A separator for alkaline water electrolysis

Abstract

A separator for alkaline water electrolysis comprising: - a porous support (100) and on at least one side of the support, in order: - an optional porous layer including a Polymer A (200), and - a non-porous layer including a Polymer B (300), characterized in that the separator is obtainable by coating on the porous support (100) or the optional porous layer (200) a Polymer B solution having a viscosity of at least 400 mPa.s, measured at 20°C and a shear rate of 100 s-1, and wherein the separator has a Bubble Point, measured according to ASTM F316, of at least 5 bar.

Description

DescriptionA separator for alkaline water electrolysisTechnical field of the invention

[0001] The present invention relates to a separator for alkaline water electrolysis.Background art for the invention

[0002] Nowadays, hydrogen is used in several industrial processes, for example its use as raw material in the chemical industry and as a reducing agent in the metallurgic industry. Hydrogen is a fundamental building block for the manufacture of ammonia, and hence fertilizers, and of methanol, used in the manufacture of many polymers. Refineries, where hydrogen is used for the processing of intermediate oil products, are another area of use. However, the production of hydrogen from fossil fuels results in massive CO2emission.

[0003] Hydrogen is also being considered an important future energy carrier, which means it can store and deliver energy in a usable form. Energy is released by an exothermic combustion reaction with oxygen thereby forming water. During such combustion reaction no greenhouse gases containing carbon are emitted.

[0004] For the realization of a low-carbon society, renewable energies using natural energy such as solar light and wind power are becoming more and more important.

[0005] The production of electricity from wind power and solar power generation systems is very much dependent on the weather conditions and therefore variable, leading to an imbalance of demand and supply of electricity. To store surplus electricity, the so-called power-to-gas technology, wherein electrical power is used to produce gaseous fuel such as hydrogen, has attracted much interest in recent years. As production of electricity from renewable energy sources will increase, the demand for storage and transportation of the produced energy will also increase.

[0006] Water electrolysis is an important manufacturing process wherein renewable electricity may be converted into hydrogen. Hydrogen produced in this way is often referred to as green hydrogen, emphasizing that no greenhouse gases are formed during its production. Ammonia and steel prepared from or with green hydrogen are also referred to as green ammonia and green steel.

[0007] In an Alkaline Water Electrolysis (AWE) cell, a porous separator is used to separate electrodes of different polarity to prevent a short circuit between these electrodes and to prevent the recombination of hydrogen (formed at the cathode) and oxygen (formed at the anode) by avoiding gas crossover. In addition, the separator shouldexhibit a high ionic conductivity for the transportation of hydroxyl ions from the cathode to the anode.A separator for AWE, for example disclosed in EP-A 1776490 (VITO), W02009 / 147084 and W02009 / 147086 (AGFA-GEVAERT NV and VITO), typically comprises a porous polymer layer provided on a porous support. Inorganic particles, such as zirconium oxide, are added to the polymer layer to render it hydrophilic, ensuring sufficient electrolyte permeability and minimal adhesion of gas bubbles on the surface of the polymer layer.

[0008] For such porous separators, a compromise has to be found between high electrolyte permeability to ensure good ionic conductivity and low gas permeability to ensure good gas separation. Also, the porous nature of the separator typically results in a rough surface that may negatively influence bubble adhesion and contact with the electrode.

[0009] When an AWE electrolyser is operated using renewable energy as power source, the operating current densities vary considerably depending on the weather conditions. When the AWE electrolyser is operated at low current densities, the oxygen production decreases while hydrogen diffusion to the anode side remains more or less constant, which may result, for state-of-the-art porous separators, in a too high concentration of hydrogen in the oxygen stream (Hydrogen-to-Oxygen, HTO). Also, for electrolysers working at elevated pressures, HTO is a particularly important parameter to monitor. Above a HTO of 4 vol %, the gas mixture is explosive and therefore a maximum of 2 vol % for HTO has been agreed upon in the International Standard on hydrogen production using water electrolysis. Moreover, the minimum load of the electrolyser, i.e., the lowest current density at which the electrolyser may be operated in a safe way, is typically determined by the current density at which the HTO reaches 1 .6 vol. %.

[0010] The HTO of state of the art porous separator for AWE ZIRFON PERL UTP 500, available from AGFA-GEVAERT NV, has been improved by KIM et al. (Journal of Power Sources 524 (2022) 231059) by providing a thin layer of crosslinked poly(vinyl alcohol) (PVA) on the surface of the porous separator. The PVA layer has been applied by an ultrasonic spray coating process. The Bubble Point of the separator, measured according to ASTM F316, could be increased from 1.90 bar to approximately 3 bar.

[0011] In KR2022 / 0073190 (KOREA RESEARCH INSTITUTE OF CHEMICAL TECHNOLOGY) a porous separator has been provided with a crosslinked PVA layer containing a metal catalyst. The metal catalyst has the effect of further reducing the HTO by converting hydrogen passing through the porous membrane towater through a catalytic reaction together with oxygen, however at the expense of electrochemical efficiency. The PVA layer was also applied by an ultrasonic spray coating process.

[0012] There is however a need to further improve the HTO of porous separators. In addition, there is a need to realize such improved separators by means of a cost- effective large-scale manufacturing process.Summary of the invention

[0013] It is an object of the invention to provide a separator for alkaline water electrolysis having less hydrogen permeability and an improved crack-resistance while the areal resistance remains acceptable and to a method of producing such improved separators.

[0014] This object is realized with the separator as defined in claim 1 .

[0015] Further objects of the invention will become apparent from the description hereinafter.Brief description of the drawings

[0016] Figure 1 schematically illustrates several embodiments of a separator according to the present invention.

[0017] Figure 2 schematically illustrates several embodiments of a catalyst coated separator according to the present invention.

[0018] Figure 3 schematically illustrates an embodiment of an electrolytic cell according to the present invention.

[0019] Figure 4 shows a SEM cross section of the comparative catalyst coated separator S-18 prepared in Example 1 (Fig.4. a) and of the embodiment of a catalyst coated separator according to the present invention S-19 prepared in Example 5 (Fig.4.b).

[0020] Figure 5 shows a SEM image (top-view) of a surface of the state-of-the-art separator ZIRFON-1 (Fig.5. a) and of a surface of the embodiment of a separator according to the present invention S-1 prepared in Example 1 (Fig.5.b).Detailed description of the inventionSeparator

[0021] A separator as used herein may also be referred to as a diaphragm or a membrane.

[0022] The separator for alkaline water electrolysis according to the present invention comprises a porous support (100) and on at least one side of the support, in order:- an optional porous layer including a Polymer A (200), and- a non-porous layer including a Polymer B (300), characterized in that the separator is obtainable by coating on the porous support (100) or the optional porous layer a Polymer B solution having a viscosity of at least 400 mPa.s measured at 20 °C and a shear rate of 100 s’1, and wherein the separator has a bubble point of at least 5 bar, measured according to ASTM F316.

[0023] The bubble point of the separator is preferably at least 6 bar, more preferably at least 7 bar, most preferably at least 8 bar, measured according to ASTM F316.

[0024] It has been found that the viscosity of the Polymer B solution has a determining effect on the coating quality. Only when the viscosity of the Polymer B solution is sufficiently high, the coating covers the entire coating area. Optimal results are obtained when the viscosity of the Polymer B solution is at least 400 mPa.s, preferably at least 500 mPa.s, more preferably at least 800 mPa.s, most preferably at least 1000 mPa.s., measured at 20 °C and a shear rate of 100 s1. When the viscosity of the Polymer B solution is too low, the Polymer B solution penetrates the pores of the porous support or the porous polymer layer and therefore does not form a uniform non-porous layer. These lower viscosities result in heterogeneous coatings with varying coating quality, or even, when the viscosity is very low, in an overall poor coating quality over the entire coating area. Only when the viscosity of the Polymer B solution is at least 400 mPa.s, measured at 20 °C and a shear rate of 100 S’1, a uniform non-porous layer is formed.

[0025] The inventors have also surprisingly found a correlation between the viscosity of the polymer B solution and the bubble point and the gas permeability of the separator according to the present invention. Applying a polymer B solution with a high viscosity on the porous support results in a higher bubble point and lower gas permeability compared to state-of-the-art separators for AWE. This is clear from the examples described below.

[0026] Thus, to obtain a separator having a non-porous, homogeneous layer, the separator is coated with a Polymer B solution having a sufficiently high viscosity of above 400 mPa.s measured at 20 °C and a shear rate of 100 s’1. This viscosity ensures not only a homogeneous layer, but also a very high bubble point and a low gas permeability. It is possible that a high bubble point may already be reached at a Polymer B solution having a viscosity below 400 mPa.s; however, if the coating quality is not uniform due to a too low viscosity, the risk of gas cross-over might increase, potentially compromising safety and long-term performance.

[0027] The non-porous layer including a Polymer B may be provided on one or both sides of the porous support thereby forming one (300) or two (300, 300’) non-porous layers. In case two non-porous polymer layers are provided, these may be identical or different from each other.

[0028] The porous layer including a Polymer A may be provided on one or both sides of the porous support. In case two porous layers including a Polymer A (200, 200’) are provided on either side of the porous support, these may be identical or different from each other.

