Crosslinked hollow fiber membrane and new method for producing same

Abstract

To provide a method for producing a hollow fiber membrane which can obtain a hollow fiber membrane that has high chemical resistance and good mechanical strength.SOLUTION: A method for producing a hollow fiber membrane includes: extruding a phase composition containing a polymer selected from the group consisting of polyimide, copolyimide, block copolyimide, polyether imide, polyamide imide and a mixture or a blend thereof, and a solvent or a solvent mixture of the polymer, from an orifice of a hollow fiber die; coextruding a phase composition containing an amine-based crosslinking agent having at least two amino groups, preferably, aliphatic or aromatic amine, and a non-solvent or a non-solvent mixture of the polymer from a central orifice of the hollow fiber die and / or an outside orifice of the hollow fiber die; passing the hollow fiber membrane through a coagulation bath; drying the hollow fiber membrane until all the moisture is not left and / or a residual solvent content is 0 wt.% to 5 wt.%; and heat-treating the hollow fiber membrane at an annealing temperature of 150-280°C.SELECTED DRAWING: None

Description

[Technical Field]

[0001] The present invention relates to a high-performance crosslinked hollow fiber membrane and a new method for producing the same. [Background technology]

[0002] Multilayer hollow fiber membranes are well known in the art. They typically consist of a support layer and a separation layer that can be made of different materials (asymmetric composite membranes) or essentially the same materials (fully asymmetric membranes). In either case, the support layer and the separation layer have different structures.

[0003] Polyimide membranes, in particular, are known to have exceptional inherent separation properties, but are prone to failure when in contact with high levels of CO2, H2S, or higher hydrocarbons. Particularly in natural gas sweetening (i.e., removal of CO2 from product gas CH4), membranes typically encounter feed streams containing numerous higher hydrocarbons (C3+, aromatic and aliphatic), high levels of CO2, and H2S.

[0004] A typical approach to making membranes stronger and more resistant to such conditions is to cross-link the polymer chains.

[0005] The most well-known method is to chemically crosslink the membrane. Patent document 1, for example, discloses a crosslinking method for hollow fiber membranes and flat membranes, in which the membranes are treated with diamines in a downstream step of the membrane manufacturing process. This method is very complicated, environmentally unfriendly, and costly due to the large amount of diamine and additional equipment required for the crosslinking step.

[0006] Patent Document 2 discloses a method for producing a gas separation membrane that exhibits good separation performance even after long-term use under harsh conditions. The membrane is thermally crosslinked at extremely high temperatures in an atmosphere with a very low O2 content. This method has very high energy consumption.

[0007] Non-Patent Documents 1, 2, and 3 disclose a one-step membrane production and cross-linking method. In this method, an organic nucleophilic cross-linking agent is added to the bore solution used in the spinning process. Cross-linking occurs sequentially during membrane formation; a separate downstream cross-linking step is not required. According to these publications, large-pore membranes suitable for ultrafiltration only can be obtained when low-molecular-weight diamines are used as organic nucleophilic cross-linking agents. To obtain membranes suitable for gas separation, high-molecular-weight amines (e.g., polyethyleneimine or PEI) must be used as cross-linking agents. However, it proved very difficult to reduce the thickness of the separation layer and obtain good gas permeability. The mechanical stability of the membranes was insufficient.

[0008] As a result, there remains a great need for efficient methods for producing hollow fiber membranes that are highly insoluble and have good mechanical strength. [Prior art documents] [Patent documents]

[0009] [Patent Document 1] U.S. Patent Publication No. 2016 / 0310912A1 [Patent Document 2] International Publication No. 2014 / 202324A1 [Patent Document 3] International Publication No. 2011 / 108929A1 [Non-patent literature]

[0010] [Non-Patent Document 1] KK Kopec et al., "Spinneret Chemistry - On the Interplay of Cross-Linking and Phase Inversion during Spinning of Novel Hollow Fiber Membranes," Journal of Membrane Science, 369 (2011), pp. 308-318 [Non-patent document 2] S. M. Dutczak et al., "Spinneret chemistry for producing hollow fibers for organic solvent nanofiltration," Separation and Purification Technology, 86 (2012), pp. 183-189 Summary of the Invention [Problem to be solved by the invention]

[0011] It is an object of the present invention to provide a new method for producing hollow fiber membranes which does not have the disadvantages of the prior art methods or has only minor such disadvantages. Another object is to provide a new hollow fiber membrane.

[0012] A specific object of the present invention is to provide a method for producing hollow fiber membranes that allows hollow fiber membranes with high chemical resistance and good mechanical strength to be obtained. Preferably, this should be achieved without a separate post-treatment step for cross-linking the membrane. Even more preferably, a continuous method for producing such hollow fiber membranes should be provided.

[0013] Furthermore, it is an object to provide a cost-effective method, especially in terms of energy consumption and investment costs for equipment. Even more preferably, the new method should be implemented in existing plants with low investment costs.

[0014] It is also an object of the present invention to provide a method that allows the production of membranes with high selectivity and good separation performance. The membranes should preferably be applicable to a wide range of applications, such as gas separation, organic solvent nanofiltration, and vapor recovery.

[0015] The new method should preferably be applicable to a variety of polymers.

[0016] A particular object of the present invention is to provide a method that allows the thickness of the separating layer of the membrane to be controlled and / or allows the production of membranes with inner and / or outer separating layers (i.e., membranes with separating layers on their inner and / or outer sides, preferably the outer side).

[0017] Further objects not expressly stated will be apparent from the overall content of the following claims, the specification, the examples and the figures. [Means for solving the problem]

[0018] The inventors have surprisingly found that these problems can be solved by the method and membranes obtained by this method according to claim 1. The addition of a crosslinker having at least two amino groups to the bore solution in the membrane spinning process, followed by a thermal post-treatment of the dried membrane under mild conditions, results in a highly crosslinked membrane with excellent chemical resistance, mechanical strength, selectivity and separation performance (permeability).

[0019] The new process is cost-effective because it is an in-line process (i.e., it does not require a separate post-treatment cross-linking step). The process of the present invention is less toxic and produces less wastewater compared to prior art processes. Costs can be reduced by reducing the amount of cross-linking agent.

[0020] The milder conditions for thermal post-treatment (i.e., lower temperatures than conventional techniques) offer additional economic benefits. Finally, the new method is advantageous because it can be implemented in existing plant equipment.

[0021] In contrast to the one-step crosslinking methods presented in the prior art, the fibers obtained by the method of the present invention do not have large pores and are suitable for gas separation even when low molecular weight diamines are used as crosslinkers.

[0022] Another important advantage of the method of the present invention compared to the prior art one-step crosslinking method is that it allows for the production of fully asymmetric membranes with a dense outer layer, even when the crosslinking agent is part of the bore solution spun from the central orifice of the spinning die. Therefore, membranes with a dense outer layer can be obtained by using the double-orifice spinneret installed in most existing plants. In the prior art, membranes with a dense inner layer were obtained when the crosslinking agent was added to the bore solution. However, a dense inner layer is usually undesirable and can lead to the risk of breakage and delamination of the hollow fiber.

[0023] Without wishing to be bound by any theory, the inventors believe that this particular advantage of the present invention can be achieved by using amine-based crosslinkers that are less polar and water-soluble. Such crosslinkers preferably diffuse more uniformly from the bore solution into the wall pores and into the polymer, whereas the more polar and water-soluble amine-based crosslinkers used in the prior art preferably remain in the bore solution and then diffuse only into the polymer near the bore.

[0024] The method of the present invention allows for flexible control of the degree of crosslinking of the membrane up to 100% (i.e., 100% insolubility in DMF), as well as flexible control of the mechanical strength and / or dense layer thickness, so that membranes can be tailored for a variety of applications, such as gas separation, vapor recovery, and organic solvent nanofiltration.

[0025] The method of the present invention allows for the use of different types of polymers, which further enhances its flexibility.

[0026] Further advantages not expressly mentioned are evident from the overall content of the following claims, the description, the examples and the figures.

[0027] Before describing the invention in detail, some general definitions are provided below.

[0028] The verb "to comprise" and its conjugations used in the specification, examples, and claims are used in an open-ended sense to include the items that follow it and not exclude bit items not specifically mentioned. In a preferred embodiment, "comprising" encompasses "consisting of," which means that the items that follow it are included and that bit items not specifically mentioned are excluded.

[0029] When an element is preceded by the indefinite article "a" or "an," it does not exclude the possibility that there is a plurality of elements, unless the context clearly dictates that there is only one element. Thus, the indefinite article "a" or "an" usually means "one or more."

[0030] The term "obtainable by" as used in the specification and claims is used in a non-limiting sense, and it is intended that a product obtainable by the method described following the term can be obtained by that method, but does not necessarily have to be obtained by that method. If the same product can be obtained by different methods, these are also included in the scope of protection. In a preferred embodiment, "obtainable" encompasses "obtained by".

