Patent Application
20230268520
The present application relates to an acid-base polymer blend membrane, a cell membrane comprising the acid-base polymer blend membrane, the use thereof, and a device comprising the cell membrane.
Different approaches and scenarios are being pursued to meet the global energy demand, which will grow even more in the future with the introduction of e-mobility. A great potential is attributed to renewable energy sources, such as wind and solar energy. However, a major disadvantage of non-fossil energy sources is that they are only available temporarily, and energy storage systems which can temporarily store the excess energy and release it as requested, are needed. This surplus energy can be stored in large reservoirs, for example, but this requires a lot of space. Another way to store energy is to convert the available energy into electrical energy, which is then stored in accumulators or batteries. Today’s Li-ion based batteries offer an excellent ratio of power or capacity to space requirements. However, the extraction of lithium as a raw material brings about a lot of disadvantages, which - among other things - cannot be reconciled with sustainability and environmental protection.
Another possibility to store the gained energy efficiently and in a space-saving manner is the use of redox-flow batteries. This is a type of accumulator in which the electrical energy is stored in chemical compounds. These chemical compounds are present as reaction partners in a solvent in dissolved form and circulate as electrolytes in two separate circuits, between which the ion exchange takes place through a membrane. The dissolved substances are chemically reduced or oxidized, releasing or storing electrical energy. The redox flow battery is a form of galvanic cell in which a conversion of chemical into electrical energy can take place in a reversible process. Since the two electrolytes are stored in two separate tanks, the amount of stored energy does not depend on the cell size, but only on the size of the electrolyte tanks.
Among the redox-flow batteries in use today, two types of technical designs can be distinguished in particular, which differ in the chemistry of the electrolytes or redox pairs used. On the one hand, there are redox-flow batteries with metal-based electrolytes, such as electrolytes based on iron and, in particular, vanadium in different oxidation states. On the other hand, also compounds based on organic substances such as lignin, lignin-based (e.g., quinone) or lignin sulfonate solutions are used. While the vanadium-based electrolytes are potentially harmful to health and environment due to their heavy metal toxicity, the organic based electrolytes are a promising alternative since the materials required for electrolyte production may be taken from renewable raw materials, and they are - in principle - available in unlimited quantities.
A core component of the redox flow battery is the cell membrane. The main tasks of the cell membrane are the separation of the two positively and negatively charged electrolytes and the selective conduction of cations through the membrane, which is necessary for the conduction of electrons via the external circuit. In addition to good electrochemical properties, such as high ionic conductivity and low electrical resistance, the cell membrane should have excellent mechanical and chemical stability, as well as low water absorption and swelling behaviour. Furthermore, the cell membrane should have good processing properties, such as handling and connectivity with other materials by welding or bonding. Finally, the redox flow batteries with the above mentioned membranes should show a high cycle stability, high energy efficiency, and high Coulomb efficiency of the whole system.
Cell membranes for, e.g., fuel cells, PEM electrolysis and redox flow batteries (RFBs) have therefore been, and are still being, wildly explored.
Membranes for fuel cells, PEM electrolysis and redox flow batteries comprising halogen containing polymers, in particular polymers containing fluorine, are currently widely used. However, similar as with vanadium based electrolytes, also halogen containing compounds are considered potentially harmful to the environment.
Thus, there is still a need for halogen-free ion exchange membranes which are more cost-effective and environmentally friendly. There is still a need for ion exchange membranes characterized by lower electrical resistance and thus higher ion conductivity, in particular in strongly basic electrolytes, such as lignin-based electrolytes, or also strongly acidic electrolytes. There is still a need for lower electrolyte crossover during charging or discharging in batteries, such redox flow batteries (RFBs). There is still a need for high discharging capacity in battery cells. There is still a need for good processability through welding or gluing, in particular in combination with a substrate made from the same raw material as the components to be welded.
It is one object of the present disclosure to provide a halogen-free ion exchange membrane having a low electrical resistance, in particular in strongly basic electrolytes, such as lignin-based electrolytes, or also strongly acidic electrolytes, which may advantageously be used in different applications, including RFBs.
In a first aspect, the present disclosure provides an acid-base polymer blend membrane comprising at least one first polymer exhibiting acidic groups (A) and at least one second polymer exhibiting basic groups (B), wherein the molar ratio of acidic groups A / basic groups B in the acid-base polymer blend membrane is at least 1 / 0.25.
In a second aspect, the present disclosure provides a cell membrane comprising a support structure and an acid-base polymer blend membrane according to the first aspect, wherein the acid-base polymer blend membrane is impregnated on the support structure.
In a third aspect, the present disclosure provides a use of the acid-base polymer blend membrane according to the first aspect, or of the cell membrane according to the second aspect in an electrodialysis cell, in a fuel cell, in a PEM electrolyzer, or in a redox flow battery, preferably in a redox flow battery.
In a fourth aspect, the present disclosure provides a device comprising an acid-base polymer blend membrane according to the first aspect, or a cell membrane according to the second aspect, wherein the device is an electrodialysis cell, a fuel cell, a PEM electrolyzer, or a redox flow battery, preferably a redox flow battery.
The present invention will be described with respect to particular embodiments and with reference to certain examples, but the invention is not limited thereto, and it is only defined by the appending claims.
In a first aspect, the present disclosure relates to an acid-base polymer blend membrane comprising at least one first polymer exhibiting acidic groups (A) and at least one second polymer exhibiting basic groups (B), wherein the molar ratio of acidic groups A / basic groups B in the acid-base polymer blend membrane is at least 1 / 0.25.
The inventors of the present disclosure have surprisingly found that a high molar ratio of acidic groups to basic groups in the acid-base polymer blend membrane of the present disclosure show good electrical properties, with low electrical resistance and high ion conductivity.
In a preferred embodiment of the first aspect, an acid-base polymer blend membrane is provided, wherein the acidic group of the first polymer is selected from the group consisting of —SO3H, —PO3H, —PO3H2, —COOH, —AsO3H, —SeO3H and/or —C6H4OH, preferably wherein the acidic group is —SO3H.
In a preferred embodiment of the first aspect, an acid-base polymer blend membrane is provided, wherein the basic group of the second polymer is selected from the group consisting of pyridine, triazole, benzotriazole, pyrazol, benzpyrazol, imidazole, and benzimidazole, preferably wherein the basic group is imidazole or benzimidazole, further preferably benzimidazole.