[0029] Different embodiments of a separator according to the present invention are schematically shown in Figure 1 (Fig. I .a to Fig.I .f).

[0030] The separator according to the present invention preferably includes one or two porous polymer layer(s) including a Polymer A, more preferably includes two porous polymer layers including a Polymer A on either side of the porous support.

[0031] When only one non-porous layer including a Polymer B is present, for example the embodiments depicted in Fig .1 .a, Fig.1 .c and Fig .1 .e, it has been observed that the non-porous layer is preferably provided on the side of the separator facing the cathode in an electrolytic cell because it that case the highest decrease in HTO will be observed. During the AWE process, it is more important to have control over the HTO (hydrogen to oxygen) than over the OTH (oxygen to hydrogen).

[0032] The total thickness of the separator is preferably from 50 to 750 pm, more preferably from 75 to 500 pm, most preferably from 100 to 250 pm. The areal resistance of the separator typically increases with the thickness of the separator. However, a minimal thickness is often necessary to ensure sufficient mechanical / physical properties of the separator and to facilitate manufacturing and handling of the separator.

[0033] The gas permeability of the separator is preferably less than 3 L / min.cm2, more preferably less than 1 .5 L / min.cm2, most preferably less than 0.5 L / min.cm2, particularly preferred less than 0.1 L / min. cm2. The gas permeability is preferably measured with a PoroluxTM 1000 apparatus at 5 bar. A too high gas permeability may result in an increase of the HTO (vol% hydrogen present in the oxygen stream formed at the anode).

[0034] Maximal ion-conductivity requires maximal electrolyte penetration of the electrolyte in the separator. The porosity of the separator is preferably from 40 to 90 %, more preferably from 50 to 80 %, most preferably from 60 to 70 %.

[0035] The presence of the non-porous layer may not result in a substantial increase of the areal resistance of the separator. The areal resistance of the separator is preferably less than 0.35 ohm. cm2, more preferably less than 0.25 ohm. cm2, most preferablyless than 0.10 ohm. cm2at 25°C in a 30 wt% aqueous KOH solution. The areal resistance is preferably determined with an Inolab® Multi 9310 IDS apparatus available from VWR, part of Avantor, equipped with a TetraCon 925 conductivity cell available from Xylem.

[0036] The separator may further comprise a catalyst layer (400) provided on the non- porous layer (300). Such a separator including a catalyst on one or both sides is often referred to as a catalyst coated separator (or catalyst coated membrane). It has been observed that the presence of a non-porous layer (300) between the porous support (100) and / or the porous polymer layer (200) and the catalyst layer avoids deposition of the catalyst into the pores of the porous support and / or the porous polymer layer.

[0037] A catalyst layer may be provided on at least one side of the separator according to the present invention. In case two catalyst layers (400, 400’) are provided on either side of the separator, these may be identical or different from each other. Different embodiments of a catalyst coated separator according to the present invention are schematically shown in Figure 2 (Fig. 2. a to Fig ,2.f) .

[0038] When only one catalyst layer is present, for example the embodiments depicted in Fig.2. a, Fig.2.c and Fig.2.e, it has been observed that the highest gain in electrolysis efficiency is obtained when the catalyst layer faces the cathode in an electrolytic cell.Non-porous layer including a Polymer B

[0039] The non-porous layer including a Polymer B, described below, is non-porous in the sense that is does not have fixed pores in the traditional meaning, i.e. permanent, well-defined pores or channels like those found in porous materials. Instead, ion transport through the non-porous layer occurs through temporary, dynamic voids or free-volume regions between individual polymer chains. These voids are formed due to the thermal motion and packing arrangement of the polymer chains. However, they are not static (or “fixed”) in structure and size. The size of these dynamic voids is typically less than 5 nm, in the order of Angstroms, from 0.1-5 nm (i.e. 1-50 A). According to the well-known solution-diffusion model, the size and chemistry of the voids allow selective transport of ions, while filtering out larger species. Thus, while the non-porous layer including a polymer B lacks fixed pores, the small and dynamic spaces between the polymer chains allow ion transport.

[0040] The non-porous layer including a Polymer B has to withstand typical AWE conditions, such as 30 wt % KOH at 80 °C during a prolonged time. Therefore, the non-porous layer preferably includes a Polymer B that is alkali-stable making thenon-porous layer and thus the separator according to the present invention suitable for alkaline water electrolysis. An alkali-stable polymer as used herein means a polymer that shows minimal degradation in polymer chain length or changes in the polymer chemistry after 4 weeks exposure to 6 M KOH at 120 °C.

[0041] Also, the non-porous layer may not adversely affect the areal resistance / conductivity of the separator. Therefore, the hydroxyl permeability of the non-porous layer in the AWE conditions must be sufficient.

[0042] Also, the non-porous layer preferably includes a polymer B that is hydrophilic as this will enhance the solubility of KOH (and water) in the non-porous layer and thus will result in a decrease of the gas permeability without adversely affecting the conductivity / areal resistance. A contact angle of water on the surface of the non- porous layer, measured as described below, is preferably less than 90 degrees, more preferably less than 75 degrees most preferably less than 60 degrees. Particularly preferred, a contact angle of water on the surface of the non-porous layer is from 40 to 60 degrees. It has been observed that less adhesion of gas bubbles occurs on hydrophilic non-porous layers resulting in a lower areal resistance.

[0043] Also, the non-porous layer preferably has a smooth surface to minimize gas bubble adhesion to the layer that may adversely affect the conductivity / areal resistance. A smooth surface also improves contact between the separator surface and the electrodes in an electrolytic cell. It has been observed (see the examples) that the surface of the non-porous layer is indeed smoother (less rough) than the surface of state-of-the-art separators without such a non-porous layer.

[0044] The hydroxyl permeability of the non-porous layer may be tuned amongst others by the layer thickness, the nature of Polymer B, the degree of crosslinking, the crosslinker type and by blending different Polymers B in the non-porous layer. This allows for the use of a wide range of polymers having different swelling characteristics in an aqueous alkaline medium.

[0045] The Polymer B is preferably crosslinked to further increase its long-term stability in the highly alkaline electrolyte of the electrolyser wherein the separator is used.

[0046] The non-porous layers may further include other ingredients to optimize its properties or to optimize the coating process. However, the non-porous layer of the invention preferably contains at least 50 parts per weight, more preferably at least 75 parts per weight, most preferably at least 90 parts per weight of the Polymer B to ensure sufficient hydroxyl permeability and smoothness of the non-porous layer and to retain sufficient mechanical properties.Other ingredients are, for example, surfactants (see below), inorganic particles (see below), viscosity regulators (see below) and recombination catalysts.

[0047] Preferred recombination catalysts are selected from the group consisting of NiO, Pt, Ir, lrO2 and stainless steel.

[0048] The thickness of the non-porous layer is preferably from 0.01 to 50 pm, more preferably from 0.1 to 25 pm, most preferably from 0.5 to 15 pm. When the thickness of the non-porous layer is more than 50 pm, the overall resistance of the membrane may become too high. On the other hand, when the thickness of the non- porous layer is less than 0.01 pm, the non-porous layer might potentially not cover the full separator surface.Polymer B

[0049] Polymer B may be selected from, for example, optionally modified polybenzimidazoles, polysulfones, poly(ether sulfones), poly(ether ketones), polyphenylene ethers), poly(ethers), poly(acetals), styrene based polymers and copolymers and poly(olefines) based polymers and copolymers. Preferred polymers have an all-carbon polymer backbone.

[0050] Polymer B is preferably functionalized with nonionic hydrophilic groups, where the modification is preferably a hydroxylation or an ethoxylation. Preferred hydrophilic fragments are selected from the group consisting of polyhydroxyl fragments and polyethylene oxide) fragments. The fragments may be part of or may be grafted on the polymer backbone. The hydrophilic fragments may be arranged in different geometries such as block copolymers or graft copolymers. Polyethylene glycol) based polymers or copolymers are particularly preferred, including block copolymers such as poly(olefin-block co-ethylene glycol) or graft copolymers such as poly(ethylene glycol) grafted on a poly(sulfone) or a poly(ether sulfone). Polyhydroxyl containing polymers are most preferred. Typical examples of polyhydroxy containing polymers include polysaccharides and vinyl alcohol based (co)polymers. Preferred polysaccharides include dextran and pullulan and derivatives thereof and starch derivatives. Preferred vinyl alcohol based (co)polymers include poly(vinyl alcohol), poly(ethylene-co-vinyl alcohol) and poly(ethylene-co-vinyl amine).

[0051] Polymer B is preferably selected from the group consisting of polyethylene glycol) or copolymers thereof, poly(saccharides), poly(ethylene-co-vinyl alcohol), poly(ethylene-co-vinyl amine) and poly(vinyl alcohol). A particularly preferred Polymer B is poly(vinyl alcohol) (PVA) or poly(ethylene-co-vinyl alcohol).

[0052] PVA is typically prepared by hydrolysis of poly(vinyl acetate). The properties of the PVA are determined by the degree of hydrolysis. Preferred hydrolysis degrees are from 50 to 100 %, more preferably from 70 to 99 %, most preferably from 85 to 98 %. It has been observed that non-porous layers including a PVA with a high degree of hydrolysis, i.e., above 85 %, are more hydrophilic and less soluble in water.