[0031] "Phase (a1)" and "Phase (a1) composition" refer to a composition comprising a polymer (a1.i) and a solvent (a1.ii) for said polymer. The "Phase (a1) composition" is also known in the art as a "spinning composition," "dope solution," or "casting solution."

[0032] "Phase (a2)" and "phase (a2) composition" refer to a composition comprising a non-solvent for the polymer (a1.i) and one or more aliphatic or aromatic amines (a2.i) having at least two amino groups. The phase (a2) extruded through the central orifice of the spinning die is also called the "bore liquid", while the phase extruded through the outer orifice is also called the "shell liquid".

[0033] a1.ii (i.e., "solvent or solvent mixture for polymer (a1.i)") is a liquid or a liquid mixture in which polymer (a1.i) can be completely dissolved. Solvent mixture (a1.ii) for polymer (a1.i) can be a mixture of different solvents for polymer (a1.i), but also a mixture of solvents and non-solvents for polymer (a1.i), with a solvent content high enough to completely dissolve polymer (a1.i).

[0034] A "non-solvent or non-solvent mixture for polymer (a1.i)" is a liquid or a liquid mixture in which polymer (a1.i) is not completely soluble, preferably in which polymer (a1.i) is not soluble at all. A non-solvent mixture for polymer (a1.i) can be a mixture of different non-solvents for polymer (a1.i), but can also be a mixture of a solvent and a non-solvent for polymer (a1.i), with a solvent content so low that polymer (a1.i) cannot be completely dissolved in the mixture.

[0035] The "annealing temperature" as used in this specification, examples and claims relates to the temperature of the atmosphere surrounding the membrane during the heat treatment step (d) at a distance of up to 10 cm, preferably 2 to 10 cm, to the outer surface of the membrane.

[0036] The present invention provides (a) the steps of: (a1) extruding a phase (a1) composition (preferably a solution) comprising a polymer (a1.i) selected from the group consisting of optionally functionalized polyimides, copolyimides, block copolyimides, polyetherimides, polyamideimides, or mixtures or blends thereof, and a solvent or solvent mixture (a1.ii) for said polymer (a1.i) through an orifice (preferably an annular orifice) of a hollow fiber die; (a2) co-extruding a phase (a2) composition comprising an amine-based crosslinker having at least two amino groups, preferably an aliphatic or aromatic amine (a2.i), and a non-solvent or non-solvent mixture (a2.ii) for the polymer (a1.i) through a central (preferably annular) orifice of the hollow fiber die and / or through an outer (preferably annular) orifice of the hollow fiber die; A hollow fiber membrane spinning process comprising: (b) passing the hollow fiber membrane through a coagulation bath; (c) drying the hollow fiber membrane until all water is removed and / or the residual solvent content is 0% by weight to 5% by weight; (d) heat treating the hollow fiber membrane at an annealing temperature of 150°C to 280°C, preferably 160°C to 260°C, more preferably 170°C to 250°C, particularly preferably 170°C to 240°C, and most preferably 180°C to 230°C, for preferably 15 minutes to 180 minutes, more preferably 30 minutes to 150 minutes, even more preferably 45 minutes to 120 minutes, and most preferably 50 minutes to 100 minutes; The present invention relates to a method for producing a hollow fiber membrane comprising the steps of:

[0037] By combining the polymer (a1.i) used in step (a) with the method of the present invention, a membrane with good separation performance, mechanical strength, and chemical resistance can be obtained. It is preferable to use a polyimide, copolyimide, or block copolyimide as the polymer (a1.i). The polymer (a1.i) may be a homopolymer, a random polymer, or a copolymer, or may be a mixture or blend of different polymers.

[0038] In principle, all polyimides, copolyimides, block copolyimides, polyetherimides, polyamideimides that are soluble in the solvent or solvent mixture (a1.ii) can be used in the process of the invention. In a preferred embodiment of the invention, the polyimide is one or more dianhydrides selected from the group consisting of BTDA (3,3',4,4'-benzophenone-tetracarboxylic dianhydride), PMDA (pyromellitic dianhydride), BPDA (3,3',4,4'-biphenyl-tetracarboxylic dianhydride), ODPA (4,4'-oxydiphthalic anhydride), BPADA (4,4'-bisphenol A dianhydride, CAS number 38103-06-9), 6FDA (4,4'-(hexafluoroisopropylidene)diphthalic anhydride), 3,3',4,4'-diphenylsulfonetetracarboxylic dianhydride (DSDA); one or more diisocyanates selected from the group consisting of 2,4-TDI (2,4-tolylene diisocyanate), 2,6-TDI (2,6-tolylene diisocyanate) and 4,4'-MDI (4,4'-methylene diphenyl diisocyanate), MesDI (mesitylene diisocyanate, 2,4,6-trimethyl-1,3-phenylene diisocyanate), 2,3,5,6-tetramethyl-1,4-phenylene diisocyanate, diethylmethylbenzene diisocyanate, phenylindane-based isocyanates, and 4,4'-methylene 2,2',6,6'-didimethylphenyl diisocyanate; The polymer (a1.i) is obtained by polycondensation of

[0039] Instead of diisocyanates, the corresponding diamines can be used. In that case, polyamic acids are formed as intermediates, which are converted in a second step to soluble polyimides, for example by chemical or thermal imidization. Such imidization methods are well known to those skilled in the art.

[0040] It is particularly preferred that the polymer (a1.i) is a polyimide having a structure of formula (1). [ka] Formula (I)

[0041] wherein x is greater than or equal to 0 and less than or equal to 0.5, y is greater than or equal to 0.5 and less than or equal to 1, and the sum of x and y is 1. R represents one or more identical or different moieties selected from the group consisting of L1, L2, L3, and L4 moieties. [ka]

[0042] The polyimide is very particularly preferably a polymer of formula (1) where x=0, y=1, and R consists of 64 mol% of L2, 16 mol% of L3, and 20 mol% of L4. This polymer is commercially available under the name P84 or P84 Type 70 and has the CAS number 9046-51-9.

[0043] Also very particularly preferably, the polyimide of formula (1) is a polymer having the following composition: x=0.4, y=0.6, R=80 mol % of L2 and 20 mol % of L3, which is commercially available under the name P84HT or P84HT325 and has the CAS number 134119-41-8.

[0044] Further details regarding the preparation of these and further similar polyimides can be found in WO 2011 / 009919, the content of which is expressly incorporated herein by reference. All polymers described in the examples of WO 2011 / 009919 are particularly preferably used as polymers (a1.i) in step (a1) of the process of the present invention.

[0045] German Patent Publication No. 21 43 080 describes the preparation of solvent-soluble polyimides made from BTDA and a mixture of toluene-2,4-diisocyanate, toluene-2,6-diisocyanate, and 4,4'-methylenediphenyldiisocyanate. It also describes the preparation of solvent-soluble polyamic acids made from BTDA and a mixture of toluene-2,4-diamine, toluene-2,6-diamine, and 4,4'-methylenediphenyldiamine, and their subsequent imidization to the corresponding polyimides. Details regarding the preparation of these and other similar polyimides and polyamic acids can be found in German Patent Publication No. 21 43 080, the entire contents of which are expressly incorporated herein by reference. All polymers described in the examples of German Patent Publication No. 21 43 080 are particularly preferably used in the process of the present invention.

[0046] In another preferred embodiment of the present invention, the polymer (a1.i) is a block copolyamide, i.e. a copolymer consisting, preferably consisting only, of blocks (A) and (B) of the following formulae (2) and (3): [ka]

[0047] The blocks A and B have different compositions, i.e., the pairs of R1 and R3 and R2 and R4, respectively, cannot be identical at all the same time. The block copolyamide of this preferred embodiment comprises a continuous phase of block A in which the functional group R1 has either or both of the following functional groups: [ka]

[0048] R2 has at least one, or two, or three of the following functional groups: [ka]

[0049] Block A has the following composition in the most preferred embodiment: AF1: 100 mol % R1b, approximately 64 mol % R2a, 16 mol % R2b, 20 mol % R2c. AF2: 40 mol % R1a, 60 mol % R1b, approximately 80 mol % R2a, 20 mol % R2b. The mole percentages given are with respect to the functional groups R1 and R2, the amounts of the various units being chosen such that the total for each of these groups is 100 mole %. Block B is chosen as a polymer that is significantly more permeable than block A. R3 of block B contains at least one or more of the following functional groups: [ka]

[0050] (wherein X is as follows): [ka]

[0051] R4 includes at least one or more of the following functional groups: [ka]

[0052] wherein X1, X2, X3, and X4 are either H or CH3, or an alkyl radical having 2 to 4 carbon atoms, and Y is -CH2-, -(CH3)2C-, -SO2-, -(CF3)2C-, -CO-, -COO-, -CONH-, or -O-.