In a preferred embodiment of the first aspect, an acid-base polymer blend membrane is provided, wherein the at least one first polymer is selected from the group consisting of sulfonated poly(arylene ether sulfone) (sPAES), sulfonated poly(ether ether ketone) (sPEEK), and sulfonated poly (ether ketone) (sPEK), preferably wherein the at least one first polymer is selected from the group consisting of sulfonated polyphenylsulfone (sPPSU), sulfonated poly(ether ether ketone) (sPEEK), and sulfonated poly (ether ketone) (sPEK), and further preferably wherein the at least one first polymer is sulfonated poly(ether ether ketone) (sPEEK).
In a preferred embodiment of the first aspect, an acid-base polymer blend membrane is provided, wherein the at least one second polymer is selected from the group consisting of meta-polybenzimidazole (m-PBI), and polybenzimidazole-OO (PBI-OO), and preferably wherein the at least one second polymer is meta-polybenzimidazole (m-PBI).
In a preferred embodiment of the first aspect, an acid-base polymer blend membrane is provided, wherein the molar ratio of acidic groups A / basic groups B in the acid-base polymer blend membrane is at least 1 / 0.24, or at least 1 / 0.23, or at least 1 / 0.22, or at least 1 / 0.21, or at least 1 / 0.20, or at least 1 / 0.19, or at least 1 / 0.18, or at least 1 / 0.17, or at least 1 / 0.16, or at least 1 / 0.15, or at least 1 / 0.14, or at least 1 / 0.13, or at least 1 / 0.12, or at least 1 / 0.11, or at least 1 / 0.10, or at least 1 / 0.09; preferably wherein the molar ratio is at least 1 / 0.21, or at least 1 / 0.20, or at least 1 / 0.15, or at least 1 / 0.14, or at least 1 / 0.10, or at least 1 / 0.09.
In a preferred embodiment of the first aspect, an acid-base polymer blend membrane is provided, wherein the molar ratio of acidic groups A / basic groups B in the acid-base polymer blend membrane is 1 / 0.07 or less, or 1 / 0.08 or less, or 1 / 0.09 or less, or 1 /0.10 or less, or 1 /0.11 or less, or 1 / 0.12 or less, or 1 /0.13 or less, or 1 / 0.14 or less, or 1 / 0.15 or less, or 1 / 0.16 or less, or 1 / 0.17 or less, or 1 / 0.18 or less, or 1 / 0.19 or less, or 1 / 0.20 or less, or 1 / 0.21 or less, or 1 / 0.22 or less, or 1 / 0.23 or less; preferably wherein the molar ratio is 1 / 0.07 or less, or 1 / 0.08 or less, or 1 / 0.12 or less, 1 / 0.13 or less, or 1 / 0.18 or less, or 1 / 0.19 or less.
In a preferred embodiment of the first aspect, an acid-base polymer blend membrane is provided, wherein the molar ratio of acidic groups A / basic groups B in the membrane is in the range of from 1 / 0.25 to 1 / 0.07, or from 1 / 0.20 to 1 / 0.08, or from 1 / 0.20 to 1 / 0.13, or from 1 / 0.20 to 1 / 0.19, or from 1 / 0.14 to 1 / 0.08, or from 1 / 0.14 to 1 / 0.13, or from 1 / 0.09 to 1 / 0.08. In another preferred embodiment, the molar ratio of acidic groups A / basic groups B in the membrane is in the range of from 1 / 0.14 to 1 / 0.04. In another preferred embodiment, the molar ratio of acidic groups A / basic groups B in the membrane is in the range of from 1 / 0.13 to 1 / 0.06. In another preferred embodiment, the molar ratio of acidic groups A / basic groups B in the membrane is in the range of from 1 / 0.12 to 1 / 0.06. In another preferred embodiment, the molar ratio of acidic groups A / basic groups B in the membrane is in the range of from 1 / 0.09 to 1 / 0.06. In another preferred embodiment, the molar ratio of acidic groups A / basic groups B in the membrane is in the range of from 1 / 0.09 to 1 / 0.08. In another preferred embodiment, the molar ratio of acidic groups A / basic groups B in the membrane is in the range of from 1 / 0.07 to 1 / 0.06.
If the molar ratio of acidic groups A / basic groups B exceeds a certain threshold, the membranes exhibit a strong decrease in chemical stability. It is understood that such decrease is caused by extensive swelling of the membranes which results in dramatic loss of membrane performance and membrane selectivity. For instance, this results in the electrolyte of a redox-flow battery being able to cross the membrane thus irreversibly reducing the capacity of the battery by an unwanted reaction of the reactive species of both half cells. Furthermore, the membrane may even decompose completely in acidic or basic media at increased temperatures.
The term membrane water uptake means that the polymer blend membrane increases in weight and expands in the dimensional length upon immersion with a solvent, such as water or aqueous solutions of acid. The membrane water uptake is generally caused by the difference in osmotic pressure inside the membrane and the surrounding solution. In particular, solvent molecules are taken up into the polymer chains which causes a swelling phenomenon and leads to a swollen polymeric membrane. In this case, an expansion of the polymer network is promoted because polymer-polymer interactions are weakened and hydrophilic channels are formed. These hydrophilic channels may promote or even enable the cross-membrane transfer of molecules such as the redox couples of a redox flow battery, thereby resulting in the highly unwanted self-discharge of the battery. Therefore, it is an ultimate prospect to reduce membrane water uptake and therewith its swelling to a minimum.
From the prior art it is known that membranes having a high degree of acidic functional groups generally swell dramatically in hydrated states, leading to a high crossover of polar substances along the large hydrophilic channels.
In the sense of the present disclosure, the membrane water uptake is determined through the formula:
wherein mwet is the weight of a polymer blend membrane in a wet state, mdry is the weight of a polymer blend membrane in the dry state. For the experiments, freshly produced, dry membranes are used. To ensure comparable conditions, the dry weight Mdry is determined after drying the membrane at 80° C. for 3 h in a convection heating cabinet. The membrane weight in the wet state mwet is determined after immersing the membrane for 40 h in deionized water or a 2.5 M aqueous H2SO4 at a temperature of 25° C. or 55° C. In general, a water uptake below 30% is desirable.
The weight of a polymer blend membrane may be determined by a high precision balance.
On the other hand, if the molar ratio of acidic groups A / basic groups B falls below the threshold of 1 / 0.25, the membrane cannot efficiently transfer charges.
In a second aspect, the present disclosure provides a cell membrane comprising a support structure and an acid-base polymer blend membrane according to the first aspect, wherein the acid-base polymer blend membrane is impregnated on the support structure.