[0053] The molecular weight of polymer B is preferably from 10 to 250 kDa, more preferably from 15 to 150 kDa, most preferably from 50 to 125 kDa. It has been observed that a non-porous layer including a Polymer B with a high molecular weight, i.e., a Mw of at least 15 kDa, has an improved homogeneity. Additionally, when the Mw is lower than 15 kDA, it is possible that there are not enough chain entanglements between the polymer chains, resulting in worse film forming properties, and a lower overall durability of the separator. Although higher molecular weight polymers will result in non-porous layers with better mechanical properties, a too high molecular weight, i.e., a MW higher than 150 kDa, might be more difficult to process.Surfactants

[0054] The non-porous layer may include surfactants to optimize the coating process, to obtain homogeneous non-porous layers and / or to optimize the non-porous layer surface properties. Surfactants may be added to reduce the static and / or dynamic surface tension, to improve wetting on the separator surface, to improve levelling of the coated layer and to avoid coating defects such as orange peel, craters / fisheyes, mottling, Bernard cells, and Marangoni flow.

[0055] Suitable surfactants are for example modified silicone surfactants, such as siliconepolyether graft- and block copolymers or trisiloxanes. Preferred silicone polyether surfactants are Tego wet 240, Tego wet KL 248, Dynol 960, Dynol 980 and Tego Foamex 822 supplied by Evonik; Byk 348 and Byk 3450 supplied by Byk Chemie; Coatosil 7607 and Silwet L77 supplied by Momentive; and Hydropalat WE 3220 supplied by BASF. Silicone surfactants with a high hydrolytic stability are Byk 3420 supplied by Byk Chemie and Silwet HS312 and Silwet HS313 supplied by Momentive.

[0056] Another class of surfactants, which may be used are fluoro tensides, e.g., Tivida FL2500 or Tivida FL2700. However, the use of fluoro tensides is less preferred due to health and safety issues.

[0057] Other preferred surfactants are alkoxylated surfactants, such as alkyl ethoxylates or alkoxylated block copolymers. Examples are Lutensol AP6, Lutensol A8, PluronicPE10500 and Kauropal K933 supplied by BASF; Emulgen 109P and Akypo RLM100 supplied by Kao; and Ecosurf EH 6 supplied by Dow Chemical.

[0058] Also, mixtures of a silicone additive and an alkoxylated surfactant, e.g., Kauropal K933 and Tego foamex 822, may be used.

[0059] Acetylene derivatives may be used to reduce the surface tension of the coating solution, such as Dynol 604, Surfynol 104, Surfynol 420 and Surfynol 465. Dynol 604 is an ethoxylated surfactant based on 2,5,8, 11-Tetramethyldodec-6-yne-5,8- diol. Surfynol grades are based on 2,4,7,9-Tetramethyl-5-decyne-4,7-diol. Also, a hydrogenated surfynol derivative such as Surfynol AD01 may be used.

[0060] In order to optimize the compatibility with poly(vinyl alcohols), hydroxyl functional surfactants, such as alkyl polyglucoside surfactants, e.g. Glucopon 420 or Glucopon 100DK supplied by BASF; Simulsol SL 826 supplied by Seppic S.A; and polyglycidol or polyglycerol based surfactants, such as PGLAL ML04 and PGLAL ML08 supplied by Daicel Europe GmbH; and AEG 102 / 61 , supplied by Lamberti may be used. Biobased non-ionic surfactants like HoneySurf LF supplied by Holiferm may also be used.

[0061] Besides non-ionic surfactants, ionic surfactants may be used to improve the coating quality, i.e., anionic, cationic or amphoteric surfactants. One can also use precursors of ionic surfactants, which become ionic at low or high pH, e.g. carboxylated surfactants Akypo RLM45 and Akypo RLM100, which become anionic at a basic pH or surfactants having tertiary amine group, which become ionic at low pH. Suitable amphoteric surfactants are for example Euroglyc AMS supplied by EOC Surfactants, Arkopon T Paste 8015 supplied by Clariant and amineoxide surfactants like Makamine LO supplied by Verdant Specialty Solutions. Suitable anionic surfactants are Aerosol OT100 and Aerosol OT75E supplied by Solvay, Exodiss SE75 supplied by EOC Surfactants or Marlon A365 supplied by Sasol.

[0062] Some surfactants may be designed as anti-foam agent, for example silicone-based products or alkyl ethoxylates. Such surfactants typically have a lower HLB (hydrophilic-lipophilic balance) value. Examples of anti-foam agents are Tego Foamex 3062 or Tego Foamex 884, supplied by Evonik; Airase 5355 or Supread 2059, supplied by Elementis; and AF8014 supplied by Dow Chemical.Viscosity regulators

[0063] A so-called thickener or rheology modifier may be added to the Polymer B solution to optimize its viscosity.

[0064] Standard rheology modifiers, such as ASE (Alkali Swellable Emulsions), HASE (Hydrophobically Modified Alkali-soluble Emulsions) or HEUR (HydrophobicallyEthoxylated URethane polymers) based thickeners, may be used. Examples of commercially available standard rheology modifiers are Tego Visco Plus 3000, Tegovisco Plus 3010, Tafigel PUR80, ADDITOL VXW6388E, BYK-LP R 21675, Rheovis AS 1130, Rheolate 278 and Rheolate 255.

[0065] Other rheology modifiers are selected from gelatin, dextran, starch, collagen derivatives, alginate, chitosan, collodion and other polysaccharides, such as xanthan gum, arabic gum, guar gum, casein, carrageenan, pectin, albumin and cellulose based thickeners, such as methyl cellulose, CMC (carboxy methyl cellulose), HPMC (hydroxypropyl methyl cellulose) and HEC (hydroxyethyl cellulose). Other preferred thickening agents are polyethylene glycol, polyglycerol, polyglycidol or EO-PO copolymers and poly(vinyl pyrrolidone). Examples of trade names of specific thickeners are Kelzan S, Kelzan T, Kelzan RD, Natrosol 250HR, Tylose CR1500, Satialgine S170, Tylose H4000P, Ambergum 3031 , Walocel CRT10000, Dextran 60000, Biozan S, Polygel, Kelcogel, and Rheozan.

[0066] Highly preferred rheology modifiers are a high molecular weight poly(vinyl alcohol), a vinyl alcohol copolymer or a branched poly(vinyl alcohol), such as KURARAY POVAL 105 88 KX SB or KURARAY POVAL 200 88 KX SB branched PVA structures corresponding to CAS registry number 1643793-45-6. The addition of polyvinyl alcohol or vinyl alcohol copolymers as a thickener will give a good compatibility and does not change the properties of the layer to a large extent.

[0067] Other thickeners, which can be used are inorganic components such as clay, silica or other metal oxide particles. Examples are Laponite JS, Laponite RD, Levasil 300, Cab-o-sil M5, Aerosil 300, Aerosil 200, Bindzil CC151 HS, Bindzil CC301 , Luvotix HT, Luvogel 4, and Luvogel LD.Porous Support

[0068] The separator according to the present invention includes a porous support. Such a porous support provides mechanical strength to the separator, facilitating its production, handling and incorporation into an electrolyser.

[0069] A thickness of the porous support is preferably 350 pm or less, more preferably 200 pm or less, most preferably 100 pm or less, particularly preferred 75 pm or less. It has been observed that the ion conductivity through a reinforced separator increases when the thickness of the porous support decreases.However, to ensure sufficient mechanical properties of the reinforced separator, the thickness of the porous support is preferably 20 pm or more, more preferably 40 pm or more.

[0070] The porous support is preferably a non-woven fabric, a woven fabric, a mesh or a felt, more preferably a non-woven or woven fabric.

[0071] Woven fabrics typically have a better dimensional stability and homogeneity of open area and thickness. However, the manufacture of woven fabrics with a thickness of 100 pm or less is more complex resulting in more expensive fabrics. The manufacture of non-woven fabrics is less complex, even for fabrics having a thickness of 100 pm or less. Also, non-woven fabrics may have a larger open area.

[0072] The open area of the porous support is preferably from 30 to 80%, more preferably from 40 to 70 %, to ensure a good penetration of the electrolyte into the support. The density of the porous support is preferably between 0.1 to 0.7 g / cm3.

[0073] The fabric preferably has a fibre diameter from 10 pm to 200 pm, more preferably from 20 pm to 150 pm, most preferably from 30 pm to 100 pm. Fabrics having a lower thickness preferably have a smaller fibre diameter. For example, a fabric having a thickness of 150 pm or lower preferably contains fibres having a fibre diameter of 75 pm or lower, more preferably of 50 pm or lower, most preferably of 35 pm or lower.

[0074] To further reduce the thickness of the fabric, the ratio of the gauze thickness to the fibre diameter is preferably less than 2.0, more preferably 1 .7 or less, most preferably 1 .4 or less. A thinner fabric makes it possible to prepare thinner separators.

[0075] The porous support preferably includes a polymer such as for example polypropylene, polyethylene, polysulfone, polyphenylene sulfide, polyamide / nylon, polyether sulfone, polyphenyl sulfone, polyethylene terephthalate, polyether ether ketone, sulfonated polyether ether keton, monochlorotrifluoroethylene, copolymers of ethylene with tetrafluorethylene or chlorotrifluoroethylene, polyimide, polyether imide and m-aramide.

