WO2017200313A1 - Procédé de fabrication d'un séparateur de traitement d'eau, séparateur de traitement d'eau fabriqué au moyen de celui-ci, et module de traitement d'eau comprenant un séparateur de traitement d'eau - Google Patents

Procédé de fabrication d'un séparateur de traitement d'eau, séparateur de traitement d'eau fabriqué au moyen de celui-ci, et module de traitement d'eau comprenant un séparateur de traitement d'eau Download PDF

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Publication number
WO2017200313A1
WO2017200313A1 PCT/KR2017/005159 KR2017005159W WO2017200313A1 WO 2017200313 A1 WO2017200313 A1 WO 2017200313A1 KR 2017005159 W KR2017005159 W KR 2017005159W WO 2017200313 A1 WO2017200313 A1 WO 2017200313A1
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Prior art keywords
formula
water treatment
monomer
random copolymer
content
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PCT/KR2017/005159
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English (en)
Korean (ko)
Inventor
이병수
김태형
전형준
이영주
신정규
곽봉주
Original Assignee
주식회사 엘지화학
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
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Priority claimed from KR1020170061255A external-priority patent/KR102085402B1/ko
Application filed by 주식회사 엘지화학 filed Critical 주식회사 엘지화학
Priority to CN201780004100.3A priority Critical patent/CN108348870B/zh
Priority to US15/770,859 priority patent/US10688449B2/en
Priority to JP2018522772A priority patent/JP6582352B2/ja
Priority to EP17799670.9A priority patent/EP3369475B1/fr
Publication of WO2017200313A1 publication Critical patent/WO2017200313A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
    • B01D69/10—Supported membranes; Membrane supports
    • B01D69/107—Organic support material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D67/00—Processes specially adapted for manufacturing semi-permeable membranes for separation processes or apparatus
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
    • B01D69/10—Supported membranes; Membrane supports
    • 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
    • B01D71/56—Polyamides, e.g. polyester-amides
    • 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
    • B01D71/58—Other polymers having nitrogen in the main chain, with or without oxygen or carbon only
    • 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
    • B01D71/76—Macromolecular material not specifically provided for in a single one of groups B01D71/08 - B01D71/74
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis

Definitions

  • the present specification relates to a method for preparing a water treatment membrane, a water treatment membrane manufactured using the same, and a water treatment module including the water treatment membrane.
  • Osmotic phenomenon is the movement of a solvent through a membrane from a solution of low solute concentration to a solution of high solute concentration between two solutions separated by semi-permeable membrane.
  • the pressure is called osmotic pressure.
  • applying an external pressure higher than osmotic pressure causes the solvent to move toward a solution with a low concentration of solute.
  • This phenomenon is called reverse osmosis.
  • a pressure gradient can be used as a driving force to separate various salts or organic substances through the semipermeable membrane.
  • the water treatment membrane using the reverse osmosis phenomenon is used to separate the material of the molecular level, remove the salt from the brine or sea water to supply the domestic, construction, industrial water.
  • water treatment separation membranes include polyamide-based water treatment separation membranes, and polyamide-based water treatment separation membranes are manufactured by forming a polyamide active layer on a microporous layer support.
  • a sulfonic layer is formed to form a microporous support, and the microporous support is immersed in an aqueous solution of m-phenylene diamine (mPD) to form an mPD layer, which in turn is formed of trimesoyl chloride (TriMesoyl Chloride, TMC)
  • TMC trimesoyl chloride
  • the present specification is to provide a water treatment membrane having an improved salt removal rate and flow rate and a method for producing the same.
  • preparing a porous support Forming a polyamide active layer on the porous support using interfacial polymerization of an aqueous solution containing an amine compound and an organic solution containing an acyl halide compound; And coating a coating solution comprising a random copolymer comprising a monomer of Formula 1, a monomer of Formula 2, and a monomer of Formula 3 on the polyamide active layer:
  • the content of the random copolymer is 0.5 to 2% by weight based on the total weight of the coating solution provides a method for producing a water treatment separation membrane.