In a preferred embodiment of the second aspect, a cell membrane is provided, wherein the support structure is a woven or nonwoven fabric, preferably wherein the fabric comprises a polymer selected from the group consisting of polyethylene (PE), polypropylene (PP), polyamide (PA), polysulfone (PSU), polyether ether ketone (PEEK), polyether ketone (PEK), polyvinylidene fluoride (PVDF), polyethersulfone (PES), polyetherimide (PEI), polybenzimidazole (PBI), polyethylene terephthalate (PET), polyester and polyphenylene oxide (PPO); or wherein the fabric comprises glass fibers, further preferably wherein the fabric comprises a polymer selected from the group consisting of polyethylene (PE), polypropylene (PP), polyamide (PA), polysulfone (PSU), polyether ether ketone (PEEK), polyether ketone (PEK), polyethylene terephthalate (PET), and polyester, or wherein the fabric comprises a polymer selected from the group consisting of polyethylene (PE), polypropylene (PP), and polyester.
In a preferred embodiment of the second aspect, a cell membrane is provided, wherein the support structure, preferably the nonwoven fabric, has a thickness in the range of from 1 to 250 µm, preferably of from 1 to 200 µm, or from 2 to 200 µm, or from 5 to 100 µm, or from 10 to 200 µm, or from 50 to 100 µm, or from 5 to 50 µm, or from 20 to 50 µm, or preferably in the range of from 1 to 60 µm, or from 10 to 50 µm, or from 1 to 25 µm, or from 2 to 20 µm.
In a preferred embodiment of the second aspect, a cell membrane is provided, wherein the support structure is impregnated with the acid-base polymer blend membrane on one side of the support structure, or wherein the entire support structure is impregnated with the acid-base polymer blend membrane.
In a preferred embodiment of the second aspect, a cell membrane is provided, wherein the support structure is impregnated with the acid-base polymer blend membrane, and wherein the impregnated support structure has a thickness in the range of from 1 µm to 400 µm, preferably of from 10 to 100 µm, or from 50 to 100 µm, or from 20 to 50 µm.
In a third aspect, the present disclosure provides a use of the acid-base polymer blend membrane according to the first aspect, or of the cell membrane according to the second aspect in an electrodialysis cell, in a fuel cell, in a PEM electrolyzer, or in a redox flow battery, preferably in a redox flow battery.
In a fourth aspect, the present disclosure provides a device comprising an acid-base polymer blend membrane according to the first aspect, or a cell membrane according to the second aspect, wherein the device is an electrodialysis cell, a fuel cell, a PEM electrolyzer, or a redox flow battery, preferably a redox flow battery.
Terms as set forth hereinafter are generally to be understood in their common sense unless indicated otherwise.
Where the term “comprising” is used in the present description and claims, it does not exclude other elements. For the purposes of the present invention, the term “consisting of” is considered to be a preferred embodiment of the term “comprising”. If hereinafter a group is defined to comprise at least a certain number of embodiments, this is also to be understood to disclose a group, which preferably consists only of these embodiments.
Where an indefinite or definite article is used when referring to a singular noun, e.g. “a”, “an” or “the”, this includes a plural of that noun unless specifically stated otherwise.
Terms like “obtainable” and “obtained” are used interchangeably. This, e.g., means that, unless the context clearly dictates otherwise, the term “obtained” does not mean to indicate that e.g. an embodiment must be obtained by e.g. the sequence of steps following the term “obtained” even though such a limited understanding is always included by the terms “obtained” as a preferred embodiment.
The membranes of the present disclosure are mainly or exclusively composed of polymers. These polymers may exhibit acidic or basic functionality.
As used herein, a “basic polymer” or “polymeric base” refers to a polymer with at least one basic group per repeating unit.
As used herein, an “acidic polymer” or “polymeric acid” refers to a polymer with at least one acidic group per repeating unit. In a preferred embodiment, said acidic group A is a sulfone group.
In a sulfonated polymer, the amount of sulfonation is expressed by the term “degree of sulfonation” or “DS”, relating to the degree to which a polymer is sulfonated. The term DS is a preferred embodiment of the generic term “DA” or “degree of acidity”. The term DA is hence exchangeable with DS in case the acidic group of the acidic polymer is a sulfonate group, —SO3H.
The degree of sulfonation is defined relative to the repeating unit of the polymer. For example, acidic polymer A2 (as used in the Examples below) is a sulfonated PEEK polymer (sPEEK) with a repeating unit comprising three phenyl groups. If each repeating unit in said PEEK polymer is sulfonated with one sulfone group, the degree of sulfonation is defined as 100 %. In other words, if the degree of sulfonation is, e.g., 50 %, every second repeating unit is sulfonated. It is understood that also a DS of above 100 % is possible if each repeating unit is, on average, substituted with more than one sulfone group.
Taking acidic polymer A2 with a DS of 60 %, it refers to a mixture of 60% of sulfonated PEEK repeating units and 40% of non-sulfonated PEEK repeating units. The degree of sulfonation cannot be entirely determined by experimental measures to the extent that every sulfonation reaction yields the same DS, despite identical reaction conditions. Rather, performing the same sulfonation reaction of the same starting material, e.g. PEEK, a different DS may be determined. The determination of the degree of sulfonation may be performed by means of GC analysis or 1H NMR spectroscopy, as it is known to the skilled person. The DA, and specifically the DS, thus is determined by analytical means after sulfonation.
In one embodiment, the DA is determined by GC analysis. In another embodiment, the DA is determined by 1H NMR spectroscopy. Methods for the calculation of DA from the signal intensities thus measured are known in the prior art, e.g., in Yee, R.-S.-L.; et al. Membranes, 2013, 3, pp. 182-195.
In one embodiment, the DS is determined by GC analysis. In another embodiment, the DS is determined by 1H NMR spectroscopy. Methods for the calculation of DS from the signal intensities thus measured are known in the prior art, e.g., in Yee, R.-S.-L.; et al. Membranes, 2013, 3, pp. 182-195.
In another embodiment, the DA is calculated from the ion exchange capacity of a membrane. In another embodiment, the DS is calculated from the ion exchange capacity of a membrane. Methods for the calculation of DA and DS from the ion exchange capacity are known in the prior art, e.g., in Yee, R.-S.-L.; et al. Membranes, 2013, 3, pp. 182-195.
The term ion exchange capacity (IEC) represents the total of functional groups responsible for ion exchange in polymer electrolyte membrane. Generally, a conventional acid-base titration method is used to determine the IEC. In one embodiment, the titration is performed with an aqueous solution of NaOH.
Generally, DS and DA are independent from the method of determination.
With the knowledge of DA, or specifically DS, the molar amount of acidic groups (nacidicgroups) in the polymer exhibiting acidic groups used in the acid-base polymer blend may be determined with consideration of the mean molecular weight of the polymer exhibiting acidic groups. And, in an analogous manner, also the amount of basic functionality (nbasicgroups) may be determined for the basic polymer. Both amounts may be used to calculate the A / B molar ratio.