[0076] A preferred porous support includes polyphenylene sulphide (PPS) or polyether ether ketone (PEEK). A PPS or PEEK based porous support has a high resistance to high-temperature, high concentration alkaline solutions and a high chemical stability against active oxygen evolved from an anode during the water electrolysis process. Also, PPS and PEEK can be easily processed into various forms such as a woven fabric or a non-woven fabric.

[0077] The porous support is preferably a continuous web to enable a manufacturing process as disclosed in EP-A 1776490 and W02009 / 147084.

[0078] The width of the web is preferably between 30 and 300 cm, more preferably between 40 and 200 cm.Porous layer including a Polymer A

[0079] The porous polymer layer comprises a Polymer A, which is capable of forming a three-dimensional porous network during a phase inversion step described below. Such polymers are described below.

[0080] The porous polymer layer may further comprise inorganic particles. Such inorganic particles typically increase the hydrophilicity of the porous polymer layer resulting in a better permeability for the electrolyte. Moreover, it has been observed that the inorganic particles may improve the alkali-resistance of the polymer. Such inorganic particles are described below.

[0081] Porous polymer layers described for state-of-the-art porous separators, such as disclosed in for example EP-A 3933069 or W02023 / 280600, both from AGFA- GEVAERT NV, may be used in the separator according to the present invention. However, the porous layers in these state-of-the-art separators are characterized by a compromise between minimal gas permeability and maximal ion-conductivity. Due to the presence of the non-porous layer in the separator according to the present invention, minimal gas permeability of the porous polymer layer is no longer necessary, and the layer may be optimized for maximal ion-conductivity.

[0082] The surface pore diameters of the porous layer may not be too large to avoid a non- homogeneous non-porous layer or too small to avoid delamination of the non- porous layer from the porous support and / or porous polymer layer. The average surface pore diameters are preferably from 0.001 to 10 pm, more preferably from 0.01 to 5 pm, most preferably from 0.1 to 1 pm. Surface pore diameters are preferably measured with Scanning Electron Microscopy.

[0083] The pores of the porous polymer layer of a separator according to the present invention may be larger compared to those of state-of-the-art separators mentioned above, again due to the presence of the non-porous layer. The porous polymer layer may even include large finger-like pores.

[0084] The porous layer including a Polymer A may be provided on one or both sides of the porous support. When two porous polymer layers are provided, these may be identical of different from each other.

[0085] Porous layers including a Polymer A provided on both sides of the separator may the same or different from each other. Such porous layer may differ in:- composition, for example different Polymers A or different inorganic particles;- thickness, as for example disclosed in WO2023 / 208776 (AGFA-GEVEART NV);- pore sizes or porosity, for example by applying different phase transition conditions for both layers as disclosed in EP-A 3652362 (AGFA-GEVAERT NV).Polymer A

[0086] The porous layer comprises a Polymer A, which is capable of forming a three- dimensional porous network, the result of a phase inversion step in the preparation of the separator, as described below. An aqueous or organic medium may be used for the phase inversion leading to the porous structure.

[0087] When using an aqueous medium for the phase inversion, Polymer A is preferably an alkali-stable polymer, which is not swellable in an alkaline aqueous medium. Polymer A is preferably selected from the group consisting of high engineering plastics and polymers having a full carbon backbone.

[0088] High engineering plastics typically consist of an aromatic hydrocarbon containing backbone. High engineering plastics are preferably selected from the group consisting of poly(sulfones), poly(ether sulfones), poly(imides), poly(ether imides), poly(amide imides), poly(phenylene sulfides), poly(phenylene oxides) and poly(ether ketones).

[0089] Full carbon backbone containing polymers, also referred to as poly(hydrocarbons), are preferably selected from the group consisting of poly(olefine) and poly(styrene) based polymer. The poly(olefine) may be fluorinated or chlorinated. Typical examples of fluorinated and chlorinated poly(hydrocarbons) are poly(vinylidene fluoride) (PVDF), poly(tetrafluorethylene) (PTFE), poly(vinyl chloride) (PVC) and poly(vinylidene chloride) (PVDC). The poly(hydrocarbons) may be pure hydrocarbon, based on non-functionalized poly(olefines) such as poly(propylene) (PP) or low density poly(ethylene). Poly(styrene) based polymers may be a pure poly(styrene) or a styrene-based copolymer such as SEBS, also known as Kraton™. Functionalized poly(olefines) may also be used, such as hydrophobically modified poly(vinyl alcohol) derivatives Typical derivatives such as hydrophobic poly(acetals), e.g. poly(vinyl butyrals), may be used as a polymer in the porous layer according to the present invention. Poly(ethylene-co-vinyl alcohol), especially the grades with a high ethylene content may also be used. In specific cases non swellable poly(esters) may be used, such as polyethylene terephthalate) and pol(butylene terephthalate).

[0090] When an organic medium is used as phase inversion medium, alkali-stable hydrophilic polymers may be used for the phase inversion, followed by crosslinking of the hydrophilic polymer to make the layer stable in alkaline medium. Poly(vinyl alcohol) is a particularly preferred polymer. Crosslinking with di- or polyfunctional aldehydes is particularly preferred to make the layer alkaline resistant.

[0091] Polymer A is preferably selected from the group consisting of poly(sulfone), poly(ether sulfone), poly(phenylene sulfide), poly(ether ether ketone) and poly(phenyl sulfone), poly(sulfone) being the most preferred.

[0092] The porous layer may comprise two, three or more different polymers A as described above.

[0093] The molecular weight (Mw) of Polymer A is preferably between 1000 and 250 000, more preferably between 25 000 and 250 000. When the Mw is too low, the physical strength and durability of the porous layer may become insufficient. When the Mw is too high, the viscosity of the dope solution may become too high.

[0094] Examples of poly(sulfones), poly(ether sulfones) and combinations thereof are disclosed in EP-A 3085815, paragraphs

[0021] to

[0032] ,

[0095] The total amount of Polymer A is preferably from 5 to 40 wt%, more preferably from 10 to 30 wt%, most preferably from 15 to 25 wt%, all relative to the total dry weight of the porous polymer layer.Inorganic particles

[0096] The porous polymer layer may further comprise inorganic particles, for example to improve the hydrophilicity and / or the alkali-stability of the porous polymer layer. Such inorganic particles may also be incorporated into the non-porous layer to further optimize its properties.

[0097] Preferred inorganic particles are selected from metal oxides and metal hydroxides.

[0098] Preferred metal oxides are selected from the group consisting of titanium oxide, bismuth oxide, cerium oxide and magnesium oxide.

[0099] Preferred metal hydroxides are selected from the group consisting of zirconium hydroxide, titanium hydroxide, bismuth hydroxide, cerium hydroxide and magnesium hydroxide. A particularly preferred magnesium hydroxide is disclosed in EP-A 3660188, paragraphs

[0040] to

[0063] ,

[0100] Other preferred inorganic particles are sulfates of calcium, barium, lead or strontium, barium sulfate particles being more preferred. Such barium sulfate particles are disclosed in EP-A 3994295.

[0101] Still other inorganic particles that may be used are nitrides and carbides of Group IV elements of the periodic table.

[0102] A combination of one or more different inorganic particles may be used.

[0103] The inorganic particles may be natural substances or synthetic substances.

[0104] The surface of the inorganic particles may be untreated or may be surface treated with for example a silane coupling agent, stearic acid, oleic acid, or a phosphoric acid ester.

[0105] The shape of the inorganic particles is not particularly limited as long as it is in the form of particles and may be any of irregular shapes, spherical shapes, such as true spherical shapes, and oblong spherical shapes, plate shapes, such as flake shapes and hexagonal plate shapes, and fibrous shapes.

[0106] The inorganic particles preferably have a d50 particle size from 0.05 to 2.0 pm, more preferably from 0.1 to 1.5 pm, most preferably from 0.15 to 1.00 pm, particularly preferred from 0.2 to 0.75 pm. The d50 particle size is preferably 0.7 pm or less, more preferably 0.55 pm or less, most preferably 0.40 pm or less.

[0107] The total amount of inorganic particles is preferably from 30 to 95 wt%, more preferably from 50 to 92 wt%, most preferably from 60 to 90 wt%, all relative to the total dry weight of the porous layer including a Polymer A. The amount of inorganic particles is preferably at least 65 wt%, more preferably at least 75 wt%, all relative to the total dry weight of the porous layer including a Polymer A.

[0108] The weight ratio of inorganic particles to polymer in the porous layer including a Polymer A is preferably 60 / 40 or more, more preferably 70 / 30 or more, most preferably 75 / 25 or more.Catalyst layer

[0109] The separator according to the present invention may further include a catalyst layer, preferably provided on the non-porous layer.

[0110] The thickness of the catalyst layer is preferably from 0.5 to 200 pm, more preferably from 1 to 100 pm, most preferably from 5 to 75, particularly preferred from 10 to 50 pm.

