WO2022103158A1 - 음이온 교환막 수전해용 산화 전극 - Google Patents
음이온 교환막 수전해용 산화 전극 Download PDFInfo
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- WO2022103158A1 WO2022103158A1 PCT/KR2021/016363 KR2021016363W WO2022103158A1 WO 2022103158 A1 WO2022103158 A1 WO 2022103158A1 KR 2021016363 W KR2021016363 W KR 2021016363W WO 2022103158 A1 WO2022103158 A1 WO 2022103158A1
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- exchange membrane
- anion exchange
- water electrolysis
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 115
- 238000005868 electrolysis reaction Methods 0.000 title claims abstract description 86
- 239000003011 anion exchange membrane Substances 0.000 title claims abstract description 76
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims abstract description 164
- 229910052759 nickel Inorganic materials 0.000 claims abstract description 75
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- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 claims abstract description 55
- 229910052751 metal Inorganic materials 0.000 claims abstract description 45
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- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 33
- 239000000203 mixture Substances 0.000 claims description 22
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- 239000001257 hydrogen Substances 0.000 description 9
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- 229910002554 Fe(NO3)3·9H2O Inorganic materials 0.000 description 1
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- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
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- UGKDIUIOSMUOAW-UHFFFAOYSA-N iron nickel Chemical compound [Fe].[Ni] UGKDIUIOSMUOAW-UHFFFAOYSA-N 0.000 description 1
- VCJMYUPGQJHHFU-UHFFFAOYSA-N iron(3+);trinitrate Chemical group [Fe+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O VCJMYUPGQJHHFU-UHFFFAOYSA-N 0.000 description 1
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- KBJMLQFLOWQJNF-UHFFFAOYSA-N nickel(ii) nitrate Chemical group [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 description 1
- 238000005580 one pot reaction Methods 0.000 description 1
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- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 229910021642 ultra pure water Inorganic materials 0.000 description 1
- 239000012498 ultrapure water Substances 0.000 description 1
Images
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
- C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
- C25B11/04—Electrodes; Manufacture thereof not otherwise provided for characterised by the material
- C25B11/051—Electrodes formed of electrocatalysts on a substrate or carrier
- C25B11/073—Electrodes formed of electrocatalysts on a substrate or carrier characterised by the electrocatalyst material
- C25B11/091—Electrodes formed of electrocatalysts on a substrate or carrier characterised by the electrocatalyst material consisting of at least one catalytic element and at least one catalytic compound; consisting of two or more catalytic elements or catalytic compounds
-
- 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
- C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
- C25B11/04—Electrodes; Manufacture thereof not otherwise provided for characterised by the material
- C25B11/051—Electrodes formed of electrocatalysts on a substrate or carrier
- C25B11/052—Electrodes comprising one or more electrocatalytic coatings on a substrate
-
- 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
- C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
- C25B11/04—Electrodes; Manufacture thereof not otherwise provided for characterised by the material
- C25B11/051—Electrodes formed of electrocatalysts on a substrate or carrier
- C25B11/055—Electrodes formed of electrocatalysts on a substrate or carrier characterised by the substrate or carrier material
- C25B11/057—Electrodes formed of electrocatalysts on a substrate or carrier characterised by the substrate or carrier material consisting of a single element or compound
- C25B11/061—Metal or alloy
-
- 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
- C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
- C25B11/04—Electrodes; Manufacture thereof not otherwise provided for characterised by the material
- C25B11/051—Electrodes formed of electrocatalysts on a substrate or carrier
- C25B11/073—Electrodes formed of electrocatalysts on a substrate or carrier characterised by the electrocatalyst material
- C25B11/075—Electrodes formed of electrocatalysts on a substrate or carrier characterised by the electrocatalyst material consisting of a single catalytic element or catalytic compound
- C25B11/077—Electrodes formed of electrocatalysts on a substrate or carrier characterised by the electrocatalyst material consisting of a single catalytic element or catalytic compound the compound being a non-noble metal oxide
-
- 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
-
- 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 an oxidizing electrode for water electrolysis of an anion exchange membrane.
- alkaline aqueous electrolysis uses an aqueous alkali solution as a reactant, so an electrode material with strong corrosion resistance to aqueous alkali solution is required.