Herein, the term “A / B molar ratio” or “acidic group A / basic group B molar ratio” refers to a calculated molar ratio of acidic groups to basic groups in an ion exchange polymer blend membrane according to the present disclosure. For example, an A / B molar ratio of 1 / 0.2 relates to an acid-base polymer blend membrane, wherein the number of acidic groups are five times higher than the number of basic groups. In the case of A2-B1 with an A / B molar ratio of 1 / 0.2, an acid-base polymer blend membrane is referred to, wherein the number of sulfonate groups are five times higher than the number of benzimidazole moieties. The A / B molar ratio may be generally calculated as follow:
If a polymer exhibits acidic functionality, said functionality may be, e.g., provided by a chemical group selected from the group consisting of —SO3H (sulfonate group), —PO3H (phosphite group), —PO3H2 (phosphonate group), —COOH (carboxyl group), —AsO3H (arsonate group), —SeO3H (selenoic group) and —C6H4OH (phenol group). Any of these groups provide acidic functionality. The total molar amount of acidic functionality in the polymer is summarized for the calculation of the molar ratio of acidic and basic functionality.
If a polymer exhibits basic functionality, said functionality may be, e.g., provided by a nitrogen containing group, such as a nitrogen in a group selected from the group consisting of pyridine, triazole, benzotriazole, pyrazol, benzpyrazol, imidazole, and benzimidazole. The total molar amount of basic functionality in the polymer is summarized for the calculation of the molar ratio of acidic and basic functionality.
The term “lignin-based electrolyte” as used herein refers to a redox pair of lignin-derived molecules, such as quinone, and derivatives thereof.
The present disclosure relates to an acid-base polymer blend membrane. The membrane is thus composed of a blend of at least two different polymers, namely a first polymer exhibiting acid groups A, and a second polymer exhibiting basic groups B. The core of the polymer is a blend of two polymers with different functionality, one providing acidic, the other providing basic functionality. In other words, acid groups A and basic groups B are not present in the same polymer but different polymers each providing only one functionality selected from the group consisting of acidic groups A and basic groups B. Therefore, it is understood that a polymer blend membrane according to the present disclosure comprises two different polymers, i.e., a first polymer and a second polymer, wherein the first polymer exhibits only acidic functional groups A and the second polymer exhibits only basic functional groups B or vice versa. With this core in mind, it is understood that for each functionality, also more than one polymer may be used, i.e., a mixture of at least two polymers both providing acidic functionality, and / or a mixture of at least two polymers both providing basic functionality. Such mixtures may allow for a further tailoring of the acidic or basic properties of the polymer blend.
The first polymer used in the polymer blend is a polymer exhibiting acidic groups. Such polymer is also referred to herein as “acidic polymer”.
In a preferred embodiment, the acidic group of the first polymer is selected from the group consisting of —SO3H, —PO3H, —PO3H2, —COOH, —AsO3H, —SeO3H and/or —C6H4OH.
In a further preferred embodiment, the acidic group is —SO3H.
However, it is understood that also more than one of the different acidic groups may be present in a single polymer.
In a preferred embodiment, the polymer exhibiting an acidic group makes use of only one acidic group, not exhibiting different acidic groups, in particular from the groups as listed above. Thus, in addition to a mixture of different polymers each exhibiting a different acidic group, different acidic groups may also be provided within a single polymer.
Thus, in one embodiment, the at least one first polymer exhibiting acidic groups is a polymer exhibiting at least one sulfonate group (—SO3H), at least one phosphite group (—PO3H), at least one phosphonate group (—PO3H2), at least one carboxyl group (—COOH), at least one arsonate group (—AsO3H), at least one selenoic group (—SeO3H) and/or at least one phenol group (—C6H4OH) per repeating unit.
The acidic polymer may be prepared from a polymer not exhibiting acidic groups by introducing said acidic groups. Acidic groups may be introduced by known measures. For instance, a sulfonate group may be introduced into a polymer by sulfonation, e.g., using concentrated sulfuric acid or oleum. Alternatively, the polymer may be prepared using monomers exhibiting the desired acidic group.
The degree of acidity may be influenced by process parameters when introducing the acidic group to the polymer, or by using a mixture of monomers wherein one type of monomer is not exhibiting an acidic group (“non-acidic monomer”), and another type of monomer exhibits an acidic group (“acidic monomer”). By varying the ratio of acidic monomer to non-acidic monomer, the DA may be influenced. It is understood that monomers may also exhibit more than one acidic group, and mixtures of non-acidic monomer, acidic monomer and acidic monomer with two or more acidic groups may also be used to vary the degree of acidity.
In a preferred embodiment, the backbone polymer, i.e., the polymer not exhibiting an acidic group, may be selected from poly(arylene ether sulfone) (PAES), poly(ether ether ketone) (PEEK), and poly (ether ketone) (PEK). A preferred embodiment of PAES is polyphenylsulfone (PPSU).
A particularly preferred acidic group is the sulfone group (—SO3H). The degree of acidity in a sulfonated polymer is expressed as degree of sulfonation (DS). As already outlined above, the sulfonated polymer may be prepared by direct sulfonation of a backbone polymer, or by (co-)polymerization using monomers having at least one sulfone group.
Thus, a preferred embodiment of the present disclosure relates to the use of sulfonated poly(arylene ether sulfone) (sPAES), sulfonated poly(ether ether ketone) (sPEEK), and sulfonated poly(ether ketone) (sPEK) as the at least one first polymer.
In a further preferred embodiment, the at least one first polymer is selected from the group consisting of sulfonated polyphenylsulfone (sPPSU), sulfonated poly(ether ether ketone) (sPEEK), and sulfonated poly(ether ketone) (sPEK), with the sulfonated poly(ether ether ketone) (sPEEK) being further preferred.
In a preferred embodiment, sPAES is sulfonated polyphenylsulfone (sPPSU) having the following structural representation:
The polymer sPPSU may be obtained by copolymerization of a monomer bearing two sulfonate groups and a monomer bearing no sulfonate group. The DS of sPPSU is calculated on the basis of the ratio of n and m, i.e., the ratio of the un-sulfonated monomer (in the amount of n) and the double-sulfonated monomer (in the amount of m). As an exemplary calculation, if the ratio of n and m is 1, i.e. both monomers are used in equal amounts, the degree of sulfonation is 50% with - on average - one sulfone group per monomer.
In another preferred embodiment, the at least one first polymer exhibiting acidic groups A is sPEEK.
sPEEK may be obtained by the direct sulfonation of PEEK.
