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WO2010029908A1 - Membrane fibre creuse et procédé de fabrication d’une membrane fibre creuse - Google Patents

Membrane fibre creuse et procédé de fabrication d’une membrane fibre creuse Download PDF

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Publication number
WO2010029908A1
WO2010029908A1 PCT/JP2009/065631 JP2009065631W WO2010029908A1 WO 2010029908 A1 WO2010029908 A1 WO 2010029908A1 JP 2009065631 W JP2009065631 W JP 2009065631W WO 2010029908 A1 WO2010029908 A1 WO 2010029908A1
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WO
WIPO (PCT)
Prior art keywords
hollow fiber
fiber membrane
membrane
film
hole
Prior art date
Legal status (The legal status 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 status listed.)
Ceased
Application number
PCT/JP2009/065631
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English (en)
Japanese (ja)
Inventor
努 上阪
典浩 谷
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.)
Toray Industries Inc
Original Assignee
Toray Industries Inc
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Publication date
Application filed by Toray Industries Inc filed Critical Toray Industries Inc
Priority to CN200980135265.XA priority Critical patent/CN102149449B/zh
Priority to BRPI0918144A priority patent/BRPI0918144A2/pt
Priority to JP2010528715A priority patent/JPWO2010029908A1/ja
Publication of WO2010029908A1 publication Critical patent/WO2010029908A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • 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
    • B01D69/08—Hollow fibre membranes
    • 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
    • B01D69/08—Hollow fibre membranes
    • B01D69/087—Details relating to the spinning process
    • 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
    • B01D71/66—Polymers having sulfur in the main chain, with or without nitrogen, oxygen or carbon only
    • B01D71/68—Polysulfones; Polyethersulfones
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2325/00—Details relating to properties of membranes
    • B01D2325/02—Details relating to pores or porosity of the membranes
    • B01D2325/021—Pore shapes