[0053] wherein at least one of the radicals X1 to X4, preferably at least two of the radicals X1 to X4, more preferably at least three of the radicals X1 to X4, and most preferably all of the radicals X1 to X4 are equal to CH3 or a C2 to C4 alkyl radical.

[0054] R 4c Y in R is preferably —CH—, —(CH)C—, —(CF)C— or —O—, more preferably —CH— or —(CH)C—. 4c It is particularly preferred that R has the following composition: X1, X2 and X3 = H, X4 = CH3 or a C2-C4 alkyl radical, Y = -CH2- or -(CH3)2C-, or X1 and X3 = CH3 or a C2-C4 alkyl radical, X2 and X4 = H or CH3, Y = -CH2- or -(CH3)2C-. 4c Most preferably, X1, X2, X3 and X4 have the following composition: X1, X2, X3 and X4 = CH3 or a C2-C4 alkyl radical, Y = -CH2- or -(CH3)2C-, preferably -CH2-. In the above preferred embodiment, if the radicals X1 to X4 are not H, they are most preferably CH3.

[0055] In one particularly preferred embodiment, block (B) has the following composition: AF3: 40-60 mol % R3a, 0-10 mol % R3b, 60-30 mol % R3c and approximately 90-100 mol % R4a, 0-10 mol % R4b and 0-10 mol % R4c. AF4: 50 mol % R3a, 50 mol % R3c and 100 mol % R4a.

[0056] The mole percentages given for AF3 and AF4 relate to the functional groups R3 and R4, respectively, so the amounts of the various units are each chosen so that the sum of each of these groups equals 100 mole %. Very particular preference is given to the combination of the abovementioned AF1 and / or AF2 with AF3 and / or AF4. Most preference is given to the combination of AF1 or AF2 with AF4.

[0057] The block lengths n and m of blocks A and B are preferably in the range of 1 to 1,000, more preferably 1 to 500, more preferably 1 to 200, more preferably 5 to 150, more preferably 10 to 100, more preferably 10 to 50, and most preferably 10 to 40. The block lengths of blocks A and B may be the same or different. Block copolyamides may also exhibit some distribution with respect to the specific block lengths of blocks A and B. That is, it is not necessary for all blocks A or all blocks B to be the same length. Thus, the ratio of blocks A to B may vary over a wide range. The proportion of block B in the block copolyamide according to the present invention may be 5 to 90% and that of block A may be 10 to 95%. A:B ratios of 80:20, 70:30, 60:40, or 50:50 are particularly preferred, and most preferably 45:55.

[0058] Further details regarding the preparation of the block copolyimide of the second preferred embodiment and further similar polyimides can be extracted from WO 2015 / 091122, the contents of which are expressly incorporated herein by reference. All polymers described in the examples of WO 2015 / 091122 are particularly preferably used as polymers (a1.i) in step (a1) of the method of the present invention.

[0059] In a third preferred embodiment, a polyimide according to US Pat. No. 3,856,752, in particular a BTDA / DAPI (diaminophenylindane) based polyimide commercially available as Matrimid 5128 with CAS number 104983-64-4, is used as polymer (a1.i).

[0060] Step (a) uses a phase (a2) comprising one or more crosslinkers having at least two amino groups (a2.i), said crosslinkers preferably being selected from the group consisting of aliphatic or aromatic amines having at least two amino groups and mixtures thereof.

[0061] In a preferred embodiment of the present invention, an aliphatic or aromatic amine having at least two amino groups is used as crosslinking agent (a2.i) selected from the group consisting of: - a substituted or unsubstituted linear or branched aliphatic amine comprising a carbon chain having 5 to 24 carbon atoms, preferably 5 to 20 carbon atoms, more preferably 6 to 18 carbon atoms, most preferably 6 to 15 carbon atoms, and 2 to 5, preferably 2 to 4, more preferably 2 to 3, most preferably 2 amino groups, preferably primary amino groups, and having 6 to 30 carbon atoms, preferably 6 to 24 carbon atoms, more preferably 6 to 20 carbon atoms, most preferably 6 to 18 carbon atoms, - Substituted or unsubstituted cycloaliphatic amines having 6 to 24 carbon atoms (preferably excluding 1,3-diaminocyclohexane and 1,4-diaminocyclohexane) (the substituted or unsubstituted cycloaliphatic amines preferably have 7 to 20 carbon atoms, more preferably 8 to 18 carbon atoms, and most preferably 8 to 15 carbon atoms, and 2 to 5, preferably 2 to 4, more preferably 2 to 3, and most preferably 2 primary amino groups, and optionally contain heteroatoms in the alkyl chain or as bonds between aliphatic rings); - substituted or unsubstituted aromatic or alkylaromatic amines having 6 to 24 carbon atoms, preferably 7 to 20 carbon atoms, more preferably 8 to 18 carbon atoms, most preferably 8 to 15 carbon atoms and 2 to 5, preferably 2 to 4, more preferably 2 to 3, most preferably 2 primary amino groups, and optionally containing heteroatoms; A mixture of them.

[0062] The linear or branched aliphatic amines may be substituted. For example, they may contain one or more functional groups, such as hydroxyl, carbonyl, thiol, ester, or amide groups, in addition to the amino group. One or more carbon atoms in the aliphatic carbon chain may be replaced by a heteroatom, such as N, O, or S, but the aliphatic amines must contain at least one fragment (not interrupted by a heteroatom) of a carbon chain having 5 to 24 carbon atoms, preferably within the above range.

[0063] Alicyclic amines may be substituted or unsubstituted. For example, they may contain, in addition to the amino group, one or more functional groups, such as hydroxyl, carbonyl, thiol, ester or amide groups. Possible further substituents are preferably selected from the group consisting of: - linear or branched alkyl groups having 1 to 6, preferably 1 to 4, more preferably 1 to 3, even more preferably 1 or 2, most preferably 1 carbon atom, and optionally carrying one or more functional groups, preferably amino or hydroxy groups, most preferably amino groups, cycloalkyl or alkyl-cycloalkyl groups having 3 to 18, preferably 4 to 15, more preferably 5 to 12, even more preferably 6 or 12 carbon atoms, optionally carrying one or more functional groups, preferably amino or hydroxy groups, most preferably amino groups; - a divalent alkyl or cycloalkyl group forming a fused ring system of two or three alkyl rings.

[0064] One or more carbon atoms of the alicyclic ring may be replaced by a heteroatom, such as N, O or S. Alicyclic amines containing up to one heteroatom in the alicyclic ring (particularly preferably, no heteroatoms) are preferred.

[0065] The aromatic or alkylaromatic amines may be substituted or unsubstituted. That is, they may contain, in addition to the amino group, one or more functional groups, such as hydroxyl, carbonyl, thiol, ester, or amide groups. The further substituents are preferably linear or branched alkyl, cycloalkyl, or alkyl-cycloalkyl groups having 1 to 6, preferably 1 to 4, more preferably 1 to 3, even more preferably 1 or 2, and most preferably 1 carbon atom, and optionally having one or more functional groups, preferably amino or hydroxyl groups, most preferably amino groups.

[0066] One or more carbon atoms of the aromatic ring or one of its substituents may be substituted with a heteroatom, such as N, O or S. Aromatic amines containing at most one heteroatom (particularly preferably no heteroatoms) in the aromatic ring are preferred.

[0067] As mentioned above, it is preferred to use as crosslinker (a2.i) an amine-based crosslinker with low polarity and water solubility, which provides the advantages described above and further illustrated in the examples below.

[0068] In another preferred embodiment of the present invention, an aliphatic or aromatic amine having at least two amino groups is used as cross-linking agent (a2.i) having an octanol-water partition coefficient log P of greater than or equal to −0.5.

[0069] The P value represents the concentration ratio of a substance in a two-phase system consisting of 1-octanol and water and is reported in logarithmic form (log P, base 10) (J. Sangster, Octanol-Water Partition Coefficients: Fundamentals and Physical Chemistry, Wiley Series in Solution Chemistry, Vol. 2, John Wiley & Sons, Chichester, 1997). The octanol-water partition coefficient increases with increasing lipid solubility and decreasing water solubility. It is particularly preferred to use amine-based crosslinkers (a2.i) with an octanol-water partition coefficient log P of -0.4 or greater, more preferably -0.3 or greater, even more preferably -0.2 or greater, and most preferably -0.2 to 3. The upper limit of the log P value depends on the solubility of the crosslinker in the Bore solution, which in turn depends on the nonsolvent or nonsolvent mixture used, the crosslinker used, and the concentration of the crosslinker. It is preferable to use a combination in which the crosslinker is completely soluble in the Bore solution.