[0111] The catalyst is preferably selected from the group consisting of Ni, Ni / NiO, Ni-Fe, Ni- Co, Ni-Mn, Ni-Mo, Fe-Co, Ni-Zn, Ni-AI, Ni-Mo-AI, Ni-Co-AI, Ni-MnAI, Ni-Si, Ni-B or Ni-Si-B. A single catalyst or a combination of catalysts may be used. Preferred catalysts at the cathode side of the separator are selected from the group consisting of Ni, Raney Ni, Ni-Fe, Ni-Co and Ni-Mo. A preferred catalyst at the anode side of the separator is selected from NiO / NiOH and NiO

[0112] The catalyst coated separator may have a catalyst layer on one or both of its surfaces. When a catalyst layer is present on only one surface, the catalyst coated separator is preferably orientated in an electrolytic cell in such a way that the catalyst layer faces the cathode. It has been observed that such an orientation results in a higher increase of the electrolysis efficiency compared to an orientation wherein the catalyst layer faces the anode.Preparation of the separator

[0113] A preferred preparation method of a separator according to the present invention comprises the steps of: providing a porous support (100),- optionally applying a dope solution described below on at least one side of the porous support and performing a phase inversion on the applied dope solution(s) thereby forming one or two porous layer(s) including a Polymer A (200, 200’) on the porous support,- applying a Polymer B solution on at least one side of the porous support and / or on at least one side not in contact with the porous support of the porous layer(s), thereby forming one or two non-porous layer(s) including a Polymer B (300, 300’), characterized in that the Polymer B polymer solution has a viscosity, measured at 20 °C and a shear rate of 100 s'1, of at least 400 mPa.s, preferably at least 500 mPa.s, more preferably at least 750 mPa.s, most preferably at least 1000 mPa.s.

[0114] After the application of the non-porous layer, a drying step is preferably carried out to remove at least partially the solvents of the coating solutions. Drying is preferably carried out at a temperature from 60 to 90 °C during 5 to 20 minutes.

[0115] The method may further include a step of applying one or two catalyst layer(s) (400, 400’) on the non-porous layer(s) of the separator, o catalyst layers (400, 400’).

[0116] The separator according to the present invention may also be prepared starting from a porous separator prepared as described in W02023 / 280600 or WO2023 / 208776, both from AGFA-GEVAERT NV. A Polymer B solution is then applied on one or both sides of such porous separators thereby forming one or two non-porous layers including a Polymer B.Application of the non-porous layer including a Polymer B

[0117] The non-porous layer including a Polymer B is preferably prepared by coating on the porous support (100) or the optional porous layer a Polymer B solution having a viscosity of at least 400 mPa.s, preferably at least 500 mPa.s, mor preferably at least 800 mPa.s, most preferably at least 1000 mPa.s, measured at 20 °C and a shear rate of 100 s’1.

[0118] Any coating technique may be used to apply the Polymer B solution. Preferred coating techniques are selected from the groups consisting of slot-die coating, curtain coating, blade coating, bar coating, air knife coating, cascade coating, extrusion coating, reverse roll coating, kiss coating and dip coating. Highly preferredcoating techniques are air knife coating, cascade coating, curtain coating, reverse roll coating, slot-die coating and kiss coating.

[0119] For an efficient and cost-effective production process of the separator, the non- porous layer is preferable applied in a single coating step.

[0120] The solvent of the Polymer B solution is dependent on the type of Polymer B. When Polymer B is a hydrophilic polymer, such as PVA, the Polymer B solution is preferably an aqueous solution. The aqueous solution may however include organic water-soluble solvents, such as for example ethanol, isopropanol, DMSO or a mixture thereof. However, most preferably the solvent is water.

[0121] Polymer B is preferably crosslinked. It has been observed that crosslinking improves the lifetime of the non-porous layer in the electrolyser. In case Polymer B is a poly(vinyl alcohol) or an ethylene vinyl alcohol copolymer the crosslinking is preferably carried out with di- or polyfunctional aldehydes, such as glutaraldehyde and benzene-1 ,4-dialdehyde. The aldehyde functional group reacts with the hydroxyl group of the poly(vinyl alcohol) or the ethylene vinyl alcohol copolymer forming an acetal bond. For example, crosslinked polyvinyl alcohol may be obtained through vapor phase crosslinking of polyvinyl alcohol and glutaraldehyde as described by KIM et al. (Journal of Power Sources 524 (2022) 231059). However, the crosslinking compound is preferably added to the Polymer B solution together with a crosslinking catalyst, in case of PVA and glutaraldehyde an acid catalyst, such as H2SO4 or HCI. The mixture is then stirred while crosslinking takes place. When a desired viscosity has been reached, the mixture is then coated on the porous support or porous polymer layer. To avoid a too high increase of the viscosity of the mixture before coating, the crosslinking agent or de acid catalyst may be added to the PVA solution just before coating. Alternatively, a separator coated with crosslinked polyvinyl alcohol may also be obtained by the following synthesis procedure. A crosslinking mixture is prepared by adding polymer B, crosslinker and catalyst in preselected concentrations to a suitable solvent. The crosslinking mixture is homogenized by stirring. The desired viscosity of the crosslinking mixture is obtained by adding viscosity modifiers or by selecting a high enough initial polymer concentration. Next, the crosslinking mixture is immediately coated on the substrate without awaiting crosslinking to take place. The coated substrate is then allowed a certain time for crosslinking to take place before being dried in an oven.

[0122] Other crosslinking compounds such as epoxides and sulfonamides may also be used. Also, a combination of crosslinking compounds may be used.

[0123] After the application of the non-porous layer, a drying step is preferably carried out to remove at least partially the solvents of the coating solutions. Drying is preferably carried out at a temperature from 60 to 90 °C during 5 to 20 minutes.

[0124] In a cost-effective, large scale manufacturing process, the non-porous layer including a Polymer B is preferably applied on at least one side of the porous support and / or the porous layer including Polymer A in a continuous roll-to-roll process.Application of the catalyst layer

[0125] The catalyst may be applied by any application method, for example those disclosed in Bladergroen et al., “Overview of Membrane Electrode Assembly Preparation Methods for Solid Polymer Electrolyte Electrolyzer”, 2012, DOI: 10.5772 / 52947.A well-known application method is the so-called decal method. In this method the catalyst layer is first deposited on a temporary substrate, for example fiberglass reinforced Teflon. In case two catalyst layers are applied, a separator is then sandwiched between two catalyst-coated decals with the catalyst layers facing each other. The catalyst layers are then transferred from the decal to the separator using a hot press followed by the removal of the decals.The catalyst may also be provided directly on the surface of the separator for example by:- electrically assisted catalyst deposition, such as electro deposition, electro spraying and electrophoretic deposition;- application of the catalyst as vapour, such as magnetron sputtering and chemical vapour deposition;- plasma spraying;- dry spraying;- phase invenrions;- coating, such as slot-die coating, curtain coating, blade coating, bar coating, air knife coating, cascade coating, extrusion coating, reverse roll coating, kiss coating and dip coating. Preferred coating techniques are air knife coating, cascade coating, curtain coating, reverse roll coating, slot-die coating and kiss coating.- printing, such a screen printing, gravure printing, inkjet printing, flexographic printing and 3D printing.

[0126] Preferred deposition methods are those that do not damage the non-porous polymer layer.

[0127] The catalyst layer(s) are preferably applied in-line in a manufacturing apparatus to provide an efficient and cost-effective production process.

[0128] When a coating or printing method is used to deposit the catalysator a catalyst composition is respectively coated or printed on a surface of a separator. Such a catalyst composition includes one or more catalyst(s) and may further comprise a binder, a solvent and further ingredients such as surfactants,Application of the porous layer including a Polymer A.

[0129] The optional porous layer including a Polymer A is provided on a porous support by applying a dope solution described below on at least one side of the porous support and performing phase inversion on the applied dope solution(s) thereby forming at least one porous layer including a Polymer A on the porous support.

[0130] The applied dope solution preferably completely impregnates the porous support before performing the phase inversion.

[0131] The methods disclosed in EP-A 1776490 and W02009 / 147084 may be used for applying porous layers on a porous support. Other suitable manufacturing methods that may be used are disclosed in EP-A 3272908, EP-A 3660188 and EP-A 3312306.Dope solution

[0132] The dope solution preferably comprises a Polymer A described above and a solvent. The dope solution may further comprise inorganic particles described above.

[0133] The solvent of the dope solution is preferably an organic solvent wherein Polymer A may be dissolved. Moreover, the organic solvent is preferably miscible in water.

[0134] The solvent is preferably selected from N-methyl-pyrrolidone (NMP), N-ethyl-pyrrolidone (NEP), N-butyl-pyrrolidone (NBP), N,N-dimethylformamide (DMF), formamide, dimethylsulfoxide (DMSO), N,N-dimethylacetamide (DMAC), acetonitrile, and mixtures thereof. A highly preferred solvent, for health and safety reasons, is N-butyl-pyrrolidone (NBP).

[0135] The dope solution may further comprise other ingredients to optimize the properties of the obtained porous layers, for example their porosity and the maximum pore diameter at their outer surface.

