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WO2023195479A1 - Membrane de filtration et procédé de production de ladite membrane - Google Patents

Membrane de filtration et procédé de production de ladite membrane Download PDF

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Publication number
WO2023195479A1
WO2023195479A1 PCT/JP2023/014039 JP2023014039W WO2023195479A1 WO 2023195479 A1 WO2023195479 A1 WO 2023195479A1 JP 2023014039 W JP2023014039 W JP 2023014039W WO 2023195479 A1 WO2023195479 A1 WO 2023195479A1
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WIPO (PCT)
Prior art keywords
membrane
filtration membrane
polymer
hollow fiber
mol
Prior art date
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Ceased
Application number
PCT/JP2023/014039
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English (en)
Japanese (ja)
Inventor
秀人 松山
ラジャブザデ サイード
崇 佐々木
将智 高橋
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Kobe University NUC
NOF Corp
Original Assignee
Kobe University NUC
NOF Corp
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Priority to JP2024514287A priority Critical patent/JPWO2023195479A1/ja
Publication of WO2023195479A1 publication Critical patent/WO2023195479A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
    • B01D71/06—Organic material
    • B01D71/28—Polymers of vinyl aromatic compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
    • B01D71/06—Organic material
    • B01D71/30—Polyalkenyl halides
    • B01D71/32—Polyalkenyl halides containing fluorine atoms
    • B01D71/34—Polyvinylidene fluoride
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
    • B01D71/06—Organic material
    • B01D71/40—Polymers of unsaturated acids or derivatives thereof, e.g. salts, amides, imides, nitriles, anhydrides, esters

Definitions

  • the present disclosure relates to a filtration membrane (particularly a hollow fiber membrane filtration membrane) having both fouling resistance and water resistance, and a method for manufacturing the membrane.
  • hollow fiber membrane filtration membranes such as ultrafiltration, microfiltration, and reverse osmosis have been used in many industrial fields such as drinking water production, water supply and sewage treatment, and wastewater treatment. Furthermore, hollow fiber membrane filtration membranes are increasingly being used in biopharmaceutical fields such as artificial dialysis, blood products, and antibody drugs. Ultrafiltration membranes and microfiltration membranes, which are hollow fiber membrane filtration membranes, are widely used for water purification. However, the problem with hollow fiber membrane filtration membranes is that they are highly hydrophobic and easily foul.
  • Fouling refers to causative substances called foulants contained in raw water (e.g., poorly soluble components, proteins, polymeric solutes such as polysaccharides, colloids, minute solids, microorganisms, etc.) that deposit on membranes and reduce the permeation flow rate. This phenomenon is known as the main cause of membrane performance deterioration.
  • raw water e.g., poorly soluble components, proteins, polymeric solutes such as polysaccharides, colloids, minute solids, microorganisms, etc.
  • This phenomenon is known as the main cause of membrane performance deterioration.
  • As a manufacturing method for hollow fiber membrane filtration membranes that are highly effective against fouling caused by proteins and microorganisms for example, materials that can suppress foulants such as proteins and microorganisms are retained or adsorbed on hollow fiber membrane filtration membranes. A method has been proposed.
  • Patent Document 1 discloses "a method for suppressing foulant adsorption by coating the surface of a hollow fiber membrane filtration membrane with a solution of a polymer obtained by polymerizing 2-methacryloyloxyethylphosphorylcholine.”
  • Patent Document 2 discloses "a method in which a solution of a polymer obtained by polymerizing 2-methacryloyloxyethylphosphorylcholine is placed in a coagulation bath, and the polymer is incorporated into a film during film formation.”
  • Patent Document 3 discloses "a production method for forming a film by mixing a solution of a polymer obtained by polymerizing specific 2-methacryloyloxyethylphosphorylcholine with polysulfone.”
  • the present disclosure provides a filtration membrane (particularly a hollow fiber membrane filtration membrane) that effectively suppresses fouling, is excellent in recovering water permeability after cleaning when fouling occurs, and has water resistance.