[0070] As used in the present specification, examples, and claims, log P refers to the partition coefficient calculated after inputting the structural formula of each compound into the program ChemDraw Prime version 15.1.0.144 (© 1998-2016 PerkinElmer Informatics, Inc.). ChemDraw Prime version 15.1.0.144 calculates three different log P values. The log P values ​​described in the present specification, examples, and claims were calculated using the Crippen fragmentation method (J. Chem. Inf. Comput. Sci., Vol. 27, p. 21 (1987)) with ChemDrawPrime version 15.1.0.144. The log P ranges described above and in the claims are specified with respect to the log P values ​​calculated with ChemDraw Prime version 15.1.0.144, ignoring standard deviations.

[0071] A non-limiting list of preferred crosslinkers (a2.i) with an octanol-water partition coefficient log P of -0.5 or greater is shown in Table 1 below. This table should not be construed as limiting the scope of application to the listed crosslinkers. Other amine-based crosslinkers with log P values ​​within the specified ranges above can also be used. The log P values ​​shown in Table 1 are calculated after entering the structural formula of each compound using the program ChemDraw Prime version 15.1.0.144 (© 1998-2016 PerkinElmer Informatics, Inc.).

[0072] [Table 1]

[0073] Particularly preferred are embodiments in which the crosslinker (a2.i) has an octanol-water partition coefficient log P of −0.5 or more, preferably −0.4 or more, more preferably −0.3 or more, even more preferably −0.2 or more, and most preferably −0.2 to 3, and is selected from the group defined in the “Preferred embodiments of the present invention” above.

[0074] 1,6-Hexamethylenediamine, 1,7-Heptamethylenediamine, 1,8-Octamethylenediamine, 1,9-Nonamethylenediamine, 1,10-Decamethylenediamine, 1,11-Undecamethylenediamine, 1,12-Dodecamethylenediamine, 1,3-Cyclohexanebis(methylamine), 2,2,4-Trimethylhexane-1,6-diamine, 2,4,4-Trimethylhexane-1,6-diamine, 2-Methylpentanediamine, Isophoronediamine(3,5,5-trimethylhexane-1,6-diamine), Trimethyl-3-aminomethyl-cyclohexylamine), 4,4'-diaminodicyclohexylmethane, 2,4'-diaminodicyclohexylmethane, 2,2'-diaminodicyclohexylmethane, its isomers alone or in mixture, 3,3'-dimethyl-4,4'-diaminodicyclohexylmethane, N-cyclohexyl-1,3-propanediamine, 1,2-diaminocyclohexane, TCD-diamine (3(4),8(9)-bis(aminomethyl)tricyclo[5.2.1.0 2,6 It is further preferred to use crosslinkers (a2.i) selected from the group consisting of decane), xylylenediamine, aromatic amines, o-, m- or p-phenylenediamine, trimethylphenylenediamine, 4,4'-diaminodiphenylmethane, mixtures of the mentioned diamines.

[0075] Most preferably, crosslinkers (a2.i) are used that are selected from the group consisting of 1,6-hexamethylenediamine, 1,7-heptamethylenediamine, 1,8-octamethylenediamine, 1,9-nonamethylenediamine, 2,2,4-trimethylhexane-1,6-diamine, 2,4,4-trimethylhexane-1,6-diamine, decane-1,10-diamine, dodecane-1,12-diamine, 2-methylpentanediamine, 1,3-cyclohexanebis(methylamine), mixtures of the diamines mentioned.

[0076] The crosslinking agent (a2.i) has at least two amino groups. They may contain primary, secondary or tertiary amino groups, or a mixture thereof. Primary and secondary amino groups are preferred. Most preferably, they contain at least one primary amino group.

[0077] According to the present invention, the solvent or solvent mixture (a1.ii) for the polymer (a1.i) preferably comprises a polar aprotic solvent. Suitable polar aprotic solvents are well known in the art and are preferably selected from the group consisting of dimethyl sulfoxide (DMSO), dimethylformamide (DMF), dimethylacetamide (DMA), N-methylpyrrolidone (NMP), N-ethylpyrrolidone, sulfolane, and tetrahydrofuran (THF). The solvent for the polymer may also be a mixture of these polar aprotic solvents.

[0078] Preferably, the solvent or solvent mixture (a1.ii) for polymer (a1.i) comprises 60 to 100% by weight, preferably 70 to 100% by weight, of a polar aprotic solvent, relative to the total weight of the solvent mixture. The polar aprotic solvent may be mixed with 0 to 40% by weight, preferably 0 to 30% by weight, of a non-solvent for polymer (a1.i), relative to the total weight of the mixture, while still maintaining the ability to dissolve polymer (a1.i).

[0079] According to the present invention, the non-solvent or non-solvent mixture (a2.ii) for the polymer (a1.i) preferably comprises a protic solvent. Such solvents are well known in the art and are preferably selected from the group consisting of water, C1-C6 alkanols (e.g., ethanol), C2-C6 alkanediols (e.g., ethylene glycol), C3-C12 alkanetriols (e.g., glycerol), C4-C20 polyols (e.g., pentaerythritol, ditrimethylolpropane, diglycerol, ditrimethylolethane, trimethylolethane, trimethylolpropane, trimethylolbutane, pentaerythritol, dipentaerythritol, tripentaerythritol, and sorbitol), and hydrophilic, preferably water-soluble, polymers or copolymers (e.g., polyalkylene polyols and polyvinylpyrrolidone). The non-solvent may also be a mixture of non-solvents. Most preferred is water or a mixture of a non-solvent and water.

[0080] Preferred polyalkylene polyols are those derived from C2-C4 alkylene glycols, which are selected from the group consisting of polyethylene glycol (PEG), polypropylene glycol (PPO), EO-PO diblock polymers, EO-PO triblock polymers, mixed poly(ethylene-propylene glycol) polymers, and mixed poly(ethylene-butylene glycol) polymers. More preferred hydrophilic polymers or copolymers of C2-C4 alkylene glycols are those having a number average molecular weight of 200 to 5,000, more preferably 400 to 3,000, and particularly 400 to 2,000. Most preferably, the hydrophilic block is PEG. Exemplary hydrophilic blocks are PEG200, PEG400, and PEG6oo.

[0081] Preferably, the non-solvent or non-solvent mixture (a2.ii) comprises 60 to 100% by weight, more preferably 70 to 100% by weight, of a protic solvent, based on the total weight of the non-solvent mixture. The protic solvent may be mixed with 0 to 40% by weight, more preferably 0 to 30% by weight, of a polymer (a1.i) solvent, based on the total weight of the non-solvent mixture, while still maintaining the ability to dissolve the polymer (a1.i).

[0082] According to the present invention, the non-solvent for the polymer is preferably miscible with the solvent for the polymer.

[0083] The method according to the present invention is based on liquid-induced phase separation. Generally, in such a method, a polymer solution and a non-solvent (preferably a non-solvent that is miscible with the polymer's solvent) are co-extruded through a multi-orifice die, and upon contact between the polymer solution and the non-solvent, the solvent is driven out of the polymer phase, and at a certain non-solvent concentration, the polymer becomes solid.

[0084] The method of the present invention can be carried out using various spinnerets, i.e., double-orifice spinnerets, triple-orifice spinnerets, or four-orifice spinnerets. Such spinnerets are known in the art and are disclosed, for example, in WO 93 / 12868 and WO 2007 / 007051, which are incorporated herein by reference. In a double-orifice spinneret, phase a1 is typically extruded through the outer annular orifice, and phase a2 is extruded through the central annular orifice. In a triple-orifice spinneret, phase a1 is extruded through the middle orifice, and phase a2 is extruded through the central and / or outer annular orifices, preferably the outer annular orifices. Similarly, triple-layer hollow fiber membranes can also be produced using a quadruple-orifice spinneret.

[0085] According to a preferred embodiment of the present invention, the phase (a1) composition comprises a polymer (a1.i) and a solvent (a1.ii) for this polymer, while the phase (a2) composition comprises an amine-based crosslinker (a2.i) having at least two amino groups, preferably an aliphatic or aromatic amine having at least two amino groups, and a non-solvent (a2.ii) for the polymer (a1.i).

[0086] According to another preferred embodiment of the present invention, the phase (a1) composition comprises a polymer (a1.i) and a solvent mixture (a1.ii) for this polymer, while the phase (a2) composition comprises an amine-based crosslinker (a2.i) having at least two amino groups, preferably an aliphatic or aromatic amine having at least two amino groups, and a non-solvent (a2.ii) for the polymer (a1.i). In this second embodiment of the present invention, the solvent mixture (a1.ii) for the polymer (a1.i) comprises, relative to the total weight of the solvent mixture, 60% to 100% by weight, more preferably 70% to 99.9% by weight of the solvent for the polymer (a1.i) and 0% to 40% by weight, more preferably 0.1% to 30% by weight of the non-solvent for the polymer (a1.i).