- Candidates for electrode materials include non-platinum-based metals such as nickel, iron, and cobalt, and relatively inexpensive electrode materials can be used. Since the electrode occupies a significant portion of the cost of water electrolysis, it has the advantage of lowering the cost of hydrogen production when a non-platinum-based metal is used.
- the alkaline water electrolysis system requires a large space and has a disadvantage in that the current per electrode area is low, and thus the efficiency is lowered due to the high overpotential required for hydrogen production.
- cation exchange membrane water electrolysis has the advantage of having a high energy density with a compact system design.
- a platinum-based metal capable of withstanding the acidic atmosphere of the cation exchange membrane is required, and thus hydrogen production cost is increased.
- anion exchange membrane water electrolysis is a system that can overcome the disadvantages while utilizing the advantages of existing systems. Because it is an alkaline environment, non-platinum-based metals can be used as electrode materials, and energy density can be obtained with a compact system design.
- An object of the present invention is to provide an oxidizing electrode for water electrolysis of an anion exchange membrane having low cost, high performance and high stability.
- nickel metal and a layered double hydroxide (LDH) of a monolayer structure including nickel and iron, located on one or both surfaces of the nickel metal; provides an oxidizing electrode for anion exchange membrane water electrolysis, including.
- LDH layered double hydroxide
- a layered double hydroxide (LDH) containing nickel and iron in a monolayer structure using a bottom-up method one surface of nickel metal Or, it provides a method of manufacturing an oxidized electrode for water electrolysis of an anion exchange membrane, comprising a series of processes of depositing on both sides.
- LDH layered double hydroxide
- an anion exchange membrane in another embodiment, an anion exchange membrane; and a reduction electrode and an oxidation electrode respectively positioned on both sides of the anion exchange membrane, wherein the oxidation electrode is the oxidation electrode of the above-described embodiment.
- the oxide electrode of one embodiment contains nickel and iron, which are non-precious metals, it can be efficiently produced at low cost and in a short time, and a layered double hydroxide of a monolayer containing nickel and iron is layered.
- double hydroxide (LDH) double hydroxide
- Figure 2a shows a B-NiFe-LDH synthesis method
- Figure 2b shows a M-NiFe-LDH synthesis method.
- Figure 3a shows a method of manufacturing an oxide electrode using B-NiFe-LDH
- Figure 3b shows a method of manufacturing an oxide electrode using M-NiFe-LDH.
- FIG. 4a and 4b are TEM images for Preparation Example 2 (B-NiFe-LDH), and FIG. 4c is an EDS mapping image at the same scale.
- FIG. 4d and 4e are TEM images for Preparation Example 1 (M-NiFe-LDH), and FIG. 4f is an EDS mapping image at the same scale.
- Example 5 is a powder catalyst of Comparative Example 1 (B-NiFe-LDH), dispersed in water to form a colloidal (colloidal) catalyst of Example 1 (M-NiFe-LDH), and dried in an oven It is a figure which shows each XRD pattern about the catalyst (M-NiFe-LDH) of Example 1 which became powder-like.
- FIGS. 6a to 6c are SEM images of the oxidized electrode (B-NiFe-LDH on Ni foam) of Comparative Example 1, and FIGS. 6d to 6f are the oxidized electrode (M-NiFe-LDH on Ni foam) of Example 1 SEM image.
- 7A is a current-voltage graph for each anion exchange membrane water electrolysis cell of Comparative Examples 1 to 5; 7B is a current-voltage graph for each anion exchange membrane water electrolysis cell of Examples 1 to 4; 7C is a current-voltage graph for each anion exchange membrane water electrolysis cell of Example 3, Comparative Examples 3 and 5, respectively.
- Example 8 is a stability evaluation graph for each anion exchange membrane water electrolysis cell of Example 3, Comparative Example 3, and Comparative Example 6.
- each layer or element is formed “on” or “over” each layer or element, it means that each layer or element is formed directly on each layer or element, or other It means that a layer or element may additionally be formed between each layer, on the object, on the substrate.
- nickel metal and a layered double hydroxide (LDH) of a monolayer structure including nickel and iron, which is located on one surface of the nickel metal, and provides an oxidizing electrode for water electrolysis of an anion exchange membrane, including.