In a preferred embodiment, the DS of sPEEK is at least 30 %, or at least 40 %, or at least 50 %, or at least 60 %, or at least 70 %, or at least 80 %, or at least 90 %. In a more preferred embodiment, the DS of sPEEK is at least 50 %, or at least 60 %, or at least 70 %.
In another preferred embodiment, the DS of sPEEK is 90 % or less, or 80 % or less, or 70 % or less, or 60 % or less, or 50 % or less, or 40 % or less, preferably 70 % or less, or 60 % or less.
In another preferred embodiment, the at least one first polymer exhibiting acidic groups is sPEK.
sPEK may be obtained by the direct sulfonation of PEK.
In a preferred embodiment, the DS of sPEK is at least 30 %, or at least 40 %, or at least 50 %, or at least 60 %, or at least 70 %, or at least 80 %, or at least 90 %. In a more preferred embodiment, the DS of sPEK is at least 30 %, or at least 40 %, or at least 50%.
In another preferred embodiment, the DS of sPEK is 90 % or less, or 80 % or less, or 70 % or less, or 60 % or less, or 50 % or less, or 40 % or less, preferably 60 % or less, or 50 % or less, or 40 % or less.
The second polymer used in the polymer blend is a polymer exhibiting basic groups. Such polymer is also referred to herein as “basic polymer”.
In a preferred embodiment, the basic group of the second polymer is selected from the group consisting of pyridine, triazole, benzotriazole, pyrazol, benzpyrazol, imidazole, and benzimidazole. Said group may be part of the polymer backbone, or present as a substituent to the polymer backbone.
In a preferred embodiment, the basic group is part of the polymer backbone.
In another preferred embodiment, the basic group is imidazole or benzimidazole, further preferably benzimidazole.
In still another preferred embodiment, only a single basic group is present in the second polymer. However, it is understood that also more than one of the different basic groups may be present in a single polymer.
Similar as the degree of acidity outlined for the first polymer above, a degree of basicity may be determined for the second polymer. Reference is made to the explanations above, which apply mutatis mutandis.
In another embodiment, the at least one second polymer exhibiting basic groups is meta-polybenzimidazole (m-PBI), or polybenzimidazole—OO (PBI—OO), with m-PBI being further preferred.
m-PBI exhibits one repeating unit, wherein each repeating unit bears two basic benzimidazole groups:
In another embodiment, the at least one second polymer exhibiting basic groups is PBI-OO. PBI-OO exhibits one repeating unit, wherein each repeating unit bears two basic benzimidazole groups:
In the acid-base polymer blend membrane of the present disclosure, at least one first polymer exhibiting acidic groups and at least one second polymer exhibiting basic groups are present. As already outlined above, it is understood that more than two polymers, and in particular more than two polymers exhibiting acid and / or basic groups may be present.
In one embodiment, an acid-base polymer blend membrane according to the present disclosure comprises a polymer bearing a sulfonate group (—SO3H) as acidic group, and a polymer bearing at least one benzimidazole group as basic group.
In another preferred embodiment, an acid-base polymer blend membrane according to the present disclosure comprises an acidic polymer selected from the group consisting of sPPSU, sPEEK, and sPEK, and a basic polymer selected from the group consisting of m-PBI and PBI-OO, preferably m-PBI.
In a more preferred embodiment, an acid-base polymer blend membrane according to the present disclosure comprises the acidic polymer sPPSU and the basic polymer m-PBI.
In another more preferred embodiment, an acid-base polymer blend membrane according to the present disclosure comprises the acidic polymer sPEEK and the basic polymer m-PBI.
In yet another preferred embodiment, an acid-base polymer blend membrane according to the present disclosure comprises the acidic polymer sPEK and the basic polymer m-PBI.
The polymer blend membrane of the present disclosure is preferably supported on a support structure. For application of the polymer blend membrane to a support structure, the polymers may be dissolved in a solvent.
Suitable solvents for the preparation of a polymer blend solution are aprotic / polar solvents, in particular N,N-dimethylacetamide (DMAc), dimethyl sulfoxide (DMSO), or N-methyl-2-pyrrolidone (NMP). Another suitable solvent is dimethylformamid (DMF).
The respective polymers may be dissolved in the solvents at a corresponding concentration. The concentration of the polymer in the solution may be in the range of from 1 to 30 wt.-%, preferably 3 to 20 wt.-%, further preferably 5 to 10 wt.-%.
The polymers may be dissolved in the solvent by stirring the solvent and the polymer for several hours, such as for 2 to 20 hours. Additionally, the polymer may be dissolved in the solvent at elevated temperatures, such as at 50 to 150° C. After preparation of the solution, it may additionally be filtered to remove excess polymer which was not dissolved.
It is preferred to prepare two separate solutions for the acidic polymer and the basic polymer, respectively. These two separate solutions may then be combined to form a single solution for application to the substrate. Optionally, the acidic solution may be deprotonated, e.g. using triethyl amine (TEA), diethyl amine (DEA) or n-propyl amine.
It is understood that the solvent may not fully dissolve the polymers, resulting in a solution, which may also be termed as stable suspension. For ease, the solution or stable suspension of the polymer is termed solution herein.
The cell membrane is composed of a support structure impregnated with the acid-base polymer blend membrane as disclosed herein.
According to a preferred embodiment, the support structure is a woven or nonwoven fabric. Both are commonly referred to as fabric in the following.
In one embodiment, the woven fabric may be a 2D woven fabric, such as a square mesh fabric, or a 3D woven fabric, such as a braid fabric.
In an alternative embodiment, the support structure is a nonwoven fabric (fleece). For economic reasons, the use of a nonwoven fabric is preferred.
As just outlined, the support structure is preferably a woven or nonwoven fabric, with a nonwoven fabric being further preferred. In a further preferred embodiment, the woven or nonwoven fabric comprises a polymer selected from the group consisting of polyethylene (PE), polypropylene (PP), polyamide (PA), polysulfone (PSU), poly(ether ether ketone) (PEEK), poly(ether ketone) (PEK), polyvinylidene fluoride (PVDF), polyethersulfone (PES), polyetherimide (PEI), polybenzimidazole (PBI), polyethylene terephthalate (PET), polyester and polyphenylene oxide (PPO).
According to a still further preferred embodiment, the woven or nonwoven fabric, preferably the nonwoven fabric, comprises a polymer selected from the group consisting of polyethylene (PE), polypropylene (PP), polyamide (PA), polysulfone (PSU), poly(ether ether ketone) (PEEK), poly(ether ketone) (PEK), polyethylene terephthalate (PET), and polyester.