Definitions

  • the present invention relates to a hollow fiber membrane suitably used as a separation membrane for a water purifier and the like, and a method for producing the hollow fiber membrane.
  • hollow fiber membrane modules that perform filtration and dialysis of substances contained in the liquid to be treated have a large effective membrane area per unit volume, so water treatment related to microfiltration, ultrafiltration, etc., nitrogen It is used in many fields such as gas separation, oxygen, hydrogen, etc., medicine, biotechnology, etc.
  • Homogeneous membranes were the mainstream of hollow fiber membranes initially used, but membranes with an asymmetric structure provided with a dense layer have become mainstream as pursuing permeability.
  • a hollow fiber membrane having an asymmetric structure is formed using a double ring nozzle, and a liquid is injected into a central pipe to form a hollow shape. If a dense structure is formed on the inner surface side and has non-solidification properties, a dense layer is formed on the outer surface side in a coagulation bath provided on the downstream side.
  • spinning draft rate is defined as the ratio of the speed at which the film forming stock solution exits from the spinneret and the take-up speed of the produced hollow fiber membrane. The values are very different.
  • Patent Document 1 discloses a method for producing a porous fiber having a spinning draft rate of 100 or 185.
  • this document is based on a melt spinning method in which film formation is stable even at a high spinning draft rate.
  • the film formation is stable at a high spinning draft rate. This is considered because the polymer, which is the film forming composition, is oriented as it is drafted, and the strength of the hollow fiber membrane is increased.
  • Patent Document 2 since the production becomes unstable if the spinning draft rate is extremely increased or decreased, the spinning draft rate is usually set in the range of 2 to 5, Patent Document 3 also describes that the spinning draft rate is in the range of 10 to 300% (0.1 to 3) for the same reason. Further, Patent Document 4 points out a problem that the inner surface of the hollow fiber is torn only when the spinning draft rate exceeds 2, and the substance to be removed easily leaks. Further, when the balance between polymer aggregation and spinning draft is lost, in an extreme example, the inner surface has a star-shaped structure and the outer surface has a pleated structure, and problems such as yarn breakage are likely to occur.
  • Patent Document 5 describes that the spinning draft rate is 5 or more.
  • this method is considered to be a membrane-forming method by a thermally induced phase separation method, although it is not specified. Since the method of forming a hollow fiber membrane having an asymmetric structure by the phase separation method does not coagulate while the polymer components are oriented, the same concept cannot be applied.
  • the phase separation method is a kind of membrane preparation method.
  • the former is a method of inducing phase separation by giving a temperature change to a uniform polymer solution.
  • a membrane with a uniform structure is used in the production of a hollow fiber membrane.
  • This is a method suitable for film formation.
  • the latter is a method of inducing phase separation by adding a non-solvent composition to a uniform polymer solution, and is a method suitable for forming an asymmetric membrane by controlling the interface conditions such as inside and outside.
  • An object of this invention is to provide the manufacturing method of the hollow fiber membrane which can be applied industrially and can increase the filling membrane area in a hollow fiber membrane module, and can improve a turbidity elimination performance.
  • a method for producing a hollow fiber membrane characterized in that when a hollow fiber membrane having an asymmetric structure is produced by a liquid injection method using a double ring nozzle, the membrane is produced with a spinning draft rate of 6 or more and 13 or less.
  • the viscosity of the membrane-forming stock solution obtained by dissolving the constituent components of the hollow fiber membrane in an organic solvent is 1 Pa ⁇ s or more and 10 Pa ⁇ s or less. .
  • the “aspect ratio of the holes formed on the film surface” refers to the dimension ratio of the formed holes in the vertical / lateral directions.
  • the longitudinal direction refers to the longitudinal direction of the hollow fiber membrane
  • the lateral direction refers to a direction within the surface of the hollow fiber membrane and perpendicular to the longitudinal direction of the hollow fiber membrane.
  • the present invention it is possible to produce a hollow fiber membrane having a small diameter without being forced to change the die, and therefore it can be applied industrially.
  • a hollow fiber membrane when such a hollow fiber membrane is incorporated into a module at the same filling rate as a module loaded with a conventional large-diameter hollow fiber membrane, the filled membrane area can be increased and more than the increase in membrane area can be removed. Turbidity can be improved. Therefore, as a cartridge, the replacement frequency is low, the energy load for disposal of such a cartridge can be reduced, and it is environmentally friendly.