- LDH layered double hydroxide
- the layered double hydroxide (LDH) of a monolayer structure including nickel and iron located on one or both surfaces of the nickel metal functions as an oxygen evolution catalyst .
- the oxidation electrode of the embodiment includes a single-layered catalyst layer, and the single-layered catalyst layer is a layered double hydroxide containing nickel and iron.
- a layered double hydroxide is a type of ionic solid having a two-dimensional structure.
- n has a multilayer structure of [(AcB)-Z-(AcB)] n , where c denotes a metal cation layer, A and B denote a hydroxide ion (OH) layer, respectively, and Z denotes another anion. and a layer containing neutral molecules (eg water), where n is the number of repeats.
- the inserted anion or neutral molecule (Z) is weakly bound and exchangeable with another anion or neutral molecule.
- interlayer basal spacing the distance between the AcB layers with anions or neutral molecules (Z) interposed therebetween is called interlayer basal spacing.
- NiFe-LDH bulk layered double hydroxide
- B-NiFe-LDH layered double hydroxide containing nickel and iron in the bulk state
- B-NiFe-LDH comprises a first hydroxide ion (OH-) layer (A), a metal layer comprising nickel and iron (c), and a second hydroxide ion (OH-) layer (B). a monolayer as one unit (AcB); Between the two units ( AcB ) , a plurality of units are stacked [(AcB)-Z-(AcB) ] has n .
- Such B-NiFe-LDH has a major disadvantage to be used as an anion exchange membrane water electrolysis catalyst, the representative reasons of which are low electrical conductivity and low stability.
- M-NiFe-LDH unlike B-NiFe-LDH, it has a structure in which all basal planes are exposed to the reactant (OH-). In this structure, as OH ⁇ is consumed, a partial acidic environment is not generated, and the problem of dissolving the catalyst can be solved. In other words, M-NiFe-LDH can solve the problem of low stability caused by B-NiFe-LDH.
- the oxide electrode of one embodiment includes a layered double hydroxide (LDH) having a monolayer structure containing nickel and iron. -LDH".
- LDH layered double hydroxide
- M-NiFe-LDH including only one unit (AcB), can solve the problems of low electrical conductivity and low stability of B-NiFe-LDH.
- M-NiFe-LDH has a higher intrinsic OER activity compared to B-NiFe-LDH due to its single-layer structure, and can improve anion exchange membrane water electrolysis performance.
- the M-NiFe-LDH can be prepared using a bottom-up method or a top-down method (top-down method).
- the bottom-up method may be capable of manufacturing an electrode with a simple and efficient manufacturing process compared to the top-down method.
- M-NiFe-LDH is more affected by the substrate due to its thinner thickness compared to B-NiFe-LDH.
- a material having high electrical conductivity such as nickel metal (eg, nickel foam, Ni foam) as a substrate, the electrical conductivity of the oxide electrode can be further supplemented.
- the oxide electrode of the embodiment includes M-NiFe-LDH prepared in a bottom-up manner as a catalyst layer and nickel metal as a substrate, so that stability is improved and electrical conductivity is improved at the same time it will be improved
- the oxidation electrode does not contain any catalyst layer; an oxide electrode comprising B-NiFe-LDH as a catalyst layer; an oxide electrode comprising M-NiFe-LDH prepared in a top-down manner as a catalyst layer; In preparation for the above, the optimal amount of catalyst may be increased, and the performance of the water electrolysis cell may be improved.
- the weight ratio of nickel/iron in the layered double hydroxide (M-NiFe-LDH) may be 15/85 to 85/15.
- the weight ratio of nickel/iron may be controlled.
- the weight ratio of nickel/iron in the layered double hydroxide may be controlled within a range of 25/85 to 85/25.
- the loading amount of the layered double hydroxide (M-NiFe-LDH) per one side of the nickel metal may be 0.1 to 5 mg/cm 2 .
- the performance of the anion exchange membrane water electrolysis cell is improved, showing the highest performance at 3 mg/cm 2 , and exceeding 3 mg/cm 2 performance may decrease in the range of
- the loading amount of the layered double hydroxide (M-NiFe-LDH) per one side of the nickel metal is 0.1 mg/cm 2 or more, 0.3 mg/cm 2 or more, 0.6 mg/cm 2 or more, or 1 mg/cm 2 or more, and 5 mg/cm 2 or less, 4.5. mg/cm 2 or less, or 4 mg/cm 2 or less, can be controlled within a range.