According to another preferred embodiment, the woven or nonwoven fabric, preferably the nonwoven fabric, comprises a polymer selected from the group consisting of polyethylene (PE), polypropylene (PP), and polyester.
In general, the support structure, preferably the nonwoven fabric, may have a thickness in the range of from 1 to 250 µm, preferably of from 1 to 200 µm, or from 2 to 200 µm, or from 5 to 100 µm, or from 10 to 200 µm, or from 50 to 100 µm, or from 5 to 50 µm, or from 20 to 50 µm, or preferably in the range of from 1 to 60 µm, or from 10 to 50 µm, or from 1 to 25 µm, or from 2 to 20 µm. If the thickness of the support structure is too low, it becomes more difficult to coat the support structure in an appropriate manner with the polymer blend solution to achieve a satisfactory polymer blend film for use as membrane. On the other hand, if the support structure is too thick, it becomes uneconomic. Also a thick support structure is more difficult to entirely coat throughout the thickness of the support structure.
The nonwoven fabric for use in the support substrate of the cell membrane according to the present disclosure may be prepared by melt-blowing processes or prepared by wet-laid technologies, optionally including a calibration using known calendar processes. The nonwoven fabric may optionally have a gradient structure, or it may be homogenous.
For use in accordance with the present disclosure, the fabric may have a thickness in the range of from 1 to 250 µm, preferably of from 1 to 200 µm, or from 2 to 200 µm, or from 5 to 100 µm, or from 10 to 200 µm, or from 50 to 100 µm, or from 5 to 50 µm, or from 20 to 50 µm, or preferably in the range of from 1 to 60 µm, or from 10 to 50 µm, or from 1 to 25 µm, or from 2 to 20 µm. The mean fiber diameter may be in the range of from 1 to 50 µm, preferably from 1 to 25 µm, or from 2 to 20 µm.
An exemplary process for the preparation of a nonwoven fabric impregnated with an acid-base polymer blend membrane according to the present disclosure is described in a non-limiting manner in the following with reference to
A nonwoven fabric (1) as substrate is provided as rolled good. For coupling activation, the nonwoven fabric (1) is treated with a plasma in a plasma treating apparatus (2). The polymer blend solution is provided in a batch reactor (3) under constant stirring to avoid precipitation and maintain a constant concentration of the polymer blend solution. With a pump (4), the solution is provided to a slot die or doctor blade assembly (5) where the polymer blend solution is applied to the nonwoven fabric (6). In an alternative method (not shown in
According to one embodiment, the cell membrane can be a partially impregnated with the acid-base polymer blend solution, resulting in a polymer blend membrane being present as a functional polymer film / ion exchange membrane on one side of the fabric support structure.
As exemplarily shown in
According to another embodiment, the cell membrane can be a fully impregnated with the acid-base polymer blend solution, resulting in a polymer blend membrane being present as a functional polymer film / ion exchange membrane on both sides of and throughout the fabric support structure. Both sides of the support structure are thus fully covered in a closed manner with an acid-base polymer blend membrane in the form of a film. In particular, if the absorptive capacity or the absorption kinetic of the fabric is low, coating on both sides and throughout the fabric may be advantageous.
In general, the thickness of the polymer blend membrane (“polymer membrane”) within and on top of the support structure, i.e. the woven or nonwoven fabric, preferably the nonwoven fabric, may be in the range of from 10 to 100 µm, preferably from 10 to 50 µm, or from 15 to 30 µm, or from 17 to 25 µm. The thickness of the cell membrane (“reinforced polymeric membrane”) for use in RFBs is usually preferably in the range of from 10 to 100 µm, while the thickness for other applications may be rather in the range of from 10 to 400 µm. It is preferred that the polymer blend membrane extends mainly into the support structure, but forming a smooth and closed surface on one or both sides of the support structure. Said smooth and closed surface may extend above and / or below the surface of the support structure, essentially sealing the support surface with the polymer blend membrane.
The acid-base polymer blend membrane fully covers the area of the support structure, providing a closed membrane. This is achieved by fully or essentially fully coating the fibers of the fabric support structure. The adherence of the acid-base polymer blend membrane may be increased by a plasma treatment of the fabric support structure, or, in an alternative or additional measure, by the use of a bonding or coupling agent. In particular for use in, e.g., a redox flow battery, the provision of a closed membrane is important. The impregnated polymer film should be a film without holes, bubbles, or other kinds of interruptions so that a defect free ion conduction through the membrane is provided for. Incorporations of gas, such as air, or holes in the polymer are disadvantageous, but may occur if the support material is not well coated or wetted by the polymer blend solution. In addition, holes in the polymer blend membrane may allow for the electrolytes to be mixed, resulting in a “cross-over”, which leads to an internal discharge of the battery, without providing an electrical current.
The cell membranes of the present disclosure, i.e., the impregnated fabric, may be further processed into suitable arrangements for use in a electrodialysis cell, a fuel cell, in a PEM electrolyzer, or a redox flow battery, preferably in a redox flow battery. Such processing may include the fixation of a cell membrane in a frame, such as a frame made of a polymeric material. The fixation may be achieved by welding or gluing, using appropriate adhesives. However, it is preferred to weld the cell membrane to frames, which may then also be arranged to stacks. When the cell membrane is welded, e.g., to a frame, the fabric support structure may be used for welding.
The cell membranes of the present disclosure have the advantage of halogen free starting materials, leading to halogen free materials. The cell membranes show low electric resistance and high ion conducting capacity, in particular in strongly basic electrolytes, such as quinone based organic electrolytes, or in strongly acidic electrolytes. The materials are very resistant to harsh conditions, such as strongly basic or acidic environments, or increased temperature during processing due to heat generated by the internal resistance in RFBs, in particular in hot areas, where temperatures in the RFB of as much as, e.g., 60° C. or even 80° C. may be reached. Also the electrolyte crossover is very low, and, if used in batteries, the discharge capacities are high.
The cell membranes may also be produced in a cheap manner due to the use of a support structure which is widely available at low cost. Furthermore, the use of a support structure allows for the preparation of acid-base polymer blend membranes having a very low thickness, such as 10 µm or below, showing a low electric resistance, compared to thicker commercially available polymer membranes, which have a thickness of, e.g., 50 µm. With the ability to prepare thin membranes, this may also add to reduced costs and reduced environmental burden due to reduced amount of polymer material used for the membranes.
In the following, the present invention is illustrated in more detail by way of examples. However, it is understood that the scope of protection is only determined by the attached claims, not being restricted to any of the following examples. The following examples are set forth to assist in understanding the invention and should not be construed as specifically limiting the invention described and claimed herein.