  • An object of the present invention is to provide a method for manufacturing the membrane.
  • the present inventors have developed a film-forming stock solution containing a polymer containing vinylidene fluoride as a monomer, and a film-forming solution containing a polymer containing styrene and maleic anhydride as monomers.
  • a method for producing a filtration membrane in particular, a hollow fiber membrane filtration membrane in which a filtration membrane is produced using an external control liquid containing a polymer containing a specific phosphorylcholine group, and a polymer containing a specific phosphorylcholine group is immobilized on the filtration membrane.
  • filtration membrane comprising a polymer and a polymer containing styrene and maleic anhydride as monomers.
  • the polymer containing 2-(methacryloyloxy)ethyl 2-(trimethylammonio)ethyl phosphate and 2-aminoethyl methacrylate or its hydrochloride as a monomer is 2-(methacryloyloxy)ethyl 2-(trimethylammonio).
  • the filtration membrane according to item 1 above which contains 40 mol% to 60 mol% of ethyl phosphate and 40 mol% to 60 mol% of 2-aminoethyl methacrylate or its hydrochloride. 4.
  • the polymer (P) includes 30 mol% to 90 mol% of 2-(methacryloyloxy)eth
  • a monovinylidene fluoride on which a polymer (P) containing 2-(methacryloyloxy)ethyl 2-(trimethylammonio)ethyl phosphate and 2-aminoethyl methacrylate or its hydrochloride of the present disclosure is immobilized is used.
  • the polymer (P) is It is immobilized so that it cannot be easily detached from the That is, in the filtration membrane of the present disclosure (particularly the hollow fiber membrane filtration membrane), the polymer (P) does not elute in water, and the fouling suppressing effect can be maintained for a long period of time.
  • the filtration membrane of the present disclosure is made of vinylidene fluoride on which a polymer containing 2-(methacryloyloxy)ethyl 2-(trimethylammonio)ethyl phosphate and 2-aminoethyl methacrylate or its hydrochloride is immobilized as a monomer.
  • This is a filtration membrane (hereinafter sometimes simply referred to as "the filtration membrane of the present disclosure") including a polymer containing as a monomer and a polymer containing styrene and maleic anhydride as monomers.
  • the filtration membrane of the present disclosure includes a hollow fiber membrane filtration membrane and a flat membrane filtration membrane, and preferably a hollow fiber membrane filtration membrane.
  • An example of the composition of the hollow fiber membrane filtration membrane of the present disclosure is that a "polymer containing vinylidene fluoride as a monomer" and "a polymer containing maleic anhydride as a monomer” form a hollow fiber membrane by physical adsorption. formed and substantially free of core liquid.
  • a monomer (constituent unit) means a unit of a compound contained in a polymer based on each monomer or derived from each monomer.
  • each lower limit value and upper limit value can be independently combined.
  • “preferable lower limit: 10” and “more preferable upper limit: 90” can be combined to become “10 to 90”. .
  • a method for manufacturing a hollow fiber membrane filtration membrane of the present disclosure includes the following steps.
  • the polymer (P) includes 30 mol% to 90 mol% of 2-(methacryloyloxy)ethyl 2-(trimethylammonio)ethyl phosphate and 70 mol% to 10 mol% of 2-aminoethyl methacrylate or its hydrochloride.
  • the method for producing a hollow fiber membrane filtration membrane of the present disclosure includes a membrane forming stock solution in which a polymer containing vinylidene fluoride as a monomer is dissolved, a polymer containing styrene and maleic anhydride as monomers, A hollow fiber is manufactured by discharging an external control liquid and a core liquid containing A hollow fiber membrane filtration membrane that has both fouling resistance and water resistance can be produced by reacting a thread membrane filtration membrane with a polymer (P) to immobilize and coat the polymer (P) on the membrane surface.