  • the content of the monomer of Formula 1 is 70 to 90% by weight based on the entire random copolymer
  • the content of the monomer of Formula 2 is 5 to 25% by weight based on the entire random copolymer
  • the content of the monomer of Formula 3 is 5 to 25% by weight based on the entire random copolymer
  • R 1 to R 3 are the same as or different from each other, and each independently hydrogen; Or a substituted or unsubstituted alkyl group.
  • the porous support A polyamide active layer provided on the porous support; And it provides a water treatment separation membrane comprising a coating layer comprising a random copolymer comprising a monomer represented by the above formulas 1 to 3 on the polyamide active layer, according to the above-described manufacturing method.
  • Reverse osmosis membrane prepared by the manufacturing method according to an embodiment of the present disclosure is excellent in permeation flux and salt removal rate.
  • the reverse osmosis membrane is prepared according to one embodiment of the present specification, by including an acetoacetyl-based compound in the coating solution, it is possible to prepare a reverse osmosis membrane excellent in durability and stain resistance.
  • substituted means that a hydrogen atom bonded to a carbon atom of the compound is replaced with another substituent, and the position to be substituted is not limited to a position where the hydrogen atom is substituted, that is, a position where a substituent can be substituted, if two or more substituted , Two or more substituents may be the same or different from each other.
  • substituted or unsubstituted is hydrogen; heavy hydrogen; Halogen group; Nitrile group; And it is substituted with one or two or more substituents selected from the group consisting of a substituted or unsubstituted alkyl group, or means having no substituent.
  • the halogen group may be fluorine, chlorine, bromine or iodine.
  • the alkyl group may be linear or branched chain, carbon number is not particularly limited, but is preferably 1 to 20.
  • Specific examples include methyl, ethyl, propyl, n-propyl, isopropyl, butyl, n-butyl, isobutyl, tert-butyl, sec-butyl, 1-methyl-butyl, 1-ethyl-butyl, pentyl, n-pentyl , Isopentyl, neopentyl, tert-pentyl, hexyl, n-hexyl, 1-methylpentyl, 2-methylpentyl, 4-methyl-2-pentyl, 3,3-dimethylbutyl, 2-ethylbutyl, heptyl, n -Heptyl, 1-methylhexyl, cyclopentylmethyl, cyclohexylmethyl, octyl, n-o
  • preparing a porous support Forming a polyamide active layer on the porous support using interfacial polymerization of an aqueous solution containing an amine compound and an organic solution containing an acyl halide compound; And coating a coating solution including a random copolymer including a monomer of Formula 1, a monomer of Formula 2, and a monomer of Formula 3 on the polyamide active layer, wherein the content of the random copolymer is It provides a method for producing a water treatment separator of 0.5 to 2% by weight based on the total weight of the coating liquid.
  • the content of the monomer of Formula 1 is 70 to 90% by weight based on the entire random copolymer
  • the content of the monomer of Formula 2 is 5 to 25% by weight based on the entire random copolymer
  • the content of the monomer of Formula 3 is 5 to 25% by weight based on the entire random copolymer
  • R 1 to R 3 are the same as or different from each other, and each independently hydrogen; Or a substituted or unsubstituted alkyl group.
  • the monomers of Chemical Formulas 1 to 3 may be continuously connected to each other, the same monomer may be connected to each other, or different monomers may be connected to each other.
  • a coating layer of a polymer material may be used on a nonwoven fabric.
  • the polymer material include polysulfone, polyethersulfone, polycarbonate, polyethylene oxide, polyimide, polyetherimide, polyether ether ketone, polypropylene, polymethylpentene, polymethyl chloride and polyvinylidene fluorine. Ride or the like may be used, but is not necessarily limited thereto.
  • polysulfone may be used as the polymer material.
  • the thickness of the porous support may be 60 ⁇ m to 100 ⁇ m, but is not limited thereto and may be adjusted as necessary.
  • the pore size of the porous support is preferably 1nm to 500nm, but is not limited thereto.