  • the present invention is a method for producing a hollow fiber membrane having an asymmetric structure by a liquid injection method using a double ring nozzle, for example, by a non-solvent induced phase separation method, and forming a film on an outer peripheral slit portion of the double ring nozzle
  • the stock solution is injected into the center pipe with a liquid such as non-solidifying to form a hollow shape.
  • the film-forming stock solution is discharged from a double ring nozzle together with, for example, a non-coagulable liquid, and after running idle in a predetermined section, is led to a coagulation bath provided on the downstream side.
  • the hollow fiber membrane solidified into a hollow shape by the coagulation bath is washed with water and then wound up in a skein.
  • a hollow fiber membrane constituent component such as a polysulfone polymer is dissolved in the membrane forming stock solution.
  • a polysulfone-based polymer is a polymer composed of repeating units of the following formula (1) or (2), but a functional group may be added to a part of the skeleton, and is not limited thereto.
  • solvents such as dimethyl sulfoxide, dimethylacetamide, dimethylformamide, N-methyl-2-pyrrolidone, dioxane and the like are used, and in particular, dimethylacetamide, dimethyl sulfoxide, dimethylformamide, N -Methyl-2-pyrrolidone is desirable and may be appropriately selected according to the viscosity of the film-forming stock solution and the coagulability of the injected liquid.
  • the viscosity of the film-forming stock solution in the double ring nozzle is preferably 1 Pa ⁇ s or more and 10 Pa ⁇ s or less.
  • An excessively high viscosity of the film-forming stock solution is not preferable because the pressure in the spinneret becomes too high, and a stable discharge state cannot be maintained.
  • the viscosity of the film-forming stock solution is too low, the spinnability is lowered, so that yarn breakage occurs before the film structure is formed, which is not preferable. More preferably, it is the range of 2 Pa ⁇ s or more and 8 Pa ⁇ s or less.
  • an additive can be added to the film-forming stock solution.
  • a hollow fiber membrane for a water purifier is preferably used because the hollow fiber membrane itself becomes hydrophilic by adding a hydrophilic polymer.
  • a hydrophilic polymer Considering the affinity with the polysulfone resin, polyvinyl pyrrolidone and polyethylene glycol are most preferable.
  • the addition amount can be reduced as compared with the case of using a hydrophilic polymer having a small molecular weight. Therefore, by examining the molecular weight of the hydrophilic polymer, Viscosity adjustment can also be performed.
  • the liquid to be injected into the center pipe is appropriately selected from solid or non-solid according to the desired form of the hollow fiber membrane.
  • This coagulation value represents the added weight of the injection liquid when the injection solution is added little by little to 50 g of the 1% by weight main polymer solution constituting the membrane and the system becomes cloudy. It shows that the solidification property of injection
  • a solidifying liquid When a solidifying liquid is used as such a liquid, solidification starts from the inner surface, so that a dense layer is formed on the inner surface side of the hollow fiber membrane.
  • a non-solidifying liquid solidification starts from the outer surface by the coagulation bath provided on the downstream side, so that a dense layer is formed on the outer surface side of the hollow fiber membrane.
  • the liquid in the coagulation bath is preferably composed mainly of water because it is inexpensive.
  • a mixture of water and a solvent of the polymer composition is preferably used, but an additive such as a dispersant can also be added.
  • the spinning draft rate is 6 or more and 13 or less in the above-described steps.
  • the spinning draft rate is a ratio between the discharge linear velocity of the film forming composition from the outer peripheral slit portion of the double ring nozzle and the winding speed of the hollow fiber, and the winding speed is the discharge linear velocity of the film forming composition. Indicates the value divided by.
  • the discharge linear velocity is a linear velocity when the film-forming composition is discharged from the outer peripheral slit of the double ring nozzle, and is a value obtained by dividing the discharge flow rate by the outer slit sectional area.
  • a low spinning draft rate means that the outer slit width is small, but in this case, when the spinning speed is increased, the pressure loss at the spinneret becomes high and a stable discharge state cannot be maintained. The membrane structure is disturbed, causing problems in quality such as water permeability and fractionation performance. Furthermore, since the difficulty of manufacturing a double ring nozzle with a small slit width increases, problems such as high costs arise.
  • the spinning draft rate is too high, when the injected liquid has coagulability, the hollow fiber inner surface cannot be maintained hollow due to the influence of the spinning draft, and the smoothness of the inner surface is lost. A polygonal structure such as a shape is formed, which is not preferable. Further, when the injected liquid has non-coagulability, the outer surface of the hollow fiber is affected by the spinning draft, the smoothness of the outer surface is lost, and a pleated structure is formed, which is not preferable.