[0087] According to a further preferred embodiment of the present invention, the phase (a1) composition comprises a polymer (a1.i) and a solvent mixture (a1.ii) for this polymer, while the phase (a2) composition comprises an amine-based crosslinker (a2.1) having at least two amino groups, preferably an aliphatic or aromatic amine having at least two amino groups, and a non-solvent mixture (a2.ii) for the polymer (a1.i). In this preferred embodiment of the present invention, the solvent mixture (a1.ii) in phase (a1) preferably comprises, based on the total weight of the solvent mixture, 60% to 100% by weight, more preferably 70% to 99.9% by weight of a solvent for the polymer (a1.1) and 0% to 40% by weight, more preferably 0.1% to 30% by weight of a non-solvent for the polymer (a1.1). The non-solvent mixture (a2.ii) of the phase (a2) composition preferably comprises from 60% to 100% by weight, more preferably from 70% to 99.9% by weight, of non-solvent for polymer (a1.i) and from 0% to 40% by weight, more preferably from 0.1% to 30% by weight, of solvent for polymer (a1.i), relative to the total weight of the non-solvent mixture.

[0088] According to yet another preferred embodiment of the present invention, the phase (a1) composition comprises a polymer (a1.i) and a solvent (a1.ii) for the polymer, while the phase (a2) composition comprises an amine-based crosslinker (a2.i) having at least two amino groups, preferably an aliphatic or aromatic amine having at least two amino groups, and a non-solvent mixture (a2.ii) for the polymer (a1.i). The non-solvent mixture (a2.ii) of the phase (a2) composition preferably comprises, based on the total weight of the non-solvent mixture, 60% to 99.9% by weight, more preferably 70% to 99.9% by weight, of a non-solvent for the polymer (a1.i) and 0.1% to 40% by weight, more preferably 0.1% to 30% by weight, of a solvent for the polymer (a1.i).

[0089] Thus, the present invention includes the following options: Phase (a1) composition: polymer (a1.i) + solvent for polymer (a1.i); Phase (a2) composition: amine-based crosslinker (a2.i) having at least two amino groups, preferably an aliphatic or aromatic amine having at least two amino groups + non-solvent for polymer (a1.i). Phase (a1) composition: polymer (a1.i) + solvent for polymer (a1.i) + non-solvent for polymer (a1.i); Phase (a2) composition: amine-based crosslinker (a2.i) having at least two amino groups, preferably an aliphatic or aromatic amine having at least two amino groups + non-solvent for polymer (a1.i). Phase (a1) composition: polymer (a1.i) + solvent for polymer (a1.i); Phase (a2) composition: amine-based crosslinker (a2.i) having at least two amino groups, preferably an aliphatic or aromatic amine having at least two amino groups + solvent for polymer (a1.i) + non-solvent for polymer (a1.i). Phase (a1) composition: polymer (a1.i) + solvent for polymer (a1.i) + non-solvent for polymer (a1.i); Phase (a2) composition: amine-based crosslinker (a2.i) having at least two amino groups, preferably an aliphatic or aromatic amine having at least two amino groups + solvent for polymer (a1.i) + non-solvent for polymer (a1.i).

[0090] A dual-orifice spinneret is shown diagrammatically in Figure 1. When the method according to the invention is carried out using a dual-orifice spinneret, phase (a1) is extruded through the outer annular orifice (1), while phase (a2) is coextruded through the central annular orifice (2). The outer diameter of the dual-material die is preferably in the range of 500 µm to 800 µm, more preferably in the range of 550 µm to 750 µm, the inner diameter is preferably in the range of 200 µm to 400 µm, more preferably in the range of 250 µm to 350 µm, and the pump speed is preferably in the range of 0.1 mL / min to 13.5 mL / min.

[0091] A triple orifice spinneret is shown diagrammatically in Figure 2. When the method according to the invention is carried out with a triple orifice spinneret, the following options are preferred.

[0092] Phase (a1) is extruded through the middle annular orifice (1), phase (a2) is coextruded through the outer annular orifice (3), and the non-solvent is coextruded through the central annular orifice (2).

[0093] Phase (a1) is extruded through the middle annular orifice (1), phase (a2) is coextruded through the central annular orifice (2), and the non-solvent is coextruded through the outer annular orifice (3).

[0094] Phase (a1) is extruded through the middle annular orifice (1) and phase (a2) is co-extruded through the central annular orifice (2) and the outer annular orifice (3).

[0095] Phase (a1) is extruded through the middle annular orifice (1), phase (a2) is coextruded through the outer annular orifice (3), and an inert gas, steam or inert liquid is coextruded through the central annular orifice (2).

[0096] Phase (a1) is extruded through the middle annular orifice (1), phase (a2) is coextruded through the central annular orifice (2), and an inert gas, steam or inert liquid is coextruded through the outer annular orifice (3).

[0097] According to a preferred embodiment of the present invention, the phase (a1) composition comprises a total of about 15% to 35% by weight, preferably 20% to 30% by weight, more preferably 22% to 30% by weight, and even more preferably 22% to 29% by weight of polymer (a1.i), based on the total weight of the phase (a1) composition. The remainder of phase (a1) is preferably a solvent / solvent mixture (a1.ii) for polymer (a1.i), and, if necessary, other components, such as non-solvents, that promote coagulation. It has been found that an increased content of polymer (a1.i) in phase (a1) is beneficial for obtaining more selective membranes. However, too high a content can lead to excessive viscosity, which can interfere with filtration.

[0098] According to a preferred embodiment of the present invention, the phase (a2) composition comprises a total of about 0.1% to 30% by weight, preferably 0.5% to 20% by weight, more preferably 1% to 10% by weight, even more preferably 2% to 8% by weight of an amine-based crosslinker having at least two amino groups, more preferably an aliphatic or aromatic amine, and 70% to 99.9% by weight, preferably 80% to 99.5% by weight, more preferably 90% to 99% by weight, even more preferably 92% to 98% by weight of the non-solvent or non-solvent mixture (a2.ii) in phase (a2), based on the total weight of the mixture of amine-based crosslinker (a2.i) and non-solvent or non-solvent mixture (a2.ii) in phase (a2). This non-solvent mixture (a2.ii) contains, relative to the total weight of the non-solvent mixture (a2.ii), 1% to 99% by weight, preferably 10% to 95% by weight, more preferably 30% to 90% by weight, even more preferably 50% to 80% by weight of a solvent for the polymer (a1.i) and 1% to 99% by weight, preferably 5% to 90% by weight, more preferably 10% to 70% by weight, even more preferably 20% to 50% by weight of a non-solvent for the polymer (a1.i). The amounts of solvent and non-solvent are selected from the above ranges so that the sum of the solvent and non-solvent amounts to 100% by weight of the non-solvent mixture. Phase (a2) may contain only the amine-based crosslinker (a2.i) having at least two amino groups and the non-solvent or non-solvent mixture (a2.ii), or it may contain additional components such as additives.

[0099] Prior to spinning, it is preferred to devolatilize and filter the solution, and, if necessary, add additives to phase (a1). More preferably, phase (a1) is thermostatically controlled at a temperature of preferably 20°C to 100°C, more preferably 30°C to 70°C. The solution is then pumped, for example, through a die using a gear pump. Devolatilization is particularly important to obtain a defect-free membrane.

[0100] The preferred distance between the spinning die and the precipitation bath in step (b), where the hollow fibers are spun and the polymer is precipitated to form a completely asymmetric hollow fiber membrane, is 1 cm to 1 m, preferably 5 cm to 60 cm.

[0101] The solvent evaporates on the outer surface of the membrane between the spinning die and the precipitation bath, resulting in densification of the layer in step (b) and the formation of a separation layer upon precipitation in the precipitation bath. The thickness of the separation layer can be adjusted via the distance from the spinning die to the precipitation bath and the atmosphere of the membrane between the spinning die and the precipitation bath.

[0102] In a preferred embodiment, the membrane obtained by the method of the present invention has high gas permeability, i.e., permeance. For this reason, the membrane should not have an excessively thick and / or dense separating layer. Therefore, during the spinning process, it is preferred that the hollow fiber after step (a) and before entering the precipitation bath in step (b) be exposed to a dry thermostatic flow of gas or air and / or pass through a corresponding gas or air atmosphere. It is particularly preferred that the membrane be passed through a gas or air flow. Drying should be understood to mean that the gas or air flow is capable of absorbing water. Therefore, it is preferred that the air or gas flow contains a moisture content of 0% to 90% relative humidity, preferably 0% to 50% relative humidity, and more preferably 0% to 30% relative humidity, at the specified air / gas temperature.