  • P polymer
  • fouling resistance means that the amount of water permeation is less likely to decrease during filtration using the hollow fiber membrane filtration membrane of the present disclosure, and that the decreased amount of water permeation is recovered during washing. Moreover, water resistance means that the polymer (P) does not peel off from the hollow fiber membrane filtration membrane of the present disclosure.
  • Membrane forming stock solution As the polymer containing vinylidene fluoride as a monomer contained in the membrane forming stock solution of the present disclosure, vinylidene fluoride alone or copolymerized with other monomers can be used. Polymers containing only vinylidene fluoride are commercially available, for example, available from Solvay Specialty Polymers Japan Co., Ltd. (Solef (registered trademark) 11010, Solef (registered trademark) 31508, Solef (registered trademark) 6020, etc.) ).
  • monomers copolymerized with vinylidene fluoride include, but are not particularly limited to, propylene hexafluoride, tetrafluoroethylene, ethylene, ethylene tetrafluoride, ethylene trifluorochloride, vinyl fluoride, and the like.
  • hollow fibers can be produced in the membrane forming stock solution if the polymer containing vinylidene fluoride as a monomer is in the range of 10% to 40% by weight, but in order to produce good hollow fibers, 15% by weight is required. % to 30% by weight is preferred, and 20% to 30% by weight is more preferred.
  • the polymer containing vinylidene fluoride as a monomer (constituent unit) contained in the membrane forming stock solution of the present disclosure is preferably exemplified by polyvinylidene fluoride.
  • the solvent for the membrane forming stock solution of the present disclosure glycerol triacetate, dimethylacetamide, dimethylformamide, dimethyl sulfoxide, N-methylpyrrolidone, and the like can be used. Glycerol triacetate is preferred from the viewpoint of phase separation when the membrane forming stock solution, external control solution, and core solution are immersed (discharged) into the coagulation solution.
  • the polymer containing styrene and maleic anhydride as monomers (constituent units) contained in the external control liquid of the present disclosure is a polymer containing styrene and maleic anhydride as constituent units, or a polymer containing styrene and maleic anhydride as monomers (constituent units), or a polymer containing styrene and maleic anhydride as monomers (constituent units), or , or other monomers (ester, carboxylic acid, diammonium maleate, monoammonium maleate monoester, monoester maleate) can be used as a constituent unit.
  • Polymers of styrene and maleic anhydride are available from Polyscope Polymers.
  • XIRAN (registered trademark) 1000P Polymers of styrene and maleic anhydride are available from Polyscope Polymers.
  • XIRAN (registered trademark) 1000P Polymers of styrene and maleic anhydride are available from Polyscope Polymers.
  • XIRAN (registered trademark) 1000P Polymers based on styrene and maleic anhydride, as well as other monomers, are available from Polyscope Polymers.
  • XIRAN (registered trademark) 1440 and XIRAN (registered trademark) 2625P can be exemplified.
  • the content of the polymer containing styrene and maleic anhydride as monomers in the external control liquid can be set at 1% by weight to 40% by weight, but in order to produce good hollow fibers, 1% by weight is required. % to 20% by weight is preferred, and 1% to 5% by weight is more preferred.
  • the polymer containing styrene and maleic anhydride as monomers (constituent units) contained in the external control liquid of the present disclosure is preferably exemplified by a polymer containing styrene and maleic anhydride as monomers. .
  • glycerol triacetate dimethylacetamide, dimethylformamide, dimethyl sulfoxide, N-methylpyrrolidone, and the like can be used. Glycerol triacetate is preferred from the viewpoint of phase separation when the membrane forming stock solution, external control solution, and core solution are immersed (discharged) into the coagulation solution.
  • core liquid As the core liquid of the present disclosure, glycerol triacetate, dimethylacetamide, dimethylformamide, dimethyl sulfoxide, N-methylpyrrolidone, and the like can be used. Glycerol triacetate is preferred from the viewpoint of phase separation when the membrane forming stock solution, external control solution, and core solution are immersed (discharged) into the coagulation solution.