[0136] The dope solution preferably comprises an additive to optimize the pore size at the surface and inside of the porous layer. Such additives may be organic or inorganic compounds, or a combination thereof. Organic compounds which may influence the pore formation in the porous layers include polyethylene glycol, polyethylene oxide, polypropylene glycol, ethylene glycol, tripropylene glycol, glycerol, polyhydric alcohols, dibutyl phthalate (DBP), diethyl phthalate (DEP), diundecyl phthalate (DUP), isononanoic acid or neodecanoic acid, polyvinylpyrrolidone, polyvinyl-alcohol, polyvinylacetate, polyethyleneimine, polyacrylic acid, methylcellulose and dextran. Preferred organic compounds which may influence the pore formation in the porous layers are selected from polyethylene glycol, polyethylene oxide and polyvinyl pyrrolidone. A preferred polyethylene glycol has a molecular weight of from 10 000 to 50 000, a preferred polyethylene oxide has a molecular weight of from 50 000 to 300 000, and a preferred polyvinylpyrrolidone has a molecular weight of from 30 000 to 1 000 000. A particularly preferred organic compound which may influence the pore formation in the porous layers is glycerol. The amount of compounds which may influence the pore formation is preferably between 0.1 and 15 wt%, more preferably between 0.5 and 5 wt% relative to the total weight of the dope solution. Inorganic compounds which may influence the pore formation include calcium chloride, magnesium chloride, lithium chloride and barium sulfate.A combination of two or more additives that influence the pore formation may be used.

[0137] The dope solutions provided on either side of the porous support may be the same or different.Applying the dope solution

[0138] The dope solution may be applied on the surface of a porous support by any coating or casting technique.

[0139] A preferred coating technique is extrusion coating. In a highly preferred embodiment, the dope solutions are applied by a slot die coating technique wherein two slot coating dies are located on either side of a porous support.The slot coating dies are capable of holding the dope solution at a predetermined temperature, distributing the dope solutions uniformly over the support, and adjusting the coating thickness of the applied dope solutions.

[0140] The viscosity of the dope solutions measured at a shear rate of 100 s1and a temperature of 20 °C is preferably at least 7.5 Pa.s, more preferably at least 15 Pa.s, most preferably at least 30 Pa.s. The dope solutions are preferably shearthinning. The ratio of the viscosity at a shear rate of 1 s1to the viscosity at a shear rate of 100 s1is preferably at least 2, more preferably at least 2.5, most preferably at least 5.

[0141] Immediately after their application, the porous support becomes impregnated with the dope solutions. Preferably, the porous support becomes fully impregnated with the applied dope solutions.Phase inversion step

[0142] After applying the dope solution onto a porous support, the applied dope solution is subjected to phase inversion. In the phase inversion step, the applied dope solution is transformed into a porous layer.

[0143] In a preferred embodiment, both dope solutions applied on a porous support are subjected to phase inversion.

[0144] Any phase inversion mechanism may be used to prepare the porous hydrophilic layers from the applied dope solutions.

[0145] The phase inversion step preferably includes a so-called Liquid Induced Phase Separation (LIPS) step, a Vapour Induced Phase Separation (VIPS) step or a combination of a VIPS and a LIPS step. The phase inversion step preferably includes both a VIPS and a LIPS step.

[0146] Both LIPS and VIPS are non-solvent induced phase-inversion processes.

[0147] In a LIPS step the porous support provided with the dope solution(s) is contacted with a non-solvent that is miscible with the solvent of the dope solution.

[0148] Typically, this is carried out by immersing the porous support provided with the dope solution(s) into a non-solvent bath, also referred to as coagulation bath.

[0149] The non-solvent is preferably water; mixtures of water and an aprotic solvent selected from the group consisting of N-methylpyrrolidone (NMP), N-ethyl- pyrrolidone (NEP), N-butylpyrrolidone (NBP), dimethylformamide (DMF), dimethylsulfoxide (DMSO) and dimethylacetamide (DMAC); water solutions of water-soluble polymers such as PVP or PVA; or mixtures of water and alcohols, such as ethanol, propanol or isopropanol. The non-solvent is most preferably water. However, when using a water-soluble, hydrophilic Polymer A, the non-solvent is preferably an organic solvent.

[0150] The temperature of the coagulation bath is preferably between 20 and 90°C, more preferably between 40 and 70°C.

[0151] The transfer of solvent from the coated Polymer A layer towards the non-solvent bath and of non-solvent into the Polymer A layer leads to phase inversion and the formation of a three-dimensional porous polymer network. The impregnation of the applied dope solution into the porous support results in a sufficient adhesion of the obtained hydrophilic layers onto the porous support.

[0152] In a VIPS step, the porous support coated with the dope solutions is exposed to non-solvent vapour, preferably humid air.

[0153] Preferably, the coagulation step included both a VIPS and a LIPS step. Preferably the VIPS step is carried out before the LIPS step. In a particular preferred embodiment, the porous support coated with the dope solutions is first exposed to humid air (VIPS step) prior to immersion in a water bath (LIPS step).

[0154] After the phase inversion step, preferably the LIPS step in the coagulation bath, a washing step may be carried out.

[0155] After the phase inversion step, or the optional washing step, a drying step may be carried out.

[0156] A preferred method to prepare porous layers including a Polymer A on a porous support is disclosed in EP-A 3933069 (AGFA-GEVAERT NV), paragraphs 117 to 129 and Figures 2 and 3.Electrolytic cell

[0157] The separator for alkaline water electrolysis according to the present invention may be used in an alkaline water electrolyser.

[0158] Such an electrolyser includes at least one electrolytic cell comprising two electrodes, an anode (A) and a cathode (C), separated by a separator. An electrolyte is present between both electrodes. An embodiment of such an electrolytic cell is schematically represented in Figure 3.

[0159] When electrical current is supplied to the electrolysis cell, hydroxyl ions of the electrolyte are oxidized into oxygen at the anode and water is reduced to hydrogen at the cathode. The hydroxyl ions formed at the cathode migrate through the separator to the anode. The separator prevents mixing of the hydrogen and oxygen gases formed during electrolysis.

[0160] An electrolyte solution is typically an alkaline solution. Preferred electrolyte solutions are aqueous solutions of electrolytes selected from sodium hydroxide or potassium hydroxide. Potassium hydroxide electrolytes are often preferred due to their higher specific conductivity. The concentration of the electrolyte in the electrolyte solution is preferably from 20 to 40 wt %, relative to the total weight of the electrolyte solution.

[0161] The temperature of the electrolyte is preferably from 50°C to 120°C, more preferably from 75°C to 100°C, most preferably from 80 to 90 °C. However, a higher temperature, for example at least 100°C, more preferably from 125 to 165°C may result in a more efficient electrolysis.

[0162] An electrode typically includes a substrate (500, 500’) provided with a catalyst layer (600, 600’). The catalyst layer may be different for the anode, where oxygen is formed, and the cathode, where hydrogen is formed.

[0163] Typical substrates are made from electrically conductive materials selected from the group consisting of nickel, iron, soft steels, stainless steels, vanadium, molybdenum, copper, silver, manganese, platinum group elements, graphite, and chromium. The substrates may be made from an electrically conductive alloy of two or more metals or a mixture of two or more electrically conductive materials. A preferred material isnickel or nickel-based alloys. Nickel has a good stability in strong alkaline solutions, has a good conductivity and is relatively cheap.

[0164] A catalyst layer preferably includes nickel, cobalt, iron, and platinum group elements. The catalyst layer may include these elements as elemental metals, compounds (e.g. oxides), composite oxides or alloys made of multiple metal elements, or mixtures thereof. Preferred catalyst layers include plated nickel, plated alloys of nickel and cobalt or nickel and iron, complex oxides including nickel and cobalt such as LaNiOs, LaCoOs, and NiC02CM, compounds of platinum group elements such as iridium oxide, or carbon materials such as graphene.

[0165] A particularly preferred catalyst layer comprises Raney Nickel. The Raney nickel structure is formed by selectively leaching aluminium or zinc from a Ni-AI or Ni-Zn alloy. Lattice vacancies formed during leaching result in a large surface area and a high density of lattice defects, which are active sites for the electro-catalytic reaction to take place.

[0166] The catalyst layer may also include organic substances such as polymers to improve the durability and the adhesion towards the substrate.

[0167] In a so-called zero gap electrolytic cell the electrodes are placed directly in contact with the separator thereby reducing the space between both electrodes. Mesh-type or porous electrodes are used to enable the separator to be filled with electrolyte and for efficient removal of the oxygen and hydrogen gases formed. Preferred porous electrodes and methods to prepare them are disclosed in for example EP-A 3575442, paragraphs 23 to 84. The pore size of porous electrodes may have an influence on the electrolysis efficiency. For example, in EP-A 3575442 it is disclosed that preferred pore sizes of the porous electrodes are from 10 nm up to 200 nm.

[0168] It has been observed that such zero gap electrolytic cells operate at higher current densities.

[0169] However, in such a zero-gap electrolytic cell it has been observed in WO2023 / 118088 (AGFA-GEVAERT NV) that gas bubbles formed inside the separator may accumulate at the top of the separator. Such accumulation of gas bubbles at the top of the separator may result in a higher ionic resistance in that part of the cell. A temperature rise as a result of less efficient cooling by the electrolyte in that area of the electrolysis cell may even result in burning of the separator. Introducing a small distance between one side of the separator and at least one electrode may result in less accumulation of gas bubbles inside the separator. The distance between one side of the separator and the anode (d1) and the distance between the other side of the separator and the cathode (d2) may be the same ordifferent. The distance between a surface of the separator and at least one electrode is preferably from 50 up to 500 pm, more preferably from 100 up to 250 pm.