  • the polyamide active layer may include forming an aqueous solution layer including an amine compound on a porous support; And contacting an organic solution including an acyl halide compound on the aqueous solution layer including the amine compound to form a polyamide active layer.
  • the contact when the aqueous solution layer containing the amine compound and the organic solution containing the acyl halide compound contact, the amine compound and acyl halide compound coated on the surface of the polyamide by interfacial polymerization Is produced and adsorbed onto the microporous support to form a thin film.
  • the contact may form an active layer through a method such as dipping, spraying or coating.
  • a method of forming an aqueous solution layer including an amine compound on the porous support is not particularly limited, and any method capable of forming an aqueous solution layer on the support may be used without limitation. Specifically, the method of forming the aqueous solution layer containing an amine compound on the porous support may be sprayed, applied, immersed, dripping and the like.
  • the aqueous solution layer may be additionally subjected to a step of removing an aqueous solution including an excess amine compound as necessary.
  • the aqueous solution layer formed on the porous support may be unevenly distributed when there are too many aqueous solutions present on the support.
  • a non-uniform active layer may be formed by subsequent interfacial polymerization. Therefore, it is preferable to remove excess aqueous solution after forming an aqueous solution layer on the said support body.
  • the removal of the excess aqueous solution is not particularly limited, but may be performed using, for example, a sponge, air knife, nitrogen gas blowing, natural drying, or a compression roll.
  • the amine compound in the aqueous solution containing the amine compound is not limited as long as it can be used for the polymerization of polyamide, but specific examples include m-phenylenediamine (mPD), p-phenylenediamine (PPD), 1,3 , 6-benzenetriamine (TAB), 4-chloro-1,3-phenylenediamine, 6-chloro-1,3-phenylenediamine, 3-chloro-1,4-phenylene diamine or mixtures thereof It can be used preferably.
  • the content of the amine compound may be 0.1 wt% or more and 20 wt% or less with respect to 100 wt% of the composition.
  • the acyl halide compound is not limited as long as it can be used for the polymerization of polyamide, but is an aromatic compound having 2 to 3 carboxylic acid halides as a specific example, and may include trimezoyl chloride, isophthaloyl chloride and terephthaloyl. One or a mixture of two or more selected from the group of compounds consisting of chlorides may be preferably used.
  • the acyl halide compound may be present in an amount of 0.05 wt% or more and 1 wt% or less with respect to 100 wt% of the composition.
  • the random copolymer including the monomer of Formula 1, the monomer of Formula 2, and the monomer of Formula 3 included in the coating solution has unreacted functional groups and self-crosslinking present in the active layer. It is possible to prevent the active layer used for a long time directly contact with the raw water, thereby increasing the durability of the active layer, it is possible to ensure continuous performance.
  • the monomer of Formula 1 may serve to prevent surface damage of the active layer and to protect the active layer for a long time in the water treatment membrane, the content of the random copolymer may be 70 to 90% by weight.
  • the monomer of Chemical Formula 2 is an intermediate in which the monomer of Chemical Formula 1 is modified to synthesize the monomer of Chemical Formula 3, and the content of the random copolymer may be 5 to 25% by weight depending on the degree of reaction.
  • the monomer of Chemical Formula 3 enables unreacted functional groups and self-crosslinking present in the active layer, and serves to prevent the coating solution from being easily removed from the active layer.
  • the monomer of Formula 3 may have a content of 5 to 25% by weight in the random copolymer, when the content is more than 25% by weight, since the flow rate is sharply reduced, the effect of the water treatment membrane protective layer is present in the range great.
  • the rapid decrease in salt removal rate and a slight decrease in flow rate may be due to the lack of an absolute amount of the compound coated on the surface of the active layer is not properly functioning as a protective layer, 2
  • the decrease in the salt removal rate and the rapid decrease in the flow rate are determined to decrease the performance due to the change in the surface properties by the compound coated in excess on the surface of the active layer.
  • it can be applied to low grade water treatment membranes.