  • a parameter for confirming the influence of the spinning draft rate is the aspect ratio of the hole formed on the surface.
  • the definition of the aspect ratio is as described above. Generally, when the draft rate is high, the aspect ratio tends to be high.
  • a film having an asymmetric structure in which a dense layer is formed on one of the inner side and the outer side is formed.
  • the porosity on the surface on which the layer is formed is 8% or more and 14% or less. Furthermore, 10% or more and 13% or less are more preferable.
  • the aspect ratio of the pores formed on the membrane surface on the side having the dense layer of the hollow fiber membrane is 3 or more and 5 or less. Furthermore, 3 or more and 4 or less are more preferable ranges.
  • the membrane of the present invention having the above-mentioned aperture ratio or aspect ratio is used for a water purifier, it becomes possible to improve the turbidity performance more than the membrane area increment.
  • the turbidity removal performance is a numerical value until turbidity accumulates and the filtration flow rate falls below a certain value, and is usually considered to be proportional to the membrane area. However, it has been found that by using the hollow fiber membrane formed according to the present invention, the turbidity is improved beyond the membrane area.
  • the turbidity is improved more than the membrane area
  • a 0.3 ⁇ m hole is formed in a perfect circle shape
  • water stops flowing through the hole if the hole is affected by the draft, even if 0.3 ⁇ m particles are captured at the center of the hole, water will still flow at both ends in the longitudinal direction of the hole.
  • the influence of the draft is the largest on the outermost surface, but even a little inside it, it is affected by the draft, and the part that can be filtered still remains after the particles are trapped.
  • the surface area on the dense layer side is 8% or more and 14% or less, or the surface pore aspect ratio is 3 or more and 5 or less.
  • the three-dimensional structure of the pores is formed due to the influence of the draft, and it is expected that the turbidity is improved for the reasons described above.
  • the aspect ratio is 5 or more, it is considered that the spinning draft rate is too high, and the discharge of the film forming solution becomes unstable, which is not preferable.
  • the dense layer does not necessarily need to be the outermost surface of the film.
  • the dense layer is provided in a portion slightly inside from the outer surface by controlling the dry part conditions, the thickness of the dense layer can be reduced and the film can be transmitted. It is also preferable from the viewpoint of improved properties.
  • the porosity of the other side of the membrane where the dense layer is not formed needs to be higher than that of the dense layer because it does not contribute much to the permeation resistance of the membrane. If the opening rate is too high, the strength of the hollow fiber membrane decreases, and the opening rate is preferably 15% or more and 20% or less, and more preferably 16% or more and 20% or less.
  • Macrovoids are pores that are clearly larger than the surrounding holes, and are often regarded as structural defects because they significantly reduce pressure resistance.
  • the obtained hollow fiber membrane is preferable because it can be processed into a cartridge by a known method and treated as a water purifier because more water can be treated while maintaining removal performance such as turbidity and iron rust.
  • the method for measuring the viscosity of the membrane-forming stock solution and the method for testing the turbidity of the water purifier cartridge are as follows.
  • Turbidity removal performance test of water purifier cartridge It evaluated along the method shown by JIS S3200 (1999).
  • Measurement of Opening Ratio on Hollow Fiber Membrane Surface A 3000 times image of the outer surface of the hollow fiber membrane was taken with a field emission scanning electron microscope (S-800, manufactured by Hitachi, Ltd.).
  • the hollow fiber membrane is influenced by the draft, it is suitable for grasping the structural characteristics when installed in the longitudinal direction.
  • the image size was 655 ⁇ 740 pixels.
  • Image processing was performed with Matrox Inspector 2.2 (Matrox Electronic Systems Ltd.).
  • the hole portion was turned white and the others were turned black, and the number of pixels in the white portion was measured.
  • the binarization boundary level was set to an intermediate value between the difference between the whitest part and the blackest part.
  • the sum of the pixels in each hole portion (total opening area) was divided by the number of pixels in the entire image, and the percentage expressed as a percentage.
  • Opening ratio (%) (total number of pixels in each hole) / (number of pixels in the entire image) ⁇ 100 Since the resolution of the image was 0.046948 ⁇ m / pixel, the area S of the electron microscope image was calculated to be 1068.4 ⁇ m 2 .
  • the average hole diameter counted the number of the holes displayed white, and measured the pixel number of each hole. When the number of pixels of the hole was 2 pixels or less, it was removed as noise.
  • the length in the direction of the longer length of each hole is the length in the vertical direction (that is, the length in the major axis direction in the case of an ellipse).