- the thickness of the layered double hydroxide (M-NiFe-LDH) may increase in proportion to the loading amount thereof.
- the nickel metal may be a nickel foam including a plurality of pores therein.
- the porosity of the nickel metal may be 50 to 200 Pores per inch (PPI), specifically 70 to 170 PPI, such as 110 PPI.
- the thickness of the nickel metal may be 150 to 350 ⁇ m, specifically 200 to 300 ⁇ m, for example, 250 ⁇ m.
- a layered double hydroxide (LDH) containing nickel and iron in a monolayer structure using a bottom-up method one surface of nickel metal Or, it provides a method of manufacturing an oxidized electrode for water electrolysis of an anion exchange membrane, comprising a series of processes of depositing on both sides.
- LDH layered double hydroxide
- a top-down method and a bottom-up method may be considered.
- a bottom-up method is used, in which a manufacturing process is simple and efficient electrode manufacturing is possible compared to a top-down method.
- the method for manufacturing an oxidized electrode of one embodiment includes the steps of: preparing a raw material mixture solution by adding an aqueous alkali solution, and an aqueous metal solution including a nickel source and an iron source to an aqueous formamide solution; generating a layered double hydroxide (LDH) having a monolayer structure including nickel and iron by reacting the raw material mixture solution; and applying the layered double hydroxide on one or both surfaces of the nickel metal.
- LDH layered double hydroxide
- NiFe-LDH having a single layer structure can be prepared from B-NiFe-LDH. This is to increase the interlayer basal spacing of B-NiFe-LDH through intercalated anion exchange, disperse it in a formamide solvent, and then peel off each layer by sonication. As a method (exfoliation), a long time of about 1-2 weeks is required.
- the bottom-up method can manufacture M-NiFe-LDH through a one-step reaction, thereby simplifying the manufacturing process, and synthesizing it within about 1 hour, thereby greatly reducing the manufacturing time.
- the finally obtained M-NiFe-LDH is dispersed in distilled water, and quick drying is possible compared to a top-down method of formamide solvent, and efficient electrode manufacturing is possible. make it
- the aqueous metal solution may include, in a total amount (100 wt%), 0.5 to 1.5 wt% of a nickel source, for example 0.7 to 1.3 wt%; 0.1 to 1.0% by weight of an iron source, such as 0.2 to 0.7% by weight; and the remainder of water.
- the nickel source is nickel nitrate (Ni(NO 3 ) 2 ) or its hydrate (Ni(NO 3 ) 2 .6H 2 O), and the iron source is iron nitrate (Fe(NO 3 ) 3 ) or its hydrate (Fe). (NO 3 ) 3 ⁇ 9H 2 O).
- the aqueous alkali solution may be an aqueous sodium hydroxide solution.
- the molar concentration of the aqueous sodium hydroxide solution is 0.05 to 5 M, such as 0.1 to 3 M; and the remainder of water.
- the aqueous sodium hydroxide solution may serve to adjust the pH to 9 to 11 by providing OH ⁇ required during catalyst synthesis.
- the sodium hydroxide content in the sodium hydroxide aqueous solution satisfies the above range, a desired shape, size, etc. of the catalyst can be obtained.
- the aqueous solution of formamide is, in the total amount (100% by volume), formamide 15 to 40% by volume, for example, 20 to 30% by volume; and the remainder of water.
- the formamide aqueous solution may play a role in inhibiting the growth in the z-axis (layered structure) by interacting with the hydroxide during catalyst synthesis. Accordingly, when the formamide content in the formamide aqueous solution satisfies the above range, the layered double hydroxide (M-NiFe-LDH) can be obtained.
- the raw material mixture solution based on 100 parts by weight of the aqueous formamide solution, 50 to 200 parts by weight of the aqueous alkali solution, for example 70 to 130 parts by weight; and 50 to 200 parts by weight of the aqueous metal solution, for example 70 to 130 parts by weight; may be mixed.