[0170] Barros et al. (International Journal of Hydrogen Energy, Vol. 49, Part C, Pages 886- 896) observed that a small distance between the separator surface and the electrode including the catalyst layer may decrease the supersaturation of gasses dissolved in the electrolyte at the separator surface. A high supersaturation at the separator surface may result in a higher gas diffusion through the separator. For example, a high supersaturation of hydrogen in the electrolyte at the surface of the separator facing the cathode may result in a higher HTO. A small distance d2 between the cathode and the separator surface facing the cathode may decrease the supersaturation of hydrogen at the separator surface and therefore decrease the HTO. An optimal distance d2 was found to be around 100 pm.

[0171] A so-called spacer may be used to realize the distance between the separator and the electrode. Such a spacer is preferably hydrophilic to avoid adhesion of gas bubbles to the spacer (static water contact angle is 90 °C or lower, preferably 45 °C or lower). Such a spacer preferably has an open structure to ensure ionic conductivity and efficient evacuation of gas bubbles.

[0172] When using a separator according to the present invention in an electrolytic cell, the distance d2 between the porous surface of the separator (surface of the porous support and / or the surface of the porous layer including a Polymer A) and the electrode may be established by the non-porous layer.

[0173] A typical alkaline water electrolyser includes several electrolytic cells, also referred to stack of electrolytic cells. Regarding the cell configuration, two types of electrolysers are typically used.A unipolar (or “tank- type”) electrolyser consists of alternate positive and negative electrodes held apart by a separator. Positive electrodes are all coupled together in parallel, as are the negative electrodes, and the whole assembly is immersed in a single electrolyte bath (“tank”) to form a unit cell. A plant-scale electrolyser is then built up by connecting these units electrically in parallel. The total voltage applied to the whole electrolysis cell is the same as that applied to the individual unit cells. On the other hand, in a bipolar electrolyser a metal sheet (or “bipole”) connects electrically adjacent cells in series. The electrocatalyst for the negative electrode is coated on one face of the bipole and that for the positive electrode of the adjacent cell is coated on the reverse face. In this case, the total cell voltage is the sum of the individual unit cell voltages. Therefore, a series-connected stack of such cells forms a module that operates at a higher voltage and lower current than the tank-type(unipolar) design. To meet the requirements of a large electrolysis plant, these modules are connected in parallel so as to increase the current.

[0174] As described above, the catalyst may also be provided on one or both surfaces of the separator, resulting in a so-called catalyst coated separator. Such a catalyst coated separator may result in a higher electrolysis efficiency due to a better contact between the separator surface and the catalyst.

[0175] In case a catalyst is provided on only one side of the separator, a catalyst may be applied on the electrode facing the other side of the separator.

[0176] When a catalyst is provided on only side of the separator, it has been observed that the highest gain in electrolysis efficiency is obtained when the side of the separator comprising the catalyst on its surface faces the cathode of the electrolysis cell.EXAMPLESMeasurementsViscosity

[0177] The viscosity of the alkali-stable polymer solutions was measured on a Malvern Kinexus LAB+ Rheometer at 20 °C. Shear rates were varied from 0.1 to 100 s1.Bubble Point, Minimal Pore Size, Mean Pore Size, Gas Permeability

[0178] The pore diameters of the separators were measured using the so-called Bubble Point Test method.

[0179] The Bubble Point Test Method entails wetting of the pores of a membrane with a wetting liquid and consequently measuring the lowest pressure that is required to overcome the surface tension forces between the wetting liquid and the pore wall in a fully wetted pore. This pressure is reffered to as the bubble point pressure.

[0180] The theory of capillarity states that the height of a water column in a capillary is indirectly proportional to the capillary diameter. By using the Young-Laplace equation, the pore diameter of the membrane can be linked to the applied pressure required to force the wetting liquid out of the pore.

[0181] The procedure for the bubble point test method is described in American Society for Testing and Materials Standard (ASMT) Method F316.

[0182] The top of the filter is placed in contact with the liquid, the bottom with air, the filter holder is connected to a source of a regulated pressure. The air pressure is gradually increased and the formation of bubbles on the liquid side is noted. Atpressures below the bubble point, gas passes across the filter only by diffusion, but when the pressure is high enough to dislodge liquid from the pores, bulk flow begins and bubbles will be seen.The initial bubble test pressure determines the size (and location) of the largest hole, the open bubble point pressure determines the mean pore size of the element.

[0183] The Bubble point, the average pore diameter, the maximum pore diameter and the gas permeability of the membranes were measured using a POROLUX 1000, commercially available from POROMETER.Non-porous layer thickness

[0184] The thickness of the non-porous layer including a Polymer A was measured by analysis of SEM images of separator cross-sections. The layer thickness was determined by performing several thickness measurements over the width of the separator with image analysis software (e.g. Image J).Crack resistanceThe separator crack resistance was evaluated as follows: the separator in both wet and dry condition was folded along direction of producing (MD) and perpendicular to direction of producing (CD) and an iron wheel with a weight of 2 kg was rolled over the fold 4 times. Next, the fold was inspected and assigned a value ranging from:- 0 = no cracks,1 = only cracks at the edges of the separator fold,- 2 = cracks at 50% of the folded separator area,- 3 = cracks at almost the entire width of the fold,- 4 = cracks at the entire width of the fold.Scanning Electron Microscopy (SEM) and Energy-dispersive X-ray spectroscopy (SEM-EDX)

[0185] SEM cross-sections were prepared by cutting the sample and embedding it in epoxy resin. Afterwards, the sample was mechanically polished and coated with a thin Pt-Pd layer. Surface samples were cut and applied to an aluminum stub with double-sided tape and coated with a thin Pt-Pd layer.Contact Angle

[0186] Contact angles were measured using the Owens- Wenth model based on average static contact angles of reference liquids (water and diiodo methane). Drops of about 2-3 pm were deposited on the substrates. The contact angle was registered for 10seconds. For further analysis, the average contact angle between 0 and 10 seconds were used. For each combination, 9 drops were analyzed.Materials

[0187] All materials used in the following examples were readily available from standard sources such as ALDRICH CHEMICAL Co. (Belgium) and ACROS (Belgium) unless otherwise specified. The water used was deionized water.

[0188] ZIRFON-1 is Zirfon Perl UTP500 from AGFA-GEVAERT NV.

[0189] ZIRFON-2 is Zirfon Perl UTP220 from AGFA-GEVAERT NV.

[0190] PVA-1 is a high molecular weight polyvinyl alcohol with a molecular weight of 85 - 124 kDa and degree of hydrolysis > 99 % from ALDRICH.

[0191] PVA-2 is a low molecular weight polyvinyl alcohol available as POVAL 4-88 from KURARAY.

[0192] EVA-5 is a poly(ethylene-co-vinyl alcohol) available as EXCEVAL AQ-4104 from KURARAY.

[0193] EVA-29 is a poly(ethylene-co-vinyl alcohol) available as SOARNOL D2908 from KURARAY.

[0194] Glutardehyde available from ALDRICH as a 25 wt% aqueous solution.

[0195] NiO is nickeloxide (99 % purity) available from BCR GMBH & CO.

[0196] PVP is polyvinylpyrolidone having a MW of 8000 available from BCR GMBH & CO.

[0197] NiO dispersion was prepared by mixing by weight: 60% NiO, 7.5% PVP and 32.5% demineralized water. This mixture was then grinded on an agitated bead mill until the Z-average particle size was smaller than 200 nm.Example 1Preparation of the separators S-1 to S-6

[0198] The separators S-1 to S-6 were prepared by coating an aqueous PVA-1 solution according to Table 2 on one side of ZIRFON-1 followed by drying at 80 °C for 15 minutes in a standard convection oven. The viscosity of the PVA-1 solution, measured as described above, was varied as shown in Table 2.Table 2

[0199] The gas permeability, bubble point and PVA-layer thickness of S-1 to S-6 determined as described above, are shown in Table 3 together with the bubble point and gas permeability of ZIRFON-1 without a PVA top-layer.Table 3*++ = homogeneous coating covering entire coating area, +- = heterogeneous coating with spots of poor and good coating quality, - = poor coating quality over entire coating area

[0200] It is clear from the results shown in Table 3 that separators with good, homogenous coating quality and a bubble point (measured according to ASTM F316) of at least 5 bar were obtained when the viscosity of the PVA solutions was at least 400 mPa.s.

[0201] The effect of coating ZIRFON-1 with a PVA-1 solution on the separator surface roughness is demonstrated in Figure 5. A SEM top-view of a surface of ZIRFON-1 not comprising a PVA-1 layer (Fig.5. a) and of S-1 comprising a PVA-1 layer (Fig.5.b) clearly illustrates that a smoother separator surface is observed for S-1 .Example 2Preparation of the separators S-7 to S-13

[0202] The separators S-7 to S-13 were prepared by coating an aqueous PVA-2 solution according to Table 4 on one side of a ZIRFON-1 separator followed by drying at 80 °C for 15 min in a standard convection oven.Table 4

[0203] The gas permeability, bubble point and top layer thickness of S-7 to S-13 and of ZIRFON-1 without a PVA top-layer, determined as described above, are shown in Table 5.Table 5

[0204] It is clear from the results shown in Table 5 that separators with a bubble point (measured according to ASTM F316) of at least 5 bar were obtained when the viscosity of the PVA solutions was at least 400 mPa.s.Example 3Preparation of the separators S-14 and S-15

[0205] The separator S-14 was prepared by bar coating an aqueous 22 wt% PVA-2 solution on one side of a ZIRFON-2 separator with a wet coating thickness of 200 pm. Next, the coated separator was dried in an oven at 80 °C for 15 min. The gas permeability was measured to be 0.03 L / min.cm2and the bubble point was > 8 bar.