  • the discharge ratio of the membrane forming stock solution, external control liquid, and core liquid is 1 part to 40 parts by mass of the film forming stock solution, 0.1 part to 20 parts by mass of the external control liquid, and 0.1 part by mass to the core liquid.
  • the amount may be 50 parts by mass, but in order to produce good hollow fibers, preferably 0.1 to 10 parts by mass of the external control liquid and 0 parts by mass of the core liquid to 1 to 20 parts by mass of the membrane forming stock solution.
  • the discharge speed of the membrane forming stock solution, external control liquid, and core liquid is preferably 5 to 20 g/min, more preferably 7 to 9 g/min, and preferably 1 to 10 g/min for the external control liquid.
  • /min more preferably 2 to 4 g/min
  • the core liquid is preferably 3 to 20 g/min, more preferably 5 to 8 g/min.
  • coagulation liquid examples include water, which is a solvent that does not dissolve the hollow fiber membrane filtration membrane of the present disclosure.
  • the amount of coagulation liquid used can be 100 parts by mass to 100,000,000 parts by mass per 100 parts by mass of the membrane-forming stock solution, but in order to favorably proceed with the formation of the hollow fiber membrane filtration membrane. It is preferable to use 1,000 parts by mass to 100,000,000 parts by mass of the coagulating liquid, and more preferably to use 1,000 parts by mass to 100,000 parts by mass.
  • the method of manufacturing a hollow fiber membrane filtration membrane by the thermally induced phase separation method of the present disclosure includes discharging a membrane forming stock solution, a membrane forming stock solution, an external control liquid, and a core liquid from a concentric multi-slit nozzle, and cooling them with a low-temperature coagulation liquid. This causes phase separation into a concentrated phase and a dilute phase in each of the polyvinylidene fluoride layer and the styrene maleic anhydride polymer layer. In this dense phase, a hollow fiber membrane is formed in which the surface of polyvinylidene fluoride is covered with a styrene maleic anhydride polymer.
  • Membrane-form membrane forming stock solution manufacturing process (hollow fiber manufacturing process)
  • the membrane forming stock solution, external control liquid, and core liquid (glycerol triacetate) are discharged from a triple slit nozzle to obtain hollow fibers.
  • the temperature of the coagulating liquid is preferably 5°C to 40°C.
  • a washing step of removing the solvent etc. using water or hot water at 5° C. to 95° C. an extraction step of removing the solvent by extraction, A drying step at 5 to 70° C. may also be performed.
  • the hollow fiber membrane filtration membrane is not used immediately, it can be stored in a storage solution containing water, glycerin, or ethanol.
  • the polymer (P) of the present disclosure comprises 30 mol% to 90 mol% of 2-(methacryloyloxy)ethyl 2-(trimethylammonio)ethyl phosphate and 70 mol% to 10 mol% of 2-aminoethyl methacrylate or its hydrochloride.
  • the polymer (P) of the present disclosure may have any structure such as a random polymer or a block polymer, or may be a mixture of these polymers.
  • Method for producing polymer (P) As a method for producing the polymer (P), known methods such as solution polymerization, bulk polymerization, emulsion polymerization, and suspension polymerization can be used. For example, 2-(methacryloyloxy)ethyl 2-(trimethylammonio)ethyl A method can be adopted in which a phosphate and 2-aminoethyl methacrylate or its hydrochloride are subjected to a polymerization reaction in a solvent in the presence of a polymerization initiator.
  • the solvent used in the polymerization reaction may be any solvent that dissolves 2-(methacryloyloxy)ethyl 2-(trimethylammonio)ethyl phosphate and 2-aminoethyl methacrylate or its hydrochloride; specifically, water, methanol, ethanol, etc. , propanol, t-butanol, benzene, toluene, dimethylformamide, dimethyl sulfoxide, N-methylpyrrolidone, tetrahydrofuran, chloroform, etc., and two or more types may be mixed.