  • the apex of the longer length of the hole is determined, and the length of the line connecting the apexes is the vertical length of the hole.
  • the horizontal length is the length in the direction perpendicular to the vertical direction, and the length of the longest portion of the hole in the horizontal direction is taken.
  • Example 1 15 parts by weight of polysulfone (hereinafter referred to as PSf, manufactured by BASF: Ultrason S6010), 7 parts by weight of polyvinylpyrrolidone (hereinafter referred to as PVP, ISP, K-90: molecular weight 1,200,000), 75 parts by weight of dimethylacetamide (hereinafter referred to as DMAc) and water 3 A part by weight was dissolved and stirred to prepare a stock solution. The viscosity of this film-forming stock solution at 40 ° C. was 3.4 Pa ⁇ s.
  • This film-forming stock solution was discharged from a double ring nozzle having an outer peripheral slit width of 0.15 mm maintained at 40 ° C., passed through a predetermined dry length, and then wound up at 36 m / min through a coagulation and water washing process. .
  • the discharge amount of the membrane forming stock solution was adjusted so that the thickness of the hollow fiber membrane was 0.07 mm and the outer diameter was 0.36 mm.
  • the discharge linear velocity of the double ring nozzle obtained by dividing the discharge amount from the double ring nozzle by the discharge cross-sectional area was 5.4 m / min, and the spinning draft rate at this time was 6.7.
  • FIGS. 1A and 1B are SEM photographs of the outer surface and the inner surface of the film obtained in Example 1, respectively.
  • the porosity of the film was measured from these, the porosity of the outer surface was 13.4%, the porosity of the inner surface was 18.9%, and no macrovoids were formed on both sides of the film. It was.
  • a white broken line thick frame portion in FIG. 1A indicates a 20 ⁇ m image area, and 20 holes are extracted in the order of increasing vertical length of the hole formed in the outermost surface on the outer membrane surface side (FIG. 1 ⁇ c)
  • the aspect ratio was 3.3
  • the vertical dimension was 11.1 mm (actual size: 2.9 ⁇ m).
  • Example 2 A hollow fiber membrane was formed in the same manner as in Example 1, and the discharge amount of the membrane forming stock solution was adjusted so that the thickness of the hollow fiber membrane was 0.065 mm and the outer diameter was 0.35 mm. The spinning draft rate at this time was 7.0.
  • the obtained hollow fiber membrane had an asymmetric structure, and a dense structure was formed on the outer surface.
  • FIGS. 2-a and 2-b are SEM photographs of the outer surface and the inner surface of the film obtained in Example 2, respectively. When the porosity was measured from these, the porosity on the outer surface was 13.7%, the porosity on the inner surface was 17.1%, and no macrovoids were formed on both sides of the film.
  • Holes formed on the outer surface of the hollow fiber membrane were extracted from the white broken line thick frame portion of FIG. 2-a in the same manner as in Example 1 (FIG. 2-c), and the aspect ratio was measured. 7.
  • the vertical dimension was 13.0 mm (actual size 3.4 ⁇ m).
  • 1032 hollow fiber membranes were bundled, made into a U shape, potted, filled into a cartridge case, filled with activated carbon, and used as a water purifier cartridge.
  • the membrane area of the cartridge was 0.086 m 2 and the turbidity removal performance was 1400 L. Compared to Comparative Example 2, the membrane area was increased by 30%, but the turbidity was improved by 82%.
  • Example 1 A hollow fiber membrane was formed in the same manner as in Example 1 except that the thickness of the hollow fiber membrane was 0.08 mm and the outer diameter was 0.46 mm. The spinning draft rate at this time was 4.2. A dense structure was formed on the outer surface of the hollow fiber membrane. From the SEM photographs of the outer surface and inner surface of the film obtained in Comparative Example 1, from FIG. 3-a and FIG. 3-b, the outer surface has a hole area ratio of 14.5% and the inner surface hole area ratio. Was 19.2%, and no macrovoids were formed on both sides of the film.
  • FIG. 3A holes formed on the outer surface of the hollow fiber membrane were extracted in the same manner as in Example 1 (FIG. 3C) and the aspect ratio was measured. 4.
  • the vertical dimension was 9.6 mm (actual size 2.5 ⁇ m).
  • 888 hollow fiber membranes were bundled to form a water purifier cartridge having the same shape as in Example 1.
  • the membrane area of the cartridge was 0.12 m 2 and the turbidity removal performance was 2400 L.
  • the membrane area of the cartridge was 0.066 m 2 and the turbidity removal performance was 770 L.
  • the hollow fiber membrane was prepared to have a film thickness of 0.04 mm, and the hollow fiber membrane was tried to be wound at a spinning draft ratio of 13.3. However, the yarn could not be wound because the yarn breakage occurred repeatedly.
  • Example 1 and Comparative Example 1 are cartridges having the same shape.
  • the membrane area was increased by 20%, but the turbidity was improved by 38%, and an effect equal to or greater than the membrane area could be obtained.
  • Example 2 and Comparative Example 2 are cartridges having the same shape.
  • the membrane area is increased by 30%, but the turbidity is improved by 82%, and an effect equal to or greater than the membrane area can be obtained.

