used without a risk of deposition of these materials on a second electrode (cathode) .
  • a second electrode (60) comprises at least one of Cu, Pt and Ag.
  • the present invention relates to a method of producing a chemical fuel according to claim 13.
  • the method comprises the steps of providing a system accord- ing to the invention, having a suitable first fluid and a suitable second fluid, and producing a chemical fuel, the chemical fuel being selected from hydrogen, a hydrocarbon, CO, a combination of CO and 3 ⁇ 4, such as syngas, an alcohol, and combinations thereof.
  • the production is established under suitable conditions.
  • the electric power is provided by at least one PV-system.
  • the electric power is provided by at least one PV-system.
  • integration of a PV-element within the present system is now possible.
  • one or more of a cathode area, an anode area, a number of electrodes, a ratio between to be oxidized first fluid and to be reduced second fluid, and product selectivity are tuned. Therewith reaction conditions and as a consequence e.g. yield and selectivity are further optimized.
  • the cathode operates in acidic conditions, the pH preferably being between 1-7, more preferably between 3-6.5, such as 4-6 or 5, and/or wherein the anode operates in basic conditions, the pH preferably being between 9-14, more preferably between 10-13.5, such as between 11-13.
  • Acidic conditions typically relate to a pH ⁇ 6, more typically a pH ⁇ 4, depending on the chemical spe ⁇ cies involved, whereas the basic conditions typically relate to a pH>9, more typically a pH>10.
  • acidic conditions are a pH of 6.5 and basic conditions are a pH of 14; this is considered a unique feature of the present system, as prior art systems typically operate at much larger pH- differences c.q. gradients.
  • the present system provides good yields.
  • the acidic conditions are a pH of 5-6.5. At this pH a relatively large concentration of CO 2 can be present, whereas the C0 2 is typically present as HC0 3 " , which is a favourable species in view of yield.
  • a cathode 60 was made from a copper wire mesh, cut in a round shape with a diameter of approximately 5 cm and a weight of 0.98 gram.
  • the cathode was attached to the present membrane 50 by positioning the copper mesh on top of the bipolar membrane and pipetting approximately 2 mL Nafion solution (5% w/w, dissolved in lower aliphatic alcohols and water) on the same bipolar membrane with copper mesh. After 1 hour, the solvent was evaporated, leaving the copper mesh at- tached to the bipolar membrane due to the dried Nafion polymer. See figure 3 for an illustration of this process.
  • This method is only one example to create a membrane electrode assembly (MEA) ; other methods for attaching the cathode in the bipolar membrane are possible as well.
  • MEA membrane electrode assembly
  • An anode 70 was made of a Ti plate with a Pt coating, prepared by magnetron sputtering. This anode was situated in a first compartment 31 filled with 1 M KOH and had a geometric area of approximately 4 cm 2 .
  • a second compartment 32 was separated from the first compartment by using a bipo- lar membrane, in which the anion exchange layer was facing the anode and the cation exchange layer was attached to the cathode as described previously.
  • the second compartment, which was in contact with the cathode, was filled with either C0 2 gas (99.995% pure) or 0.1 M KHC0 3 (99.995% pure) solution that was continuously purged with C0 2 gas. In all cases, the CO 2 gas flow was 4 mL/min.
  • An Ag/AgCl (Radiometer) reference electrode 21 was installed at the anodic compartment 31 via a capillary 21a that was positioned at approximately 1 mm distance from the anion exchange layer 51 of the bipolar mem- brane 50.
  • the potential between this reference electrode and the cathode was controlled using a potentiostat 24 (Princeton Applied Research), applying -1.9 V at the cathode versus the Ag/AgCl reference electrode, which corresponds to -0.9 V versus reversible hydrogen electrode (RHE) .
  • the current was measured with the same potentiostat.
  • the effluent gas composition from the cathodic compartment 32 was measured using gas chromatography (GC, ThermoScientific) and is vented after measuring. The setup is illustrated in Figure 4.
  • the temperature in these experiments was 25 ( ⁇ 2)°C, and the pressure was near atmospheric (100 kPa) (strictly speaking a slight overpressure to circulate the gas flow) .
  • the same cell was constructed using a copper cathode of the same size that was not attached to the bipolar membrane, but at approximately 10 mm distant from the bipolar membrane.