[0103] It is very particularly preferred that the hollow fibers emerging from the die after step (a) enter a shaft (tube, chimney) filled with dry thermostatic gas. Useful gases are nitrogen, air, argon, helium, carbon dioxide, methane, or other industrial inert gases. The gas temperature is regulated by a heat exchanger and is preferably between 20°C and 250°C, more preferably between 25°C and 120°C, and most preferably between 30°C and 80°C.

[0104] The gas velocity in the tube is preferably 0.1 m / min to 10 m / min, more preferably 0.3 m / min to 5 m / min, even more preferably 0.5 m / min to 3 m / min, and most preferably 0.5 m / min to 2 m / min. The length of the tube is preferably between 1 cm and 1 m, more preferably between 2 cm and 50 cm, even more preferably between 5 cm and 40 cm, and most preferably between 5 cm and 30 cm. The length of the shaft, gas velocity, and temperature all affect the actual separating layer thickness of the membrane.

[0105] As mentioned above, the choice of amine-based crosslinker (a2.i) influences the membrane structure and the layer structure. For the production of fully asymmetric membranes with an outer separating layer, it is particularly preferred to use less polar and less water-soluble amine-based crosslinkers (a2.ii), as defined above as preferred crosslinkers. Such crosslinkers preferably diffuse from the bore solution into the wall pores of the hollow fiber membrane and then more uniformly into the polymer. On the other hand, the more polar and water-soluble amine-based crosslinkers used in the prior art preferably remain in the bore solution and then diffuse only into the polymer near the bore.

[0106] The spun and preferably conditioned fibers from step (a) are then immersed in a precipitation bath in step (b) to coagulate the polymer mass and thus form a membrane. The bath temperature is preferably between 1°C and 80°C, more preferably between 20°C and 70°C, and most preferably between 40°C and 65°C.

[0107] The concentration of aprotic dipolar solvents and other solvents (e.g., dimethylformamide, dimethylacetamide, N-methylpyrrolidone, N-ethylpyrrolidone, sulfolane, dimethyl sulfoxide, tetrahydrofuran, dioxane, isopropanol, ethanol, or glycerol, but not limited to these) in the precipitation bath is preferably between 0.01% and 20% by weight, more preferably between 0.1% and 10% by weight, and most preferably between 0.2% and 1% by weight, with the remainder being water. Similarly, it is preferable to use pure water for the water bath.

[0108] The take-up speed of the hollow fiber is preferably between 2 m / min and 100 m / min, more preferably between 10 m / min and 80 m / min, and most preferably between 30 m / min and 70 m / min. It has been found that if the take-up speed is too high, permeance is lost. Nevertheless, the preferred process of the present invention may be preferably operated at a high take-up speed to achieve improved productivity compared to the prior art.

[0109] The fibers are preferably washed at a point downstream of the precipitation bath until the residual solvent content is less than 1% by weight, preferably 0.5% by weight or less. Various washing techniques can be used for this. It is preferred to use a continuous process in which the fibers pass through one or more successive water baths. To achieve more effective washing, it is particularly preferred to heat the water baths to 40-90°C, preferably 50-80°C.

[0110] However, the fibers obtained from the precipitation bath can also be wound up and washed with water in an off-line manner. Washing can be carried out at any temperature. However, as mentioned above, it is preferred that relatively high temperatures be used for washing. It is preferred that the water be applied perpendicular to the fiber, i.e., flowing from the inner surface of the fiber to the outer surface.

[0111] This is preferably followed by a solvent exchange (more preferably in isopropanol and / or hexane) to remove water and DMF. Solvent exchange can be performed in a continuous operation (online) or offline, like washing. In the case of online solvent exchange, the fiber is guided through one or more solvent baths, preferably downstream of a washing bath.

[0112] The fibers are then dried in step (c), preferably at a temperature ranging from room temperature to 150°C, more preferably between 50 and 100°C, to remove the isopropanol and hexane. The overall moisture and / or residual solvent content after drying is preferably in the range of 0% to 5% by weight, preferably less than 3% by weight, more preferably in the range of 0.1% to 3% by weight, and preferably consists solely of water, isopropanol, and hexane fractions.

[0113] Too much water can lead to hydrolysis, chain scission, and mechanically unstable films. Although some of the water and solvent evaporates during annealing, the maximum content before the start of annealing has been found to be advantageously less than 5 wt. %, preferably less than 3 wt. %.

[0114] In step (d), the hollow fiber membrane obtained in step (c) is subjected to a heat treatment at an annealing temperature of 150 to 280°C, preferably 160 to 270°C, more preferably 160 to 260°C, even more preferably 170 to 250°C, particularly preferably 170 to 240°C, and most preferably 180 to 230°C. The conditions during the heat treatment can be varied depending on the properties required for the membrane. If the annealing temperature is too low or too high, the degree of crosslinking, i.e., insolubility in DMF, will be very low. If a very high degree of crosslinking, and therefore chemical stability, is desired, the optimum annealing temperature for step (d) of the method according to the invention has been found to be in the range of 180-230°C.

[0115] Furthermore, it has been found that if the annealing temperature during step (d) is too high, the mechanical stability of the membrane, in particular the elongation at break, deteriorates.

[0116] The gas selectivity and permeability of the membrane can be influenced and controlled by selecting an appropriate annealing temperature in step (d): a higher annealing temperature leads to better selectivity but lower permeability.

[0117] The examples provided below will make clear to one skilled in the art how variations affect product properties and how those properties can be established.

[0118] The temperature treatment time in step (d) (the time from when the target temperature is reached) has a small effect on the membrane performance compared to the annealing temperature. Regardless, as shown in the examples, some properties such as gas selectivity, permeance, and insolubility can also be influenced and controlled by the time of the heat treatment in step (d). Preferably, the heat treatment in step (d) is carried out for 15 to 300 minutes, preferably 30 to 240 minutes, even more preferably 30 to 90 minutes, and most preferably 60 to 90 minutes.

[0119] The heating rate selected to achieve the heat treatment temperature in step (d) is preferably in the range of 0.1-10°C / min, more preferably 1-5°C / min, and most preferably 1-2°C / min, from about 35°C to ensure uniform annealing throughout the membrane bundle and simultaneous arrival of the final temperature. In particular, for simultaneous annealing of large numbers of fibers, a relatively slow heating rate is advantageous to ensure uniform annealing of the fibers.

[0120] The annealing temperature, i.e., the atmosphere surrounding the membrane at a distance of up to 10 cm, preferably 2-10 cm, is measured with three or more sensors, preferably thermocouples. The distances specified relate to the distance from the outer surface of the membrane when only one membrane is annealed. When two or more membranes are annealed simultaneously, for example, in a membrane bundle or membrane stack arrangement, the distance relates to the distance from the outer surface of the outermost membrane (i.e., the distance from the outer surface of the membrane bundle) or to the distance to another membrane arrangement.

[0121] It has been found that the mechanical properties of the films and in particular their productivity are particularly good if the oxygen content of the atmosphere surrounding the film at a distance of up to 10 cm, preferably 2-10 cm, does not exceed a certain maximum value during annealing. It is therefore preferable to carry out the heat treatment at an oxygen content of not more than 0.5% by volume, preferably not more than 0.25% by volume, even more preferably not more than 0.1% by volume, and even more preferably not more than 0.01% by volume.

[0122] Particularly good results are obtained when the films are annealed not only in a vacuum but also in a gas atmosphere or gas flow with a correspondingly low oxygen content. Without being bound by any theory, the inventors believe that the gas atmosphere and / or gas flow ensures a uniform temperature distribution within the film bundle to be annealed, i.e., uniform annealing of all films.

[0123] Therefore, it is preferred that the film is surrounded by an atmosphere with a corresponding low oxygen content during annealing, preferably at least in the first stage of cooling, more preferably from the start of annealing and / or until the end of the cooling process. It is particularly preferred that the film is exposed to a flow of a gas or gas mixture or a gas stream or gas mixture with the above-mentioned low oxygen content during the above-mentioned stages, more preferably at least one inert gas (e.g., a noble gas, nitrogen, or sulfur hexafluoride), even more preferably nitrogen. It is most preferred to use a corresponding gas stream. During cooling, i.e., as soon as the temperature drops completely below the maximum annealing temperature, a vacuum can also be applied.

[0124] It is particularly preferred if, after starting cooling to a temperature below 150° C., the atmosphere surrounding the membrane at a distance of up to 10 cm, preferably 2 to 10 cm, corresponds to the above-mentioned gas atmosphere and / or vacuum. At lower temperatures, especially below 150° C., the membrane has such low reactivity that contact with an oxygen-rich atmosphere usually does not cause any damage.