  • the random copolymer has a molecular weight (MW) of 20,000 to 40,000, preferably 25,000 to 35,000.
  • the solvent of the coating liquid may be a hydrophilic solvent, preferably may be distilled water.
  • a method of forming a coating solution on the polyamide active layer is not particularly limited, and any method capable of forming a coating layer on the polyamide active layer may be used without limitation.
  • the method of forming a coating layer on the polyamide active layer may include drying, after treatment such as spraying, coating, dipping, dropping, and the like.
  • the coating layer may be further subjected to the step of removing the excess coating liquid as needed.
  • the coating layer formed on the polyamide active layer may be unevenly distributed when there is too much coating liquid present on the support. Therefore, it is preferable to remove excess coating liquid after forming a coating layer on the polyamide active layer.
  • the excess coating liquid is not particularly limited, but may be performed using, for example, a sponge, air knife, nitrogen gas blowing, air drying, or a compression roll.
  • the R One To R 3 They are the same as or different from each other, and each independently hydrogen; Or a substituted or unsubstituted alkyl group having 1 to 20 carbon atoms.
  • R 1 and R 2 may be hydrogen.
  • the end group of the random copolymer may be a linear or branched alkyl group, and specific examples thereof include methyl, ethyl, and propyl, but are not limited thereto.
  • a porous support A polyamide active layer provided on the porous support; And a random copolymer comprising a monomer of Formula 1, a monomer of Formula 2, and a monomer of Formula 3 on the polyamide active layer, and provides a water treatment separation membrane prepared according to the above-described preparation method.
  • the water treatment separation membrane may further include an additional layer, if necessary, for example, the water treatment separation membrane may further include an antifouling layer provided on the polyamide active layer.
  • the water treatment separation membrane may be used as a micro filtration membrane, an ultra filtration membrane, an ultra filtration membrane, a nano filtration membrane, a reverse osmosis membrane, or a reverse osmosis membrane. Can be used.
  • One embodiment of the present specification provides a water treatment module including the aforementioned water treatment separation membrane.
  • a specific kind of the water treatment module is not particularly limited, and examples thereof include a plate & frame module, a tubular module, a hollow & fiber module or a spiral wound module.
  • the water treatment module includes the reverse osmosis membrane according to one embodiment of the present specification described above, other configurations and manufacturing methods are not particularly limited, and any general means known in the art may be employed without limitation. .
  • the water treatment module according to an exemplary embodiment of the present specification has excellent salt removal rate and permeate flow rate, and uses a reverse osmosis membrane having a large effective membrane area, and has a small performance deviation and improved uniformity. It can be usefully used in water treatment devices such as water treatment devices.
  • An aqueous solution layer was formed by applying an aqueous solution containing 3.6 wt% of metaphenylenediamine (mPD) on the porous polysulfone support prepared by the above method.
  • mPD metaphenylenediamine
  • An organic solution was prepared by adding 0.25 wt% of trimezoyl chloride (TMC) solution using an ISOPar (Exxon) solvent, and then applying the organic solution onto the aqueous layer and drying to form a polyamide active layer.
  • TMC trimezoyl chloride
  • a random copolymer (weight average molecular weight 30,000, GOHSENX Z-) comprising 89.4% by weight of the monomer of Formula 1, 4.0% by weight of the monomer of Formula 2 and 6.6% by weight of monomer of Formula 3 on the polyamide active layer 200, Nippon Synthetic Chemical Industry Co., Ltd) and 0.5% by weight of a coating solution using distilled water as a solvent and then coated by the method of drying to prepare a water treatment separation membrane.
  • R 1 and R 2 in Chemical Formula 3 applied in Example 1 are hydrogen, and R 3 is a methyl group.
  • a water treatment separation membrane was manufactured in the same manner as in Example 1, except that a random copolymer including the monomer of Formula 1, the monomer of Formula 2, and the monomer of Formula 3 was 1 wt%.
  • a water treatment separation membrane was manufactured in the same manner as in Example 1, except that the content of the random copolymer including the monomer of Formula 1, the monomer of Formula 2, and the monomer of Formula 3 was 1.5% by weight.