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

Abstract

L'invention concerne un module muni d'une membrane fibre creuse qui possède une couche dense à l'intérieur ou à l'extérieur et pour laquelle les rapports longueur/diamètre des pores formés sur la surface du côté à couche dense de la membrane sont de 3 à 5. Le module exerce une performance de purification supérieure à celle prévue par une augmentation de l'aire de la membrane et peut réduire la fréquence de remplacement de la cartouche.
PCT/JP2009/065631 2008-09-10 2009-09-08 Membrane fibre creuse et procédé de fabrication d’une membrane fibre creuse Ceased WO2010029908A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
CN200980135265.XA CN102149449B (zh) 2008-09-10 2009-09-08 中空丝膜及中空丝膜的制造方法
BRPI0918144A BRPI0918144A2 (pt) 2008-09-10 2009-09-08 membrana de fibra oca e processo para a produção de membrana de fibra oca
JP2010528715A JPWO2010029908A1 (ja) 2008-09-10 2009-09-08 中空糸膜及び中空糸膜の製造方法

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2008-231853 2008-09-10
JP2008231853 2008-09-10

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WO2010029908A1 true WO2010029908A1 (fr) 2010-03-18

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PCT/JP2009/065631 Ceased WO2010029908A1 (fr) 2008-09-10 2009-09-08 Membrane fibre creuse et procédé de fabrication d’une membrane fibre creuse

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JP (1) JPWO2010029908A1 (fr)
CN (1) CN102149449B (fr)
BR (1) BRPI0918144A2 (fr)
TW (1) TWI472370B (fr)
WO (1) WO2010029908A1 (fr)

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JP2014073487A (ja) * 2012-09-11 2014-04-24 Toray Ind Inc 多孔質膜、多孔質膜を内蔵する浄水器および多孔質膜の製造方法
WO2014148470A1 (fr) * 2013-03-21 2014-09-25 旭化成ケミカルズ株式会社 Membrane à fibres creuses multiporeuses et procédé pour produire la membrane à fibres creuses multiporeuses
JP2015013228A (ja) * 2013-07-03 2015-01-22 東レ株式会社 中空糸膜およびその製造方法
WO2015046411A1 (fr) 2013-09-30 2015-04-02 東レ株式会社 Membrane poreuse, module de purification du sang comprenant une membrane poreuse, et procédé de production de membrane poreuse
JPWO2014156644A1 (ja) * 2013-03-28 2017-02-16 東レ株式会社 多孔質膜および浄水器
WO2017164019A1 (fr) * 2016-03-22 2017-09-28 東レ株式会社 Membrane à fibres creuses
CN112672814A (zh) * 2018-09-20 2021-04-16 住友电气工业株式会社 中空纤维膜
WO2025047238A1 (fr) * 2023-08-30 2025-03-06 日東電工株式会社 Corps poreux de type fibre creuse, membrane à fibres creuses, et procédé de fabrication de corps poreux de type fibre creuse

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JP7314797B2 (ja) * 2018-05-24 2023-07-26 東レ株式会社 多孔質中空糸膜
WO2020090494A1 (fr) * 2018-10-30 2020-05-07 東レ株式会社 Filière à membrane à fibres creuses et procédé de fabrication de membrane à fibres creuses

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS58114702A (ja) * 1981-12-28 1983-07-08 Kuraray Co Ltd ポリスルホン中空繊維膜
WO1990003210A1 (fr) * 1988-09-29 1990-04-05 Toray Industries, Inc. Membrane poreuse et procede de production
JPH04180824A (ja) * 1990-11-13 1992-06-29 Daicel Chem Ind Ltd 多孔性中空糸膜
JPH11179174A (ja) * 1997-12-19 1999-07-06 Toray Ind Inc 分離用中空糸膜およびその製造方法
JP3117575B2 (ja) * 1992-04-29 2000-12-18 株式会社クラレ ポリスルホン系中空繊維膜とその製造方法
JP2003038940A (ja) * 2001-07-30 2003-02-12 Toyobo Co Ltd 選択分離膜

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5340480A (en) * 1992-04-29 1994-08-23 Kuraray Co., Ltd. Polysulfone-based hollow fiber membrane and process for manufacturing the same
JP2006000810A (ja) * 2004-06-21 2006-01-05 Toray Ind Inc 中空糸膜の製造方法、中空糸膜およびそれを用いて得られる中空糸膜モジュール
US20080000830A1 (en) * 2004-08-10 2008-01-03 Kimihiro Mabuchi Highly Water Permeable Hollow Fiber Membrane Type Blood Purifier and Process for Manufacturing the Same
JP5218044B2 (ja) * 2006-03-09 2013-06-26 東洋紡株式会社 性能安定性に優れた中空糸膜および血液浄化器および中空糸膜の製造方法