  • the initiator used in the polymerization reaction any common initiator may be used.
  • an azo compound water-soluble azo polymerization initiator
  • an organic peroxide can be used. .
  • the solvent used when performing the immobilization reaction between the hollow fiber membrane filtration membrane and the polymer (P) in the immobilization step (e) of the present disclosure is a solvent in which the polymer (P) is dissolved and which is a membrane material.
  • Any solvent that does not dissolve the polyvinylidene fluoride or styrene maleic anhydride polymer can be used. Examples include water, methanol, ethanol, propanol, t-butanol, benzene, toluene, dimethylformamide, dimethyl sulfoxide, N-methylpyrrolidone, tetrahydrofuran, chloroform, etc., and two or more types may be mixed.
  • the concentration of the polymer (P) when performing the immobilization reaction between the hollow fiber membrane filtration membrane and the polymer (P) may be between 0.1% and 10% by weight, but this may be due to economical and environmental considerations. Considering the influence, 0.1% by weight to 5% by weight is preferable.
  • a catalyst can be used to promote the reaction.
  • an acid catalyst or a base catalyst can be used as the solvent used in the immobilization reaction of the hollow fiber membrane filtration membrane and the polymer (P).
  • Examples include hydrochloric acid, acetic acid, sulfuric acid, phosphoric acid, p-toluenesulfonic acid monohydrate, etc.
  • Base catalysts include 4-dimethylaminopyridine, pyridine, triethylamine, etc., but triethylamine is preferred from the viewpoint of reactivity and cost. is preferred.
  • the amount of catalyst used when performing the immobilization reaction between the hollow fiber membrane filtration membrane and the polymer (P) can be in the range of 0.1% to 10% by weight, but it is important to maintain reactivity and protect the environment. Considering the influence, it is preferably 0.1% to 5% by weight, more preferably 0.1% to 1% by weight.
  • the filtration membrane of the present disclosure (in particular, the hollow fiber membrane filtration membrane) has been confirmed to have excellent fouling resistance and water resistance through the following examples. All applications where filtration membranes, reverse osmosis membranes, etc. are used (e.g., removal of microorganisms, bacteria, and viruses, separation and concentration of proteins, enzymes, etc., artificial dialysis, separation and removal of yeast in the production of draft sake and draft beer, seawater desalination) It can be used for production of industrial pure water and ultrapure water, concentration of fruit juice and milk, purification of wastewater, etc.).
  • filtration membrane of the present disclosure can be exemplified below, but are not particularly limited.
  • polyvinylidene fluoride powder Solvay 6020 manufactured by Solvay Specialty Polymers Japan Co., Ltd., weight average molecular weight 687 kDa
  • glycerol triacetate Frujifilm Wako Pure Chemical Industries, Ltd., hereinafter referred to as "GTA”
  • External control liquid preparation step (b) 10 parts by mass of styrene maleic anhydride polymer (SMA-6000 manufactured by Polyscope Polymers, weight average molecular weight 10 kDa, polystyrene:maleic anhydride molar ratio 6:1) to 190 parts by mass of GTA. It was dissolved at 60°C.
  • the discharge speed was 8.5 g/min for the film forming stock solution, 2.5 g/min (2 ml/min) for the external control liquid, and 6.2 g/min for the core solution (GTA).
  • Membrane forming step (d) The discharged hollow fibers were immersed in a coagulating liquid (water) and cooled to obtain a hollow fiber membrane-like filtration membrane. At this time, the temperature of the coagulation liquid was 15°C. Washing step (d-1): Once the hollow fiber membrane filtration membrane was formed, it was soaked in 40°C warm water to remove glycerol triacetate. Storage step (d-2): The hollow fiber membrane filtration membrane was left standing in pure water and stored.