[0125] Cooling of the film after the heat treatment step (d) can be carried out "passively", i.e., by turning off the heat source. However, it is particularly preferred that the fully annealed film is "actively" cooled, for example, by flushing an oven or by contacting the film with a suitably temperature-controlled inert gas having an O content as specified below. However, cooling with a heat exchanger and / or a cooling circuit is also preferred instead. Further technical alternatives for achieving adequate cooling are known to those skilled in the art and are encompassed by the present invention. Active cooling increases the space-time yield and reduces the risk of still suffering from undesired deterioration of the film properties during cooling.

[0126] In the process of the present invention, it may be preferable to treat the membrane after drying with a silicone-type elastomer (e.g., Sylgard® 184) to repair possible defects. Another embodiment of the present invention is a hollow fiber membrane obtainable by the process according to the present invention. The fibers of the present invention are preferably fully asymmetric hollow fiber membranes.

[0127] The degree of crosslinking of the polymers in the fibers can be controlled, but is preferably very high. It can be measured by immersing the membrane in DMF at 25°C for 24 hours under stirring. The undissolved material is filtered, dried, and weighed. Undissolved material corresponds to a degree of crosslinking of 100%, and complete dissolution corresponds to a degree of crosslinking of 0%. Preferably, the membranes of the present invention have a degree of crosslinking of at least 85%, more preferably 90-100%, and even more preferably 95-100%.

[0128] The crosslinked hollow fiber membrane of the present invention is a polymer selected from the group consisting of polyimides, copolyimides, block copolyimides, polyetherimides, polyamideimides, or mixtures or blends thereof; an amine-based crosslinker having at least two amino groups, preferably an aliphatic or aromatic amine; The hollow fibers have a densely crosslinked outer layer and a homogeneous, crosslinked inner support layer. By "homogeneous, crosslinked inner support layer," we mean that, at 300x magnification, only one layer is visible in a scanning electron microscope image of the front surface of the hollow fiber, between the dense outer layer, which is invisible at that magnification, and the inner surface of the hollow fiber. An example of a membrane according to the present invention having a homogeneous support layer is shown in Figure 3b, while a membrane with a heterogeneous inner layer structure (i.e., a membrane with two visible inner layers and a clearly visible dividing line between the two layers) is shown in Figure 3a. The structure according to Figure 3a has poor mechanical stability due to weak bonding between the two layers at the visible dividing line. Membranes of the present invention having a homogeneous structure are advantageous in terms of their mechanical stability. Furthermore, hollow fibers of the present invention having a crosslinked inner layer (i.e., having not only a dense outer layer but also an inner layer) are crosslinked and therefore highly insoluble.

[0129] The preferred polymers and amine-based crosslinking agents that may be contained in the crosslinked hollow fiber membrane of the present invention are those defined above as preferred embodiments of the method of the present invention.

[0130] The crosslinked hollow fiber membranes of the present invention are preferably fully asymmetric hollow fiber membranes, which can be obtained by the method according to the present invention.

[0131] The hollow fiber membranes of the present invention are particularly useful in gas separation processes, vapor separation processes, and liquid filtration processes.

[0132] Analysis method transparency The gas permeance of the hollow fiber membrane is expressed as GPU (gas permeance unit, 10 -6 cm 3. cm -2 .s -1 .cmHg -1 ) to report. (Because the thickness of the separation layer is unknown) Calculate the permeance P / l using the following formula:

number

[0133] P / l: Permeance in GPU (gas permeance units). 10 -6 cm 3. cm -2 .s -1 .cmHg -1 ) Q: Permeation gas flux (cm 3 (STP) / s) R: Gas constant (cm 3 .cmHg.K -1 .mol -1 ) T: Temperature in Kelvin (room temperature, ~23°C) A: External area of ​​hollow fiber (cm 2 )(60~80cm 2 ) Δp: Pressure difference between the feed side and the permeate side (cmHg) dp / dt: Pressure increase per unit time on the permeate side (cmHg.s -1 )

[0134] The selectivity of various gas pairs is the selectivity of the pure gases. The selectivity between two gases is calculated from the ratio of the permeabilities:

number

[0135] S: Ideal gas selectivity P1: Permeability or permeance of gas 1 P2: Permeability or permeance of gas 2

[0136] Residual solvent content measurement Residual solvents (e.g., isopropanol, hexane) are determined by gas chromatography by headspace injection of the polymer dissolved / dispersed in 1,3-dimethyl-3,4,5,6-tetrahydro-2(1H)-pyrimidinone (DMPU). Accurately weigh 250-300 mg of sample to the nearest 0.1 mg (= initial weight) into a pre-weighed vial. Next, add 5.00 mL of DMPU using a full pipette or dispenser, and seal the vial with a septum using a cap crimper. Thermostat the sample at 120 °C in the headspace sampler for 90 minutes, then inject the headspace onto the GC column. Residual DMF in wet hollow fiber samples is measured by Soxhlet extraction in ethanol. Subsequent quantification is by direct injection of the extract into GC. Residual DMF in dried hollow fiber samples is measured using headspace GC. GC: Perkin Elmer AutoSystem XL Column: Perkin Elmer WAX ETR, 30m x 0.53mm, df=2.00μm, #N931-6570 Headspace autosampler: Perkin Elmer TurboMatrix 40 Carrier gas: 5 mL Helium 4.6 (or higher) FID detection gas: 40 mL / min hydrogen, 400 mL / min synthetic air GC temperature program: Initial temperature: 175°C for 3 minutes Ramp 1: 20°C / min to 230°C for 3 min Run Time: 8.75 minutes Cycle time: 15 minutes

[0137] After analysis, the residual solvent content is automatically calculated according to the formula below and output as "concentration (%)".

number

[0138] Residual moisture measurement The residual water content is measured by extracting the membrane with isopropanol and analyzing it by Karl Fischer titration. The membrane is transferred to a pre-dried 250 mL Schott glass and covered to the top with weighed dry isopropanol. The container is left at room temperature overnight.

[0139] Tensile strength and elongation at break Tensile strength and elongation at break are tested using a Zwick Z050 static materials testing machine. The values ​​obtained are the average of 10 readings from 10 individual hollow fibers. The parameters set are as follows: [Table 2]

[0140] Tensile strength is recorded when the elongation is no longer linear with applied load. Elongation at break is recorded as the change in length of the hollow fiber before it breaks. [Brief explanation of the drawings]

[0141] [Figure 1] FIG. 1 is a schematic diagram of a dual orifice spinneret. [Figure 2] FIG. 2 is a schematic diagram of a triple orifice spinneret. [Figure 3a] FIG. 3a shows a membrane with a heterogeneous inner layer structure (ie, a membrane with two visible inner layers and a clearly visible dividing line between the two layers). [Figure 3b] FIG. 3b shows a membrane according to the invention with a homogeneous support layer. [Example]

[0142] The following experimental examples are intended to explain and describe the present invention in more detail, but should not be construed as limiting the present invention in any way.

[0143] Chemicals used Polymers (a1.i): PI 1: P84 HT prepared according to Example 7 of WO 2011 / 009919 Co-PI: A block copolyimide having the following was prepared according to Example 40 of WO 2015 / 091122 with a block ratio of 80:20 instead of 75:25: - Block A: BTDA / PMDA-TDI - Block B: BTDA / PMDA-MesDA - A:B ratio = 80:20 Crosslinker (A2.i): [Table 3]

[0144] solvent: DMF: dimethylformamide obtained from BASF. Non-solvent: water

[0145] Experimental Example 1: General description of membrane production method To produce the phase (a) solution, polymer (a1.i) was dissolved in a solvent. The solution was degassed, thermostated at 50 °C, and pumped by a gear pump through a bi-component die. The flow rate was 324 g / h. While the polymer solution (a1) was transported to the outer region of the bi-component die, phase (a2), consisting of a non-solvent (a2.ii) for polymer (a1.i) and a diamine crosslinker (a2.1), was transported to the inner region as a bore solution to form the hollow fiber. The bore solution flow rate was 120 mL / h. After being placed 13 cm from the die, the hollow fiber entered a coagulation bath containing hot water at 50 °C. The hollow fiber traveled from the die to the precipitation bath through a tube. This tube was filled with a nitrogen flow at 0.90 mL / min, and the internal temperature of the tube was 35 °C. The fiber was transported through a water wash bath and finally wound up at a speed of 40 m / min. After extraction with water for several hours, the hollow fibers were immersed in isopropanol. After solvent exchange, the membranes were introduced into a drying zone at 70 °C and dried within approximately 50 seconds. The resulting membranes were heated to the desired annealing temperature in a vacuum of 30 mbar (absolute) (N flush, O content: less than 0.001% by volume) and subsequently left at the final temperature for the desired time. The materials used as polymer (a1.i), diamine crosslinker (a2.i), solvent (a1.ii), non-solvent (a2.ii), the composition of phases (a1) and (a2), the annealing temperature, and the annealing time are shown in each of the following examples and comparative examples.