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS58114702A (ja) * 1981-12-28 1983-07-08 Kuraray Co Ltd ポリスルホン中空繊維膜
WO1990003210A1 (fr) * 1988-09-29 1990-04-05 Toray Industries, Inc. Membrane poreuse et procede de production
JPH04180824A (ja) * 1990-11-13 1992-06-29 Daicel Chem Ind Ltd 多孔性中空糸膜
JP3117575B2 (ja) * 1992-04-29 2000-12-18 株式会社クラレ ポリスルホン系中空繊維膜とその製造方法
JPH11179174A (ja) * 1997-12-19 1999-07-06 Toray Ind Inc 分離用中空糸膜およびその製造方法
JP2003038940A (ja) * 2001-07-30 2003-02-12 Toyobo Co Ltd 選択分離膜

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2014073487A (ja) * 2012-09-11 2014-04-24 Toray Ind Inc 多孔質膜、多孔質膜を内蔵する浄水器および多孔質膜の製造方法
US10023709B2 (en) 2013-03-21 2018-07-17 Asahi Kasei Chemicals Corporation Multiporous hollow-fiber membrane and process for producing multiporous hollow-fiber membrane
WO2014148470A1 (fr) * 2013-03-21 2014-09-25 旭化成ケミカルズ株式会社 Membrane à fibres creuses multiporeuses et procédé pour produire la membrane à fibres creuses multiporeuses
JPWO2014148470A1 (ja) * 2013-03-21 2017-02-16 旭化成株式会社 多孔性中空糸膜及び多孔性中空糸膜の製造方法
JP2019048297A (ja) * 2013-03-28 2019-03-28 東レ株式会社 多孔質膜
JPWO2014156644A1 (ja) * 2013-03-28 2017-02-16 東レ株式会社 多孔質膜および浄水器
JP2015013228A (ja) * 2013-07-03 2015-01-22 東レ株式会社 中空糸膜およびその製造方法
WO2015046411A1 (fr) 2013-09-30 2015-04-02 東レ株式会社 Membrane poreuse, module de purification du sang comprenant une membrane poreuse, et procédé de production de membrane poreuse
JPWO2015046411A1 (ja) * 2013-09-30 2017-03-09 東レ株式会社 多孔質膜、多孔質膜を内蔵する血液浄化用モジュールおよび多孔質膜の製造方法
EP3053614A4 (fr) * 2013-09-30 2017-06-14 Toray Industries, Inc. Membrane poreuse, module de purification du sang comprenant une membrane poreuse, et procédé de production de membrane poreuse
KR102230435B1 (ko) * 2013-09-30 2021-03-22 도레이 카부시키가이샤 다공질막, 다공질막을 내장하는 혈액 정화용 모듈 및 다공질막의 제조 방법
KR20160065047A (ko) 2013-09-30 2016-06-08 도레이 카부시키가이샤 다공질막, 다공질막을 내장하는 혈액 정화용 모듈 및 다공질막의 제조 방법
KR20180122623A (ko) 2016-03-22 2018-11-13 도레이 카부시키가이샤 중공사막
JPWO2017164019A1 (ja) * 2016-03-22 2019-01-24 東レ株式会社 中空糸膜
KR102219541B1 (ko) 2016-03-22 2021-02-24 도레이 카부시키가이샤 중공사막
WO2017164019A1 (fr) * 2016-03-22 2017-09-28 東レ株式会社 Membrane à fibres creuses
CN112672814A (zh) * 2018-09-20 2021-04-16 住友电气工业株式会社 中空纤维膜
CN112672814B (zh) * 2018-09-20 2022-08-02 住友电气工业株式会社 中空纤维膜
US12115503B2 (en) 2018-09-20 2024-10-15 Sumitomo Electric Industries, Ltd. Hollow-fiber membrane
WO2025047238A1 (fr) * 2023-08-30 2025-03-06 日東電工株式会社 Corps poreux de type fibre creuse, membrane à fibres creuses, et procédé de fabrication de corps poreux de type fibre creuse

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TW201016306A (en) 2010-05-01
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