  • a water treatment separation membrane was manufactured in the same manner as in Example 1, except that the content of the random copolymer including the monomer of Formula 1, the monomer of Formula 2, and the monomer of Formula 3 was 2% by weight.
  • a water treatment separation membrane was manufactured in the same manner as in Example 1, except that the content of the random copolymer including the monomer of Formula 1, the monomer of Formula 2, and the monomer of Formula 3 was 0.1 wt%.
  • a water treatment separation membrane was manufactured in the same manner as in Example 1, except that the content of the random copolymer including the monomer of Formula 1, the monomer of Formula 2, and the monomer of Formula 3 was 0.25 wt%.
  • a water treatment separation membrane was manufactured in the same manner as in Example 1, except that the content of the random copolymer including the monomer of Formula 1, the monomer of Formula 2, and the monomer of Formula 3 was 5% by weight.
  • a water treatment separation membrane was manufactured in the same manner as in Example 1, except that the content of the random copolymer including the monomer of Formula 1, the monomer of Formula 2, and the monomer of Formula 3 was 10 wt%.
  • a water treatment separation membrane was manufactured in the same manner as in Example 1, except that a coating solution including 1.5 wt% of polyvinyl alcohol including only Formula 1 as a monomer instead of acetoacetylated polyvinyl alcohol was used.
  • a water treatment separation membrane was manufactured in the same manner as in Example 1, except that a coating solution including 2.0 wt% of polyvinyl alcohol including only Formula 1 as a monomer instead of acetoacetylated polyvinyl alcohol was used.
  • the initial salt removal rate and initial permeate flow rate of the water treatment membranes prepared according to Examples 1 to 4 and Comparative Examples 1 to 7 were evaluated by the following method.
  • a water treatment module including a flat plate permeation cell, a high pressure pump, a storage tank, and a cooling device was used.
  • the structure of the plate-shaped transmission cell was 28 cm 2 in an effective cross-flow (cross-flow) manner.
  • the reverse osmosis membrane was installed in the permeation cell, and then preliminarily operated for about 1 hour using tertiary distilled water to stabilize the evaluation equipment.
  • the flux was calculated by measuring the amount of water permeated at 25 ° C. for 15 minutes. Rejection was calculated by analyzing the salt concentration before and after permeation using a conductivity meter.
  • the coating solution contains 0.5 to 2% by weight of acetoacetylated polyvinyl alcohol, it was found that the salt removal rate and the flow rate significantly increased as compared with less than 0.5% or more than 2% by weight.
  • the membrane is exposed to contaminants (foulant, skim milk) and chemical cleaning is performed in order to evaluate the fouling resistance and chemical resistance through the change in membrane performance caused by contaminants and the change in membrane performance after chemical cleaning to remove contaminants.
  • contamination foulant, skim milk
  • chemical cleaning is performed in order to evaluate the fouling resistance and chemical resistance through the change in membrane performance caused by contaminants and the change in membrane performance after chemical cleaning to remove contaminants. The performance during the removal of contaminants stuck to the membrane surface was observed over time.
  • a water treatment module including a flat plate permeation cell, a high pressure pump, a storage tank, and a cooling device was used.
  • the structure of the plate-shaped transmission cell was 28 cm 2 in an effective cross-flow (cross-flow) manner.
  • the reverse osmosis membrane was installed in the permeation cell, and then preliminarily operated for about 1 hour using tertiary distilled water to stabilize the evaluation equipment. Thereafter, 50 ppm skim milk was injected into the 2,000 ppm sodium chloride solution, and the equipment was operated for about 1 hour at a flow rate of 225 psi and 4.5 L / min, and then stabilized.
  • the amount of water permeated at 25 ° C. for 15 minutes was measured.
  • the flux was calculated, and the salt removal rate was calculated by analyzing the salt concentration before and after the permeation using a conductivity meter. Thereafter, the flow rate and the salt removal rate were measured at regular time intervals while the performance of the separator decreased to 50% of the initial flow rate.