  • the hollow fiber membrane filtration membrane (30 cm) produced in Production Example 1 was immersed in water containing 2 wt% polymer (P-1) and 0.25 wt% triethylamine (catalyst: Fuji Film Wako Pure Chemical Industries, Ltd.). After that, the solution temperature was raised to 60°C and left for 6 hours. Thereafter, it was washed with pure water and stored in pure water.
  • a hollow fiber membrane filtration membrane of the present disclosure was produced in the same manner as in Example 1, except that polymer (P-1) was replaced with polymer (P-2).
  • a hollow fiber membrane filtration membrane of the present disclosure was produced in the same manner as in Example 1, except that polymer (P-1) was replaced with polymer (P-3).
  • the water permeation amount (LMH/Bar) was measured at 1 bar using pure water (initial water permeation amount). Subsequently, a 1,000 ppm bovine serum albumin solution was used as a model foulant, and the solution was permeated for 60 minutes. Thereafter, backwashing was performed for 10 minutes using pure water with the direction of water permeation reversed. After backwashing, the amount of water permeation (LMH/Bar) was measured again using pure water (the amount of water permeation after the first backwashing), and the water permeation recovery rate (%) was calculated.
  • LMH/Bar water permeation amount
  • M-1 of the present disclosure produced in Example 1 first, a 0.85% by weight sodium chloride (Fujifilm Wako Pure Chemical Industries, Ltd.) aqueous solution was used at 0.5 bar. The water permeation amount (LMH/Bar) was measured (initial water permeation amount). Subsequently, a bacterial suspension (Sphingomonas paucimobilis) was used as a model foulant, and the solution was permeated for 90 minutes. Thereafter, backwashing was performed for 10 minutes with a 0.85% by weight aqueous sodium chloride solution in which the direction of water permeation was reversed.
  • the water permeation recovery rate (%) is a value expressed by the following formula (2).
  • the unit of water permeation amount "LMH/Bar” represents the amount of water passing through the filter membrane (L) per 1 m 2 of the filter membrane per hour under 1 bar.
  • the results are shown in Table 2.
  • Water permeability recovery rate (%) (water permeability after backwashing/initial water permeation) x 100...Formula (2)
  • the bacterial suspension was prepared by culturing the culture using tryptic soy broth (manufactured by Becton Dickinson, 30 g/L) at 120 rpm and 30°C for 12 hours with shaking, then diluting it 50 times with tryptic soy broth and culturing it for 4 hours.
  • the cells were cultured again at °C and diluted with tryptic soy broth to a bacterial concentration of 0.05 at 450 nm absorbance.
  • the hollow fiber membrane filtration membrane manufactured in Manufacturing Example 1 was used.
  • the hollow fiber membrane filtration membrane (M-1) of the present disclosure manufactured in Example 1 was cut into approximately 1 cm pieces, placed on a test stand, and a water droplet was dropped on it, and the contact angle change was determined with the moment of drop as the initial stage and 120 seconds later as the final stage. was measured. Furthermore, the contact angle was similarly measured for the hollow fiber membrane filtration membrane (M-1) of the present disclosure that had been stored in water for 30 and 60 days. The results are shown in Table 3. The contact angle was measured using a contact angle goniometer Drop Master (manufactured by Kyowa Interface Science Co., Ltd.). In Comparative Example 3, the hollow fiber membrane filtration membrane manufactured in Manufacturing Example 1 was used.
  • Example 6 The contact angle change was measured in the same manner as in Example 6, except that the hollow fiber membrane filtration membrane (M-2) of the present disclosure manufactured in Example 2 was used. The results are shown in Table 3.
  • Example 3 The contact angle change was measured in the same manner as in Example 6, except that the hollow fiber membrane filtration membrane (M-3) of the present disclosure manufactured in Example 3 was used. The results are shown in Table 3.
  • the water permeation recovery rate of the hollow fiber membrane filtration membrane of the present disclosure was significantly superior to that of Comparative Example 1.