- the pH of the raw material mixture solution may be controlled within a range of 9 to 11, for example, 9.5 to 10.5 by using the aqueous alkali solution.
- the pH may affect the final form of the catalyst.
- the layered double hydroxide (M-NiFe-LDH) can be well synthesized.
- the reaction of the raw material mixture solution may be performed within a temperature range of 70 to 90 °C, for example, 75 to 85 °C.
- the temperature may affect the catalyst synthesis rate, thereby affecting the shape and size of the catalyst.
- the reaction of the raw material mixture solution may be performed for 1 to 20 minutes, for example, 5 to 15 minutes.
- the reaction time may affect the crystallinity of the catalyst.
- a washing solvent eg, a mixture of water and ethanol
- impurities remaining in the layered double hydroxide (M-NiFe-LDH) are removed from the solvent
- centrifugation may be performed to remove the solvent in which the impurities are dissolved.
- an aqueous solution containing the layered double hydroxide and water may be applied.
- Nafion since Nafion is dispersed and applied together with the catalyst, it may serve as a binder to prevent the catalyst from being desorbed during the reaction.
- the Nafion solution one having a Nafion content of 5 to 10% by weight among the total amount (100% by weight) may be used.
- a spray drying method may be used.
- the nickel metal when the layered double hydroxide is applied, the nickel metal may be positioned on a hot plate at 70 to 90 °C.
- the spray drying it may be advantageous to evenly apply the catalyst, and at this time, when the temperature of the nickel metal is within the above range, the evaporation rate of the solvent may be well controlled so that the catalyst is evenly applied.
- an anion exchange membrane in another embodiment, an anion exchange membrane; and a reduction electrode and an oxidation electrode respectively positioned on both sides of the anion exchange membrane, wherein the oxidation electrode is the oxidation electrode of the above-described embodiment.
- This may have improved water electrolysis performance by including the oxide electrode of the above-described embodiment.
- FIG 1 shows an electrolytic cell according to one embodiment.
- the water electrolysis cell of the embodiment may include a potentiostat connected to the reduction electrode and the oxidation electrode, respectively.
- the oxidation electrode uses the oxidation electrode of the above-described embodiment, and as the reduction electrode, platinum (Pt) and carbon (C) may be composite coated on carbon paper.
- a water electrolysis stack may be configured by using one water electrolysis cell as a unit cell and stacking a plurality of unit cells in series.
- the water electrolysis stack may include an electrolyte tank (not shown), and the electrolyte tank stores an aqueous alkali solution such as potassium hydroxide (KOH) and sodium hydroxide (NaOH), and serves to supply it to the anion exchange membrane.
- KOH potassium hydroxide
- NaOH sodium hydroxide
- hydroxide ions which are decomposition products of the aqueous alkali solution in the anion exchange membrane, are generated on the surface of the oxidation electrode.
- the catalytic reaction generates oxygen, water, and electrons, which can move to the reduction electrode along an external conductor.
- electrons and water catalytically react to generate hydrogen and hydroxide ions (OH ⁇ ).
- Oxygen generated from the oxidation electrode and hydrogen generated from the reduction electrode may be moved to and stored in a storage tank (not shown) outside the unit cell, respectively.
- Solution A aqueous metal solution
- the metal weight ratio of Ni:Fe is 3:1.
- Solution B aqueous alkali solution
- the internal temperature of the constant temperature water bath was prepared at 80 °C.
- the gel When the gel is precipitated during washing using the centrifugal separator, it can be sufficiently dispersed through bath sonication, and then the washing process can be performed again.
- aqueous solution of M-NiFe-LDH of Preparation Example 1 an aqueous solution containing M-NiFe-LDH and water (hereinafter referred to as "aqueous solution of M-NiFe-LDH of Preparation Example 1") was obtained.
- the solid content in the M-NiFe-LDH aqueous solution of Preparation Example 1 is about 88.33 wt% based on 100 wt% of the total aqueous solution.
- NiCl 2 ⁇ 6H 2 O 32 mmol and FeCl 3 10.7 mmol were added, and the solution was sufficiently dispersed by bath sonication to prepare Solution C.
- the metal weight ratio of Ni:Fe is 3:1.