Solvents N,N-dimethylacetamide (DMAc) and dimethyl sulfoxide (DMSO) were purchased from RIVA GmbH Batteries (Germany) and Carl Roth GmbH & Co. KG (Germany), respectively. Prior to its use, DMAc was dried according to a standard distillation method known in the art.
Poly(ether ether ketone) (PEEK) was purchased from Sigma-Aldrich (USA).
Poly(ether ketone) (PEK) was purchased from Axiva.
Polybenzimidazol—OO (PBI—OO) was purchased from Fumatech GmbH (Germany).
Meta-polybenzimidazole (m-PBI, B1) was purchased from HOS-Technik Vertriebs- und Produktions-GmbH (Austria). Prior to the use of polymer m-PBI, it was dried in vacuo for 12 hours at 110° C.
Polymer A1 (sPPSU, sulfonated poly(arylene ether sulfone) was prepared according to a method previously reported in D. Xing, J. Kerres Journal of New Materials for Electrochemical Systems 2006, 9,51-60.
Polymers A2 (sPEEK, sulfonated poly(ether ether ketone)) and A3 (sPEK, sulfonated poly(ether ketone)) were prepared according to a method previously reported in H.-H. Ulrich, G. Rafler Die Angewandte Makromolekulare Chemie 1998, 263, 71-78.
For the GPC (gel permeation chromatography; Agilent Technologies 1200 Series GPC system, USA) measurements, a differential refractometer (Shodex RI71, Showa Denko America, Inc., USA), a viscometer (PSS ETA-2010, PSS GmbH, Germany), and a multi-angle light scattering photometer (PSS SLD 7000, PSS GmbH, Germany) were used as detectors. The stationary phase consisted of two columns of different pore sizes: PSS PFG, 5-7 µm, 300 Å, and PSS PFG 5-7 µm, 1000 Å (PSS GmbH, Germany).
The total ion exchange capacity (IECtotal) was determined by acid-base titration experiments using bromothymol blue. Prior to experiments the polymers were washed with demineralized water until complete neutralization. Subsequently, the polymers were transferred into the respective Na+ form by bathing the membrane in saturated NaCI solution for 24 hours. The acidic solution was then titrated with 0.1 M NaOH solution until complete neutralization. Afterwards, a defined surplus of NaOH was added to the solution and titrated back with 0.1 M HCI until the equivalent point was reached. The IECtotal was calculated using formula (1):
The degree of sulfonation (DS) was determined in a four-step procedure. At first, the molecular weight of polymers of different degrees of sulfonation, e.g. 25, 50, 75, and 100 %, are calculated. In a subsequent step, the IECtheor of the polymers with above mentioned degrees of sulfonation are calculated via formula (2): [0153]
Then, the degree of sulfonation was plotted over the calculated IECtheor values. The obtained data points were fitted with a polynomic function. In the third step, the degree of sulfonation is plotted over the IECtheor and the data points are fitted with a polynomic function. At last, the degree of sulfonation of the polymers is calculated by inserting the experimentally determined IECtotal into said polynomic function.
Each polymer product was dissolved in a solution of 5 g LiBr per 1 L of DMAc and then subjected to GPC measurement in order to perform mass analysis. In particular, the sulfonation degree (DS) was determined in order to prepare polymer blends of the acid group/base group ratio according to the present disclosure. The results of each polymer batch used in the experiments are presented in Table 1.
Step 1: An acidic polymer A1, A2 and/or A3 was dissolved in a respective solvent (e.g., DMSO and/or DMAc) preparing a 10 wt.-% solution under stirring for nine (9) hours at room temperature. Alternatively, stirring was performed for four (4) hours at 80° C. The stirring was performed at 500 rpm for 1 hour, then at 300 rpm for 3 hours.
Step 2: In a sealed Schott flask, a basic polymer of B1 was dissolved in solvent DMAc preparing a 5 wt.-% solution under stirring for 12 hours at 150° C. The stirring was performed at 700 rpm for 2 hours, then at 400 rpm for 10 hours. The dissolved basic polymer was cooled to room temperature and then filtered with a suction filter.
Step 2.1: In the case of an acid-base polymer blend combination comprising the acidic polymer A3, e.g. A3-B1, the acidic polymer solution obtained in step 1 was subjected to deprotonation by adding triethyl amine (TEA; about 0,5 mL/1 g of A3), followed by step 3.
Step 3: Both solutions obtained in steps 1 and 2, or steps 1 and 2.1 were mixed in different weight ratios 90 / 10, 93 / 7 and 96 / 4. The distinct molar ratio of acid groups A to basic groups B in said mixtures are presented in Table 2. Depending on the used acidic polymer, the mixture was stirred at room temperature at 400 rpm for different periods of time (A1 or A2: three (3) hours; A3: 12 hours). The mixture was then filtered obtaining a homogeneous polymer solution.
The acid-base polymer blend membrane was prepared using a membrane casting machine Elcometer 4340 using a squeegee with an adjustable gap height from 0-2000 µm both (Elcometer Instruments GmbH, Germany). Prior to usage, the glass plate of the membrane casting machine was pre-treated as described in the following. The glass plate was cleaned with a sponge and demineralized water. The surface of the cleansed glass plate was passivated using isopropyl alcohol (purity > 98 %), then dried with a cloth.
The acid-base polymer solution prepared as described above was coated on the pre-treated glass plate (about 25 mL/DIN A4-sized area). The squeegee gap was set at a distance of 600 µm to the glass plate. At a processing temperature of 20° C. to 45° C., the coating acid-base polymer solution was drawn out to a thin film using a squeegee at a speed of 20 mm/s to 60 mm/s. A spacer (with a height of about 1 to 2 cm) and then a further pre-treated glass plate was stacked on top of the coated glass plate. The resulting pile was dried at 80° C. for 12 hours, then at 130° C. for 2 hours. After bathing the coated and dried glass plate in demineralized water for 5 to 10 minutes, the membrane was separated from the glass plate. The obtained membrane was then activated in HCI (10 wt.-%) or a mixture of NaOH/KOH (1 M/1M) for 24 hours at 90° C. The activated membrane was washed with demineralized water for 5 minutes, then bathed in fresh demineralized water for 24 hours at 90° C.
In order to investigate the battery performance, the specific membrane resistance (Rm), the cell resistance (Rc), the coulombic efficiency (CE) and the ion exchange capacity (IEC) were analyzed for the acid-base polymer blend membranes of the combination types A1-B1, A2-B1 and A3-B1 at 20° C. The data of the acid-base polymer blend membranes was compared to the reference membrane Fumasep® E620PE from Fumatech. The results are presented in Table 3.