  • the hollow fiber membrane filtration membrane of the present disclosure showed a high water permeability recovery rate even when the number of backwashes was increased, and also showed a high water permeability recovery rate even in cell suspensions containing proteins and bacteria. Highly ring-like.
  • the hollow fiber membrane filtration membrane of the present disclosure did not change the contact angle even after being stored in water for a long period of time, so the polymer (P) did not peel off, and it was excellent. It was revealed that it has water resistance.
  • the hollow fiber membrane filtration membrane of the present disclosure has excellent fouling resistance and water resistance.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

La présente invention concerne : une membrane de filtration (en particulier, une membrane de filtration de type membrane à fibres creuses) qui inhibe efficacement l'encrassement, qui présente une excellente récupération de la perméabilité à l'eau après le nettoyage lorsque l'encrassement s'est produit, et qui présente une résistance à l'eau ; et un procédé de production de ladite membrane.　La présente divulgation a été obtenue lors de la découverte d'un procédé de production d'une membrane de filtration (en particulier, une membrane de filtration de type membrane à fibres creuses) : une membrane de filtration étant produite avec une solution mère formant une membrane qui contient un polymère qui contient du fluorure de vinylidène en tant que monomère et une solution de contrôle externe qui contient un polymère qui contient du styrène et de l'anhydride maléique en tant que monomères ; et immobilisation sur la membrane de filtration d'un polymère qui contient un groupe phosphorylcholine spécifique.
PCT/JP2023/014039 2022-04-08 2023-04-05 Membrane de filtration et procédé de production de ladite membrane Ceased WO2023195479A1 (fr)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN120459816A (zh) * 2025-07-16 2025-08-12 贵州中车绿色环保有限公司 一种复合膜及其制备方法

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2012055870A (ja) * 2010-09-13 2012-03-22 Kobe Univ ポリフッ化ビニリデン多孔質濾過膜の製造方法
JP2014200752A (ja) * 2013-04-05 2014-10-27 ダイキン工業株式会社 高分子多孔質膜
JP2017170319A (ja) * 2016-03-23 2017-09-28 旭化成株式会社 ポリフッ化ビニリデン製多孔膜とその製造方法
US20190282968A1 (en) * 2016-05-11 2019-09-19 Guizhou Material Industrial Technology Institute Preparation method of high-strength anti-pollution antibacterial hollow fiber nanofiltration membrane and product
WO2020231797A1 (fr) * 2019-05-10 2020-11-19 Trustees Of Tufts College Membranes à copolymères chargés zwitterioniques

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2012055870A (ja) * 2010-09-13 2012-03-22 Kobe Univ ポリフッ化ビニリデン多孔質濾過膜の製造方法
JP2014200752A (ja) * 2013-04-05 2014-10-27 ダイキン工業株式会社 高分子多孔質膜
JP2017170319A (ja) * 2016-03-23 2017-09-28 旭化成株式会社 ポリフッ化ビニリデン製多孔膜とその製造方法
US20190282968A1 (en) * 2016-05-11 2019-09-19 Guizhou Material Industrial Technology Institute Preparation method of high-strength anti-pollution antibacterial hollow fiber nanofiltration membrane and product
WO2020231797A1 (fr) * 2019-05-10 2020-11-19 Trustees Of Tufts College Membranes à copolymères chargés zwitterioniques

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
HAN GANG, LIU JIANG TAO, LU KANG JIA, CHUNG TAI-SHUNG: "Advanced Anti-Fouling Membranes for Osmotic Power Generation from Wastewater via Pressure Retarded Osmosis (PRO)", ENVIRONMENTAL SCIENCE & TECHNOLOGY, AMERICAN CHEMICAL SOCIETY, US, vol. 52, no. 11, 5 June 2018 (2018-06-05), US , pages 6686 - 6694, XP093097826, ISSN: 0013-936X, DOI: 10.1021/acs.est.7b05933 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN120459816A (zh) * 2025-07-16 2025-08-12 贵州中车绿色环保有限公司 一种复合膜及其制备方法

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