- a nickel foam having a porosity of 110 PPI and a thickness of 250 ⁇ m was placed on a hot plate at 80° C.
- the sonicated aqueous solution was evenly sprayed on the nickel foam (Ni foam) to form a catalyst layer.
- Example 1 having a loading amount of 1.0 mg/cm 2 was prepared.
- each water electrolysis cell was prepared.
- a reduction electrode an electrode obtained by spray coating carbon (40 wt% Pt/C) supported with a platinum catalyst on carbon paper is used, and an anion exchange membrane (Sustainion TM , Dioxide Material) is used. company) was used.
- the oxidizing electrode and the reducing electrode were positioned on both sides to prepare a laminate in which an oxidizing electrode/anion exchange membrane/reducing electrode were stacked in this order, and then a gasket was placed and 100 kg ⁇ Pressurized with a torque of f ⁇ cm, the anion exchange membrane water electrolysis cell of Example 1 was completed.
- the cell has a reaction area of 5 cm 2 , a titanium block with single serpentine flow-pattern is used as a passage for delivering a reactant (1M KOH) and a product (oxygen) to the oxidation electrode, and a reactant (1M KOH) to the reduction electrode ) and a graphite block with a single serpentine flow-pattern were used as a passageway to deliver the product (hydrogen).
- This block is in contact with the gold plated current collector, which is connected to the potential stat.
- the manufacturing method of an anion exchange membrane water electrolysis cell generally known in the art was followed.
- Oxidation electrode and anion exchange membrane water electrolysis cell of Example 2 were prepared in the same manner as in Example 1, except that the loading amount of the catalyst layer per side of the nickel foam was changed to 2.0 mg/cm 2 did
- Oxidation electrode and anion exchange membrane water electrolysis cell of Example 3 were prepared in the same manner as in Example 1, except that the loading amount of the catalyst layer per side of the nickel foam was changed to 3.0 mg/cm 2 .
- Oxidation electrode and anion exchange membrane water electrolysis cell of Example 4 were prepared in the same manner as in Example 1, except that the loading amount of the catalyst layer per side of the nickel foam was changed to 4.0 mg/cm 2 .
- a nickel foam having a porosity of 110 PPI and a thickness of 250 ⁇ m was placed on a hot plate at 80° C.
- the sonicated aqueous solution was evenly sprayed on the nickel foam (Ni foam) to form a catalyst layer.
- a water electrolysis cell of Comparative Example 1 was prepared in the same manner as in Example 1, except that the oxidation electrode of Comparative Example 1 was used instead of the oxidation electrode of Example 1.
- Oxidation electrode and anion exchange membrane water electrolysis cell of Comparative Example 2 were prepared in the same manner as in Comparative Example 1, except that the loading amount of the catalyst layer per side of the nickel foam was changed to 1.5 mg/cm 2 did
- Oxidation electrode and anion exchange membrane water electrolysis cell of Comparative Example 3 were prepared in the same manner as in Comparative Example 1, except that the loading amount of the catalyst layer per side of the nickel foam was changed to 2.0 mg/cm 2 did
- Oxidation electrode and anion exchange membrane water electrolysis cell of Comparative Example 4 were prepared in the same manner as in Comparative Example 1, except that the loading amount of the catalyst layer per side of the nickel foam was changed to 3.0 mg/cm 2 did
- An oxidized electrode and anion exchange membrane water electrolysis cell of Comparative Example 5 were prepared in the same manner as in Comparative Example 1, except that Ni foam itself was used as the oxidation electrode.
- FIGS. 4A and 4B are TEM images for Preparation Example 2 (B-NiFe-LDH), and FIG. 4C is an evaluation of element distribution on the same scale.
- FIGS. 4d and 4e are TEM images for Preparation Example 1 (M-NiFe-LDH), and FIG. 4f is an evaluation of element distribution on the same scale.
- Preparation Example 2 B-NiFe-LDH
- M-NiFe-LDH M-NiFe-LDH
- Example 5 is a powder catalyst of Comparative Example 1 (B-NiFe-LDH), dispersed in water to form a colloidal (colloidal) catalyst of Example 1 (M-NiFe-LDH), and dried in an oven It is a figure which shows each XRD pattern about the catalyst (M-NiFe-LDH) of Example 1 which became powder-like.