[0146] Experimental Example 2: Effect of the amount of diamine crosslinker (a2.i) on the degree of crosslinking of the membrane (insolubility in DMF) Hollow fiber membranes were fabricated according to Example 1, according to the parameters listed in Table 4. [Table 4]

[0147] The analysis results in Table 4 show that the degree of crosslinking can be varied over a wide range by the method of the present invention.

[0148] Experimental Example 3: Effect of the polarity of diamine crosslinker (a2.i) and annealing temperature on the structure and properties of the film Hollow fiber membranes were fabricated according to Example 1, according to the parameters listed in Table 5. [Table 5]

[0149] The results in Table 5 show that when polyethyleneimine with a very low log P value is used as the crosslinker, the degree of crosslinking after annealing is comparable. However, when TMD with a high log P value is used as the crosslinker, the method of the present invention allows for flexible adjustment of the degree of crosslinking. Furthermore, as shown in Figure 3a, when polyethyleneimine was used as a cross-linker, a dense inner layer formed near the lumen surface of the hollow fiber. This structure could be at risk of fracture and could lead to membrane delamination. When TMD, the preferred cross-linker, was used, the formation of the dense inner layer could be avoided, resulting in a homogeneous membrane, as shown in Figure 3b. Table 5 also shows that the use of crosslinkers with high log P values ​​leads to hollow fiber membranes with excellent mechanical properties after heat treatment of the crosslinked membrane. As shown below, heat treatment is necessary to obtain good membrane selectivity.

[0150] Experimental Example 4: Effect of annealing temperature in step (d) on membrane performance and chemical and mechanical stability Hollow fiber membranes were prepared according to Example 1, according to the parameters listed in Table 6. [Table 6]

[0151] The results in Table 6 show the effect of the annealing temperature in step (d). Increasing the temperature improves selectivity and tensile strength, but increasing the annealing temperature decreases permeance and elongation. For chemical resistance (insolubility in DMF), a temperature of 200-250°C is optimal.

[0152] Experimental Example 5: Effect of annealing time in step (d) on film performance and chemical and mechanical stability Hollow fiber membranes were prepared according to Example 1, according to the parameters listed in Table 7. [Table 7]

[0153] Table 7 shows that the annealing duration in step (d) has a slight effect on the film properties.

[0154] Experimental Example 6: Comparison of the effect of different crosslinkers (a2.i) on the mechanical properties and chemical resistance of the obtained films Hollow fiber membranes were prepared according to Example 1, according to the parameters listed in Tables 8.1 to 8.6. [Table 8.1] [Table 8.2] [Table 8.3] [Table 8.4] [Table 8.5] [Table 8.6]

[0155] Tables 8.1 to 8.6 show that the method according to the present invention, in which chemical crosslinking occurs during the phase invention step (step (a) hollow fiber formation), allows the crosslinking process to be controlled by selecting the crosslinker according to its polarity. The use of amine-based crosslinkers with higher log P values ​​(greater than -0.5), lower polarity, and lower water solubility allows for better control of the crosslinking process. The degree of crosslinking can be further improved by moderate heat treatment at temperatures between 150 and 250°C.

Claims

1. (a) the steps of: (a1) extruding through an orifice of a hollow fiber die a phase (a1) composition comprising a polymer (a1.i) selected from the group consisting of polyimides, copolyimides, block copolyimides, polyetherimides, polyamideimides, or mixtures or blends thereof, and a solvent or solvent mixture (a1.ii) for said polymer (a1.i); (a2) co-extruding a phase (a2) composition comprising an amine-based crosslinker having at least two amino groups and a non-solvent or non-solvent mixture (a2.ii) of the polymer (a1.i) through the central orifice of the hollow fiber die and / or through the outer orifices of the hollow fiber die; A hollow fiber membrane spinning process comprising: (b) passing the hollow fiber membrane through a coagulation bath; (c) drying the hollow fiber membrane until all water is removed and / or the residual solvent content is 0% by weight to 5% by weight; (d) heat treating the hollow fiber membrane at an annealing temperature of 150°C to 280°C in a surrounding atmosphere having an oxygen content of 0.5% by volume or less.

2. 10. The method of claim 1, wherein the hollow fiber die is a dual orifice spinneret, a triple orifice spinneret, or a quadruple orifice spinneret.

3. The method of claim 2, wherein the double orifice spinneret, triple orifice spinneret, or quadruple orifice spinneret has an annular orifice.

4. 2. The method of claim 1, wherein the phase (a1) composition comprises a total of 15% to 35% by weight of the polymers (a1.i) relative to the total weight of the phase (a1) composition.

5. 2. The method of claim 1, wherein the phase (a2) composition comprises, based on the total weight of the phase (a2.i), a total of 0.1% to 30% by weight of an amine-based crosslinker (a2.i) having at least two amino groups.

6. 2. The method according to claim 1, wherein an amine-based crosslinking agent (a2.i) having at least two amino groups and an octanol / water partition coefficient (log P) of −0.5 or more is used.

7. The amine-based crosslinker (a2.i) having at least two amino groups is a carbon chain having 5 to 24 carbon atoms; a substituted or unsubstituted, linear or branched aliphatic amine containing 2 to 5 amino groups and having 6 to 30 carbon atoms; a substituted or unsubstituted cycloaliphatic amine having 6 to 24 carbon atoms and 2 to 5 primary amino groups; a substituted or unsubstituted aromatic or alkylaromatic amine having 6 to 24 carbon atoms and 2 to 5 primary amino groups; and mixtures thereof.

8. The method of claim 7, wherein the substituted or unsubstituted cycloaliphatic amine contains a heteroatom in the alkyl chain or as a bond between the aliphatic rings.

9. The method of claim 7 or 8, wherein the substituted or unsubstituted aromatic or alkylaromatic amine contains a heteroatom.

10. The amine-based crosslinking agent (a2.i) having at least two amino groups is selected from the group consisting of 1,6-hexamethylenediamine, 1,7-heptamethylenediamine, 1,8-octamethylenediamine, 1,9-nonamethylenediamine, 1,10-decamethylenediamine, 1,11-undecamethylenediamine, 1,12-dodecamethylenediamine, 2,2,4-trimethylhexane-1,6-diamine, 2,4,4-trimethylhexane-1,6-diamine, 2-methylpentanediamine, isophoronediamine (3 , 5,5-trimethyl-3-aminomethyl-cyclohexylamine), 4,4'-diaminodicyclohexylmethane, 2,4'-diaminodicyclohexylmethane, 2,2'-diaminodicyclohexylmethane, its isomers alone or in mixture, 3,3'-dimethyl-4,4'-diaminodicyclohexylmethane, N-cyclohexyl-1,3-propanediamine, 1,2-diaminocyclohexane, TCD-diamine (3(4),8(9)-bis(aminomethyl)tricyclo[5.2.1.0 ２，６ ]decane), xylylenediamine, aromatic amines, o-, m- or p-phenylenediamine, trimethylphenylenediamine, 4,4'-diaminodiphenylmethane, mixtures of the diamines listed.

11. 8. The method of claim 7, wherein the amine-based crosslinker (a2.i) having at least two amino groups is selected from the group consisting of aliphatic amines, 1,6-hexamethylenediamine, 1,7-heptamethylenediamine, 1,8-octamethylenediamine, 1,9-nonamethylenediamine, 2,2,4-trimethylhexane-1,6-diamine, 2,4,4-trimethylhexane-1,6-diamine, decane-1,10-diamine, dodecane-1,12-diamine, 2-methylpentanediamine, 1,3-cyclohexanebis(methylamine), mixtures of the diamines listed.

12. The method of claim 1 , wherein the solvent (a1.ii) for the polymer (a1.i) comprises a polar aprotic solvent.

13. The method of claim 12, wherein the polar aprotic solvent is selected from the group consisting of dimethyl sulfoxide, dimethylformamide, dimethylacetamide, N-methylpyrrolidone, N-ethylpyrrolidone, sulfolane, tetrahydrofuran, and mixtures thereof.

14. The method of claim 1 , wherein the non-solvent (a2.ii) for the polymer (a1.i) comprises a protic solvent.

15. The method of claim 14, wherein the protic solvent is selected from the group consisting of water, C1-C6 alkanols, C2-C6 alkanediols, C3-C12 alkanetriols, C4-C20 polyols, hydrophilic polymers or copolymers.

16. The method according to claim 1, wherein the heat treatment of the hollow fiber membrane in step d) is carried out at an annealing temperature of 160 to 270°C.

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