  • a solution of 0.1 M KHCO 3 was used in the cathodic compartment. All other elements were equal to the cases where the cathode was attached to the bipolar membrane.
  • Figure 5 shows the current density (mA/cm 2 ) as a function of time (h) , when applying -0.9 V vs RHE to the cathode for Cu in HC0 3 ⁇ (bottom line), for BPM EA in HC0 3 ⁇ ⁇ middle fluent line) and for BPM MEA in CO 2 gas (middle irregular line) .
  • Figure 6 shows the concentrations for the products CO and H 2 in the effluent gas, for the same cases as shown in Figure 5.
  • Figure 6 shows that the yield of fuel products (H 2 and CO in parts per thousand/million, respectively) as a function of time (h) using a HC0 3 ⁇ solution is significantly higher for the BPM MEA case (top line) and when the cathode is attached to the bipolar membrane (BPM) compared to the reference case (bottom line) when the cathode is not attached to the bipolar membrane. This higher yield is also reflected in the current density ( Figure 5), which is higher for the
  • the case in which the membrane electrode assembly (MEA) is operated in a gaseous C0 2 environment has a higher current density than the reference case and shows much higher yield for H 2 as well.
  • the CO yield is lower than for the other cases, but slightly increases over time, whereas the production rate for the reference case decreases over time.
  • Fig. 1 shows an illustration of bipolar membrane with embedded cathode.
  • FIG. 1 System design with bipolar membrane and embedded electrode in tubular shape and a photovoltaic (PV)- panel at the back side.
  • PV photovoltaic
  • FIG. 3 a method for attaching cathode to bipolar membrane.
  • CEL and AEL represent the cation exchange layer and anion exchange layer, respectively.
  • FIG 4 illustration of experimental setup.
  • the anion exchange layer 51 and cation exchange layer 52 are to- gether referred as the bipolar membrane 50.
  • Figure 5 current density as a function of time, at fixed cathode potential of -0.9 V vs RHE, for the bipolar membrane with attached Cu electrode (BPM MEA) in C0 2 gas, in 0.1 M HC0 3 " , and a Cu electrode (in 0.1 M HC0 3 ⁇ ) that was not attached to the bipolar membrane as a reference case.
  • FIG. 6 fuel production rate, indicated by the H 2 and CO product concentrations in the effluent gas, for the same cases as in figure 3.
  • Fig. 1 shows an illustration of a system 100
  • a bipolar membrane 50 having an anion exchange layer (AEL) 51 and a cation exchange layer (CEL) 52, a cathode 60 attached to the CEL, a first compartment 31 adjacent to the AEL, a second compartment 32 adjacent to the cathode, and an anode 70 adjacent to the first compartment. It is used for C0 2 reduction (in gas phase) to CO and H 2 (syngas) . The same system could be applied for water splitting (i.e., only H 2 and 0 2 evolution). Also an aqueous phase at both sides of the membranes is possible .
  • AEL anion exchange layer
  • CEL cation exchange layer
  • FIG 1A (left side) a typical system set-up is shown. On a top side a power source is indicated, connected to the anode (left) and cathode (right) . In the aqueous left side oxygen is generated (top left) and removed from the sys- tern. The membrane allows passage of hydrogen. On a right side carbon dioxide (top right ⁇ is provided, and syngas and water are generated.
  • FIG. IB (right side) a section of fig. 1A is enlarged. Therein the aqueous solution, comprising K + and OH " , the AEL, the CEL, the cathode, and the gas phase are shown) from left to right) . In the gas phase further H 2 is generated.
  • FIG. 2 System design with a bipolar membrane and embedded electrode in a tubular shape and an optional photovoltaic (PV) -panel at the back side. Light is absorbed by the photo anode and remaining light is absorbed by the PV-panel. This drives a redox reaction, in this case of C0 2 reduction and H 2 evolution. Combination with an additional power supply are possible as well.
  • PV photovoltaic
  • a tube 80 comprising a compartment 32 with a gas phase with carbon dioxide and carbon monoxide, the tube comprising an cathode 60, attached to the cathode a CEL 52, an AEL 51, the tube-structure being in an aqueous solution 31, comprising water.
  • an anode 70 is provided in the aqueous solution.
  • the anode is connected to a (first) solar system 91, whereas, as an alternative or in combination, a second solar system 92 is provided in contact with the cathode.
  • a solar system 92 is provided in contact with the cathode.