- the catalyst of Example 1 (M-NiFe-LDH) is applied in a colloidal phase, but the catalyst of Example 1 (M-NiFe-LDH) is applied to the dried oxide electrode after preparation. exists in a dry state.
- FIGS. 6a to 6c are SEM images of the oxide electrode (B-NiFe-LDH on Ni foam) of Comparative Example 1, and it can be confirmed that nanoparticles in a bulk state are present in agglomerated state. there is.
- FIGS. 6d to 6f are SEM images of the oxide electrode (M-NiFe-LDH on Ni foam) of Example 1, and a smooth surface is confirmed because NiFe-LDHs of a monolayer are closely attached.
- the contact properties with nickel metal are excellent, and the contact properties with the anion exchange membrane are also excellent, which can improve the performance of the anion exchange membrane water electrolysis cell.
- FIG. 7A A current-voltage graph for each anion exchange membrane water electrolysis cell of Comparative Examples 1 to 5 is shown in FIG. 7A;
- FIG. 7B A current-voltage graph for each anion exchange membrane water electrolysis cell of Examples 1 to 4 is shown in FIG. 7B ;
- 7c shows current-voltage graphs for each anion exchange membrane water electrolysis cell of Comparative Example 5, as well as Example 3, which had the highest efficiency among Examples, and Comparative Example 3, which was the most efficient among Comparative Examples.
- the driving conditions were 50° C. and 1 A/cm 2 .
- ⁇ is the energy conversion efficiency “energy conversion efficiency”.
- E0 is the thermodynamically required voltage for water electrolysis (H 2 O ⁇ H 2 + 1 ⁇ 2 O 2 ),
- V is the measured voltage
- ⁇ G is the free energy changed after the water electrolysis reaction
- n is the number of participating electrons (2)
- F is a faradaic constant (96485 C/mol).
- Example 3 which was the most efficient among Examples
- Comparative Example 3 which was the most efficient among Comparative Examples
- Comparative Example 6 using a commercially available Iridium oxide (IrO x ) catalyst stability was evaluated.
- Example 3 in the case of Example 3 and Comparative Example 3, stable driving was performed compared to Comparative Example 6. Among them, it can be seen that the driving of Example 3 is more stable.
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Abstract
Description
Claims (19)
- 니켈 금속; 및상기 니켈 금속의 일면 상에 위치하고, 니켈과 철이 포함된 단층 구조(monolayer)의 층상 이중 수산화물(layered double hydroxide, LDH);을 포함하는,음이온 교환막 수전해용 산화 전극.
- 제1항에 있어서,상기 층상 이중 수산화물 내 니켈/철의 중량 비율은,15/85 내지 85/15인 것인,음이온 교환막 수전해용 산화 전극.
- 제1항에 있어서,상기 니켈 금속의 편면 당 상기 층상 이중 수산화물의 로딩량은,0.1 내지 5 mg/cm2 인 것인,음이온 교환막 수전해용 산화 전극.
- 제1항에 있어서,상기 니켈 금속의 두께는,150 내지 350 ㎛인 것인,음이온 교환막 수전해용 산화 전극.
- 제1항에 있어서,상기 니켈 금속의 기공도는,50 내지 200 PPI인 것인,음이온 교환막 수전해용 산화 전극.
- 포름아마이드 수용액에, 알칼리 수용액, 그리고 니켈 소스 및 철 소스를 포함하는 금속 수용액을 투입하여, 원료 혼합 용액을 제조하는 단계;상기 원료 혼합 용액을 반응시켜, 니켈과 철이 포함된 단층 구조(monolayer)의 층상 이중 수산화물(layered double hydroxide, LDH)을 생성하는 단계; 및니켈 금속의 일면 또는 양면 상에, 상기 층상 이중 수산화물을 도포하는 단계;를 포함하는,음이온 교환막 수전해용 산화 전극의 제조 방법.
- 제6항에 있어서,상기 금속 수용액은,총량(100 중량%) 중, 니켈 소스 0.5 내지 1.5 중량%, 철 소스 0.1 내지 1.0 중량%, 및 잔부의 물을 포함하는 것인,음이온 교환막 수전해용 산화 전극의 제조 방법.