[0206] The separator S-15 was prepared by bar coating an aqueous 10 wt% PVA-1 solution on both sides of a ZIRFON-2 separator with a wet coating thickness of 100 pm. First, one side of the ZIRFON-2 separator was coated with the PVA-1 solution and dried in an oven at 80 °C. Next, the other side of the separator was coated with the PVA-1 solution and the resulting separator dried in an oven at 80 °C. The gas permeability was measured to be 0.01 L / min.cm2and the bubble point was > 8 bar.Example 4Preparation of the separators S-16 and S-17

[0207] To prevent dissolution of the non-porous layer in water or in a concentrated solution of KOH in water, a PVA layer was crosslinked with glutaraldehyde. A crosslinking mixture was prepared by adding to 10 g of a solution of 5 wt% PVA-1 in water 0.114 g of glutaraldehyde. Next, 1 mL solution of 1 M H2SO4 in water was added to the mixture as a crosslinking catalyst. The mixture was then stirred until the viscosity was > 400 mPa.s, afterwhich the crosslinking mixture was bar coated with a wet coating thickness of 200 pm on a ZIRFON-1 and ZIRFON-2 separator and dried in an oven at 80 °C for 15 min (separator S-16 and S-17, respectively).

[0208] The separator S-16 demonstrated a gas permeability of 0.03 L / min.cm2and a bubble point of > 8 bar.

[0209] The separator S-17 demonstrated a gas permeability of 0.05 L / min.cm2and a bubble point of > 8 bar.Example 5Preparation of the separators S-18 and S-19

[0210] Separator S-18 was prepared by coating the NiO dispersion on one side of a ZIRFON- 1 separator.

[0211] Separator S-19 was prepared by first coating a PVA-1 solution on one side of a ZIRFON-1 separator followed by drying in an oven at 80 °C, forming a dry PVA layer. Next, a NiO dispersion was coated on the dried PVA layer.

[0212] A SEM cross-section of S-18 and S-19 is shown in respectively Fig. 4. a. and Fig.4.b.

[0213] From these SEM cross-sections can be derived that the thickness of the NiO catalyst layer of S-18 and S-19 and of the PVA layer of S-19 is respectively 3-4 pm and 7-8 pm.

[0214] Whether or not NiO penetrated into the pores of the ZIRFON-1 separator was investigated using SEM-EDX. SEM-EDX analysis of the cross-sections of the separators S-18 and S-19 revealed that for S-18, Ni could be detected 20-30 pm beneath the ZIRFON-1 Surface, while for S-19, no Ni could be detected at or below the ZIRFON-1 Surface. This clearly illustrates that the presence of the non-porous alkali-stable polymer layer between the catalyst layer and the surface of the porous separator prevents penetration of the catalysator into the pores of the porous separator.Example 6

[0215] Separator S-16 (see example 4 above) was compared to pristine ZIRFON-1 in terms of crack resistance. From Table 6, it can be derived that applying a PVA layer on top of the ZIRFON-1 improves the crack resistance of the membrane.Table 6Preparation of the separator S-20 to S-24

[0216] The separators S-20 to S-24 were prepared by coating an aqueous EVA-5 solution according to Table 7 on one side of ZIRFON-1 followed by drying at 80 °C for 15 min in a standard convection oven. The viscosity of the EVA-5 solution, measured as described above, was varied as shown in Table 7.Table 7

[0217] The gas permeability, bubble point and EVA-5 layer thickness of S-20 to S-24 determined as described above are shown in Table 8 together with the bubble point and gas permeability of ZIRFON-1 without an EVA-5 top-layer.Table 8coating with spots of poor and good coating quality, - = poor coating quality over entire coating area

[0218] It is clear from the results shown in Table 8 that separators with good, homogenous coating quality and a bubble point (measured according to ASTM F316) of at least 5 bar were obtained when the viscosity of the EVA-5 solutions was at least 400 mPa.s.Example 8Preparation of the separator S-25 to S-27

[0219] The separators S-25 to S-27 were prepared by coating an aqueous EVA-29 solution according to Table 9 on one side of ZIRFON-1 followed by drying at 80 °C for 15 min in a standard convection oven. The viscosity of the EVA-29 solution, measured as described above, was varied as shown in Table 9.Table 9

[0220] The gas permeability, bubble point and EVA-29 layer thickness of S-25 to S-27 determined as described above, are shown in Table 10 together with the bubble point and gas permeability of ZIRFON-1 without an EVA-29 top-layer.Table 10

[0221] It is clear from the results shown in Table 10 that separators with good, homogenous coating quality and a bubble point (measured according to ASTM F316) of at least 5 bar were obtained when the viscosity of the EVA-29 solutions was at least 400 mPa.s.Example 9Preparation of the separators S-28

[0222] To prevent dissolution of the non-porous layer in water or in a concentrated solution of KOH in water, a EVA-5 layer was crosslinked with glutaraldehyde. A crosslinking mixture was prepared by adding to 50 g of a solution of 17 wt% EVA-5 in a water / IPA mixture 8.5 g of glutaraldehyde. Next, 1 mL solution of 1 M H2SO4 in water was added to the mixture as a crosslinking catalyst. The mixture was then stirred until the viscosity was > 400 mPa.s, afterwhich the crosslinking mixture was bar coated with a wet coating thickness of 200 pm on a ZIRFON-1 separator and dried in an oven at 80 °C for 15 min (separator S-29).The separator S-28 demonstrated a gas permeability of 0.00 L / min.cm2and a bubble point of > 8 bar.

Claims

Claims1 . A separator for alkaline water electrolysis comprising;- a porous support (100) and on at least one side of the support, in order:- an optional porous layer (200) including a polymer A, and- a non-porous layer including a polymer B (300), characterized in that the separator is obtainable by coating on the porous support (100) or the optional porous layer (200) a polymer B solution having a viscosity of at least 400 mPa.s, measured at 20 °C and a shear rate of 100 s'1, and wherein the separator has a bubble point, measured according to ASTM F316, of at least 5 bar.

2. The separator for alkaline water electrolysis according to claim 1 wherein Polymer B is selected from the group consisting of a polyethylene glycol) or copolymers thereof, a poly(saccharide), a poly(ethylene-co-vinyl alcohol), a poly(ethylene-co-vinyl amine), poly(vinyl butyral), poly(vinyl acetal), polybenzimidazole and a poly(vinyl alcohol).

3. The separator for alkaline water electrolysis according to claim 1 or 2 wherein Polymer B is a poly(vinyl alcohol) or a poly(ethylene-co-vinyl alcohol).

4. The separator for alkaline water electrolysis according to any of the preceding claims wherein Polymer B has a Molecular Weight from 15 to 150 kDa.

5. The separator for alkaline water electrolysis according to any of the preceding claims wherein the non-porous layer is crosslinked.

6. The separator for alkaline water electrolysis according to any of the preceding claims wherein the thickness of the non-porous layer is from 0.1 to 25 pm.

7. The separator for alkaline water electrolysis according to any of the preceding claims wherein the total thickness of the separator is from 50 to 750 pm.

8. The separator for alkaline water electrolysis according to any of the preceding claims wherein Polymer A is selected from the group consisting of poly(sulfone), poly(ether sulfone), poly(phenylene sulfide), poly(ether ether ketone) and poly(phenyl sulfone).

9. The separator for alkaline water electrolysis according to any of the preceding claims further comprising a catalyst layer (400) provided on the non-porous layer.

10. The separator for alkaline water electrolysis according to claim 9 wherein the catalyst is selected from the group consisting of Ni, NiO, Raney Ni, Ni-Fe, Ni-Co, Ni-Mo and NiO / NiOH.11 . A method of preparing a separator for alkaline water electrolysis as defined in any of the preceding claims comprising the steps of:- providing a porous support (100),- optionally applying a dope solution including a Polymer A on the porous support and performing a phase inversion step on the applied dope solution thereby forming a porous layer including a Polymer A (200) on the porous support, and- coating on the porous support (100) or the optional porous layer (200) a Polymer B solution thereby forming a non-porous layer (300), characterized in that the viscosity of the Polymer B solution is at least 400 mPa.s, measured at 20 °C and a shear rate of 100 s’1.

12. The method according to claim 11 wherein the Polymer B solution is applied by a single coating step.

13. The method according to claim 11 or 12 further comprising the step of applying a catalyst composition on a non-porous layer thereby obtaining a catalyst layer (400).

14. An electrolytic cell for alkaline water electrolysis comprising an anode, a cathode and a separator as defined in any of the claims 1 to 10 positioned between the anode and the cathode.

15. Use of a separator for alkaline water electrolysis as defined in any of the claims 1 to 10 in the production process of green hydrogen, green ammonia or green steel.

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