  • Chemical cleaning was performed to remove contaminants from the contaminated membrane.
  • NaOH solution with pH 12 was operated for 30 minutes at 4.5 L / min flow rate and circulated in flat plate permeation cell. Soaking was performed for 60 minutes and equipment was again operated for 30 minutes. It was circulated in the type permeation cell. The distilled water was then operated for about 30 minutes at a flow rate of 4.5 L / min to remove NaOH remaining in the flat permeation cell.
  • HCl (or Citric acid) solution of pH 2 was operated for 30 minutes at 4.5 L / min flow rate and circulated in the flat-type permeation cell, soaking for 60 minutes, and again for 30 minutes. It was made to circulate in a flat permeation cell.
  • the equipment was operated for about 30 minutes at 4.5 L / min flow rate to remove HCl (or Citric acid) solution remaining in the flat permeate cell, and then 2,000 ppm sodium chloride at 225 psi and 4.5 L / min flow rate for 1 hour.
  • the flux is calculated by measuring the amount of water permeated at 25 ° C. for 15 minutes, and the salt removal rate is analyzed by analyzing the salt concentration before and after the permeation using a conductivity meter. Rejection was calculated.
  • the existing polyvinyl alcohol applied film (Comparative Example 7) was found to be reduced by 41.71% compared to the initial flow rate, 0.13% compared to the initial removal rate, respectively, when exposed to contaminants for 30 hours, acetoacetylated poly Vinyl alcohol applied separator (Example 2) was found to be 29.55% compared to the initial flow rate, 0.11% compared to the initial removal rate, respectively, under the same conditions.

Abstract

La présente invention concerne un procédé de fabrication d'un séparateur de traitement d'eau, un séparateur de traitement d'eau fabriqué au moyen de celui-ci, et un module de traitement d'eau comprenant le séparateur de traitement d'eau, le procédé comprenant les étapes de : préparation d'un support poreux ; formation d'une couche active de polyamide sur le support poreux au moyen d'une polymérisation interfaciale d'une solution aqueuse contenant un composé aminé et une solution organique contenant un composé d'halogénure d'acyle ; et l'enduction d'un liquide de revêtement sur la couche active de polyamide, le liquide de revêtement contenant un copolymère statistique comprenant des monomères représentés par les formules chimiques 1 à 3, la teneur en copolymère statistique étant comprise entre 0,5 et 2 % en poids par rapport au poids total du liquide de revêtement.
PCT/KR2017/005159 2016-05-18 2017-05-18 Procédé de fabrication d'un séparateur de traitement d'eau, séparateur de traitement d'eau fabriqué au moyen de celui-ci, et module de traitement d'eau comprenant un séparateur de traitement d'eau WO2017200313A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
CN201780004100.3A CN108348870B (zh) 2016-05-18 2017-05-18 水处理分离件的制造方法、使用其制造的水处理分离件及包括水处理分离件的水处理模块
US15/770,859 US10688449B2 (en) 2016-05-18 2017-05-18 Method for manufacturing water treatment separator, water treatment separator manufactured using same, and water treatment module comprising water treatment separator
JP2018522772A JP6582352B2 (ja) 2016-05-18 2017-05-18 水処理分離膜の製造方法、これを用いて製造された水処理分離膜、および水処理分離膜を含む水処理モジュール
EP17799670.9A EP3369475B1 (fr) 2016-05-18 2017-05-18 Procédé de fabrication d'un séparateur de traitement d'eau, séparateur de traitement d'eau fabriqué au moyen de celui-ci, et module de traitement d'eau comprenant un séparateur de traitement d'eau

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
KR10-2016-0061092 2016-05-18
KR20160061092 2016-05-18
KR1020170061255A KR102085402B1 (ko) 2016-05-18 2017-05-17 수처리 분리막의 제조방법, 이를 이용하여 제조된 수처리 분리막, 및 수처리 분리막을 포함하는 수처리 모듈
KR10-2017-0061255 2017-05-17

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