- 제6항에 있어서,상기 알칼리 수용액은,수산화나트륨 수용액인 것인,음이온 교환막 수전해용 산화 전극의 제조 방법.
- 제8항에 있어서,상기 수산화나트륨 수용액의 몰 농도는,0.05 내지 5 M인 것인,음이온 교환막 수전해용 산화 전극의 제조 방법.
- 제6항에 있어서,상기 포름아마이드 수용액은,총량(100 부피%) 중, 포름아마이드 15 내지 40 부피% 및 잔부의 물을 포함하는 것인,음이온 교환막 수전해용 산화 전극의 제조 방법.
- 제6항에 있어서,상기 원료 혼합 용액의 제조 시,상기 포름아마이드 수용액 100 중량부 기준, 상기 알칼리 수용액 50 내지 200 중량부, 및 상기 금속 수용액 50 내지 200 중량부를 혼합하는 것인,음이온 교환막 수전해용 산화 전극의 제조 방법.
- 제6항에 있어서,상기 원료 혼합 용액의 반응은,pH 9 내지 11 범위 내에서 수행되는 것인,음이온 교환막 수전해용 산화 전극의 제조 방법.
- 제6항에 있어서,상기 원료 혼합 용액의 반응은,70 내지 90 ℃의 온도 범위 내에서 수행되는 것인,음이온 교환막 수전해용 산화 전극의 제조 방법.
- 제6항에 있어서,상기 원료 혼합 용액의 반응은,1 내지 20 분 동안 수행되는 것인,음이온 교환막 수전해용 산화 전극의 제조 방법.
- 제6항에 있어서,상기 원료 혼합 용액의 반응 후,세척 용매를 이용하여 상기 층상 이중 수산화물을 세척하는 단계; 및상기 세척된 상기 층상 이중 수산화물을 물에 분산시키는 단계;를 더 포함하는 것인,음이온 교환막 수전해용 산화 전극의 제조 방법.
- 제6항에 있어서,상기 층상 이중 수산화물의 도포 시,상기 층상 이중 수산화물에 나피온 용액을 첨가한 뒤 도포하는 것인,음이온 교환막 수전해용 산화 전극의 제조 방법.
- 제6항에 있어서,상기 층상 이중 수산화물의 도포 시,분무 건조 방법을 이용하는 것인,음이온 교환막 수전해용 산화 전극의 제조 방법.
- 제6항에 있어서,상기 층상 이중 수산화물의 도포 시,상기 니켈 금속은 70 내지 90 ℃의 핫 플레이트 상에 위치하는 것인,음이온 교환막 수전해용 산화 전극의 제조 방법.
- 음이온 교환막; 및상기 음이온 교환막의 양측에 각각 위치하는 환원 전극 및 산화 전극을 포함하고,상기 산화 전극은 제1항의 산화 전극인 것인,음이온 교환막 수전해 셀.
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AU2021379496A AU2021379496A1 (en) | 2020-11-11 | 2021-11-10 | Anode for anion exchange membrane water electrolysis |
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JP2023528317A JP2023549368A (ja) | 2020-11-11 | 2021-11-10 | 陰イオン交換膜水電解用酸化電極 |
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KR100481591B1 (ko) * | 2002-11-13 | 2005-04-08 | 주식회사 협진아이엔씨 | 연료전지용 고분자 나노복합막, 그의 제조방법 및 이를이용한 연료전지 |
EP3015429A1 (en) * | 2014-10-30 | 2016-05-04 | Wintershall Holding GmbH | Monolayer from at least one layered double hydroxide (LDH) |
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KR20200119097A (ko) * | 2019-04-09 | 2020-10-19 | 한국과학기술연구원 | 양기능성 수전해용 전극촉매 및 그 제조방법, 그리고, 상기 전극 촉매를 포함하는 수전해 전지 |
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KR100481591B1 (ko) * | 2002-11-13 | 2005-04-08 | 주식회사 협진아이엔씨 | 연료전지용 고분자 나노복합막, 그의 제조방법 및 이를이용한 연료전지 |
EP3015429A1 (en) * | 2014-10-30 | 2016-05-04 | Wintershall Holding GmbH | Monolayer from at least one layered double hydroxide (LDH) |
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