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  • 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)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

La présente invention concerne le domaine de la formation d'un combustible chimique, telle que par électrolyse de l'eau pour former de l'hydrogène. D'autres approches concernent la formation d'hydrogène, un hydrocarbure, un gaz de synthèse et un alcool pouvant également être formés. Ces combustibles chimiques peuvent être produits sur la base de fluides rapidement et facilement utilisables. Une source pour, par exemple, l'électrolyse peut être le rayonnement solaire.
PCT/NL2016/050189 2015-03-20 2016-03-17 Assemblage électrodes-membrane bipolaire pour la production de combustible Ceased WO2016153341A1 (fr)

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NL2014500 2015-03-20
NL2014500A NL2014500B1 (en) 2015-03-20 2015-03-20 Water splitting device.

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2019106456A1 (fr) * 2017-12-01 2019-06-06 Juan Jose Lozada Castro Réacteur qui produit de l'hydrogène à partir de la réduction des ions hydronium présents dans l'équilibre chimique de l'eau et par oxydation des molécules organiques présentes dans les excréments
CN116234835A (zh) * 2020-09-30 2023-06-06 富士胶片制造欧洲有限公司 膜

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Publication number Priority date Publication date Assignee Title
EP0459820A2 (fr) 1990-05-31 1991-12-04 Tokuyama Corporation Membrane bipolaire et son procédé de fabrication
US20070023290A1 (en) 2005-07-26 2007-02-01 Pionetics, Inc. Electrochemical ion exchange with textured membranes and cartridge
CN102912374A (zh) 2012-10-24 2013-02-06 中国科学院大连化学物理研究所 一种以双极膜为隔膜的电化学还原co2电解池及其应用
WO2014114806A1 (fr) * 2013-01-28 2014-07-31 Industrie De Nora S.P.A. Procédé de génération d'eau par électrolyse et générateur associé
US20150075997A1 (en) * 2013-09-18 2015-03-19 U.S. Army Research Laboratory Attn: Rdrl-Loc-I Power-free apparatus for hydrogen generation from alcohol

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0459820A2 (fr) 1990-05-31 1991-12-04 Tokuyama Corporation Membrane bipolaire et son procédé de fabrication
US20070023290A1 (en) 2005-07-26 2007-02-01 Pionetics, Inc. Electrochemical ion exchange with textured membranes and cartridge
CN102912374A (zh) 2012-10-24 2013-02-06 中国科学院大连化学物理研究所 一种以双极膜为隔膜的电化学还原co2电解池及其应用
WO2014114806A1 (fr) * 2013-01-28 2014-07-31 Industrie De Nora S.P.A. Procédé de génération d'eau par électrolyse et générateur associé
US20150075997A1 (en) * 2013-09-18 2015-03-19 U.S. Army Research Laboratory Attn: Rdrl-Loc-I Power-free apparatus for hydrogen generation from alcohol

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2019106456A1 (fr) * 2017-12-01 2019-06-06 Juan Jose Lozada Castro Réacteur qui produit de l'hydrogène à partir de la réduction des ions hydronium présents dans l'équilibre chimique de l'eau et par oxydation des molécules organiques présentes dans les excréments
CN116234835A (zh) * 2020-09-30 2023-06-06 富士胶片制造欧洲有限公司 膜

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