The measurement of the specific membrane resistance (Rm) was performed on an Autolab PGSTAT 204 potentiostat / galvanostat instrument (Metrohm, Switzerland) through a potentiostatic electrochemical impedance spectroscopy (EIS) with an amplitude of 20 mV in a frequency range of 105 Hz to 1 Hz using a TSC battery test cell (RHD Instruments, Germany) with 0,5 M H2SO4 electrolyte solution. The applied test cell exhibits an active membrane surface of 38 mm2. Prior to the experiment, the acid-base polymer blend membrane was bathed in a 0,5 M H2SO4 electrolyte solution for at least 12 hours.
The measurements of the cell resistance (Rc) and the coulombic efficiency (CE) were performed on an Autolab PGSTAT 204 potentiostat / galvanostat instrument (Metrohm, Switzerland) using a redox flow battery (RFB) test cell with an all-vanadium electrolyte system (1.6 M V3+/V4+ electrolyte, GfE Metalle und Materialien GmbH, Germany). The active membrane surface in the RFB cell was 6 cm2. Two thermally pre-treated SIGRACELL GFD 2,5 EA carbon-fleeces with an uncompressed thickness of 2.5 mm (SGL Carbon, Germany) served as electrodes which were placed into a flow channel. Epoxy impregnated graphite plates (Müller & Rössner, Germany) were used as current collectors.
For the battery experiments, 20 mL of the vanadium electrolyte was pumped into each half cell at a constant flow rate of 25 mL/min using a peristaltic pump (Ismatec, USA).
The cell resistance (Rc) was determined by means of polarization experiments. During a polarization experiment, energy was taken from the RFB by applying an electrical load at a constant current of 2.5 mA/cm2 for 30 seconds. Then, the constant current was gradually increased to 65 mA/cm2 with a stepsize of 2.5 mA/cm2 each time holding the particular current for 30 seconds. The resulting battery voltages were simultaneously recorded. The cell resistance (Rc) was calculated from the measured gradient of the polarization curve with current and voltage plotted on the x-axis and the y-axis, respectively.
The coulombic efficiency (CE) was calculated via the charge and discharge currents recorded within the charge/discharge cycles using formula (3):
During the charge / discharge cycles, the RFB was charged with a constant current of 43 mA/cm2 and 65 mA/cm2, respectively, and then discharged. The calculated coulombic efficiency values are each mean values of 4 charge / discharge cycles. Prior to the experiment, the acid-base polymer blend membrane was bathed in a 2.5 M H2SO4 electrolyte solution for at least 12 hours.
The ion exchange capacity (IEC) was determined by acid-base titration experiments using bromothymol blue. Prior to the experiment the acid-base polymer blend membrane in the protonated form was transferred into the respective Na+ form by bathing the membrane in saturated NaCI solution for 24 hours. The acidic solution was then titrated with 0.1 M NaOH solution until complete neutralization. The ion exchange capacity (IEC) was calculated using formula (4):
The battery performances of the acid-base polymer blend membranes according to the present disclosure were compared to the prior art reference membrane Fumasep® E620PE. Data on the reference membrane are presented in Table 3.
The battery performances of the acid-base polymer blend membranes according to the present disclosure were compared to the prior art reference membrane Fumasep® E620PE. Data on the reference membrane are presented in Table 3.
In order to investigate the battery performance, the specific membrane resistance (Rm), the cell resistance (Rc), the coulombic efficiency (CE) and the ion exchange capacity (IEC) were analysed for the acid-base polymer blend membranes of the combination types A1-B1, A2-B1 and A3-B1 at 20° C. The data of the acid-base polymer blend membranes was compared to the prior art reference membrane Fumasep® E620PE. The results are presented in Table 4.
The results show that each one of the ion exchange membranes according to the present disclosure exhibit, in particular, more favourable membrane resistance, cell resistance and ion exchange capacity than the reference membrane (see Table 3). Notably, the acid-base polymer blend membranes A1-B1, A2-B1 and A3-B1 exhibit at least half the membrane resistance Rm as the reference membrane. The Rm value of A2 B1 stands out with an Rm of 45,4 Ω*cm.
The effect of different processing temperatures and speed of squeegee, respectively, during the preparation of membrane A2-B1 was investigated with regard to the membrane resistance Rm (Table 5).
The results presented show that the membrane resistance strongly depends on the method the ion exchange membrane was prepared. Herein, it is described two parameters during the membrane preparation, namely the processing temperature and the speed of squeegee which determine the membrane resistance.
Investigations show that the Rm value decreases when increasing the processing temperature during the membrane preparation. For example, the membrane resistance of A2-B1 with the A / B molar ratio of 1 / 0.2 decreases from 90.03 Ω*cm to 44.39 Ω*cm when increasing the processing temperature from 20° C. to 45° C. A similar trend is observed for the other two A / B molar ratios. Notably, the extent of the decrease in Rm attenuates at higher A / B molar ratios, i.e. when the acidic proportion of the polymer blend increases.
Furthermore, the Rm value depends on the speed of squeegee during the membrane preparation. Overall a trend is observed, wherein the membrane resistance increases at higher speeds of squeegee. For example, the Rm value of the A2-B1 membrane with an A / B molar ratio of 1 / 0.14 is 1.5 times higher when increasing the speed of squeegee from 40 mm/s to 60 mm/s (from 33.53 Ω*cm to 54.36 Ω*cm). Again, similarly to the effect observed for the processing temperature, this trend smoothens at increasing A / B molar ratios. At an A / B molar ratio of 1 / 0.08, for example, the speed of squeegee has no considerable effect on the membrane resistance. To the contrary, a slight decrease of the Rm value is observed when increasing the speed of squeegee from 20 mm/s to 60 mm/s (from 22.05 Ω*cm to 21.28 Ω*cm).
To determine the water uptake of the polymer blend membranes according to the present disclosure, the polymer blend membranes A2-B1 were immersed in deionized water or 2.5 M H2SO4 for 40 h at 25° C. or 55° C. The weight in the dry (Mdry) and wet (mwet) states have been measured and the water uptake was determined according to formula (5):
The results are summarized in the following table:
| Number | Date | Country | Kind |
|---|---|---|---|
| 20205083.7 | Oct 2020 | EP | regional |
This application is a continuation application of International Application No. PCT/IB2021/060007 filed on Oct. 29, 2021, which claims the benefit of European Application No. 20205083.7 filed on Oct. 31, 2020, the entire disclosures of which are incorporated herein by reference for all purposes.
| Number | Date | Country | |
|---|---|---|---|
| Parent | PCT/IB2021/060007 | Oct 2021 | WO |
| Child | 18296488 | US |
