WO2011007714A1 - フッ化ビニリデン系樹脂多孔膜、その製造方法およびろ過水の製造方法 - Google Patents
フッ化ビニリデン系樹脂多孔膜、その製造方法およびろ過水の製造方法 Download PDFInfo
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- WO2011007714A1 WO2011007714A1 PCT/JP2010/061630 JP2010061630W WO2011007714A1 WO 2011007714 A1 WO2011007714 A1 WO 2011007714A1 JP 2010061630 W JP2010061630 W JP 2010061630W WO 2011007714 A1 WO2011007714 A1 WO 2011007714A1
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- WIPO (PCT)
- Prior art keywords
- vinylidene fluoride
- fluoride resin
- porous membrane
- plasticizer
- membrane
- Prior art date
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Images
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
- B01D71/30—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
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
-
- 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
- B01D67/0002—Organic membrane manufacture
- B01D67/002—Organic membrane manufacture from melts
-
- 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
-
- 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
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01D—MECHANICAL METHODS OR APPARATUS IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS
- D01D5/00—Formation of filaments, threads, or the like
- D01D5/24—Formation of filaments, threads, or the like with a hollow structure; Spinnerette packs therefor
-
- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
- D01F1/00—General methods for the manufacture of artificial filaments or the like
- D01F1/02—Addition of substances to the spinning solution or to the melt
- D01F1/10—Other agents for modifying properties
-
- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
- D01F6/00—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof
- D01F6/44—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from mixtures of polymers obtained by reactions only involving carbon-to-carbon unsaturated bonds as major constituent with other polymers or low-molecular-weight compounds
- D01F6/48—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from mixtures of polymers obtained by reactions only involving carbon-to-carbon unsaturated bonds as major constituent with other polymers or low-molecular-weight compounds of polymers of halogenated hydrocarbons
-
- 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
-
- 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
- B01D2325/0283—Pore size
- B01D2325/02834—Pore size more than 0.1 and up to 1 µm
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Definitions
- the present invention is suitable as a porous membrane for separation, and in particular, (filtration) a porous membrane made of a vinylidene fluoride resin excellent in contamination resistance and regenerative performance in addition to water treatment performance, a method for producing the same, and filtered water using the same It relates to a manufacturing method.
- Patent Documents 1 and 2 disclose non-solvent-induced phase separation in which a vinylidene fluoride resin solution is brought into contact with a liquid (generally a vinylidene fluoride resin nonsolvent) that solidifies the vinylidene fluoride resin solution.
- a method for producing a porous membrane by the method is disclosed.
- it is easy to form a film on the film surface due to slow diffusion of non-solvent in the film (mass transfer), and the surface of the water to be treated has a high resin concentration (that is, low porosity). ) give a porous membrane.
- Patent Document 3 discloses that a relatively large amount of an organic liquid which is incompatible with vinylidene fluoride resins such as dioctyl phthalate and dibutyl phthalate is dispersed in vinylidene fluoride resin together with silica powder in the organic resin after molding. Disclosed is a method of forming a porous membrane by extracting and removing liquid and silica powder.
- the present inventors also melt-extruded a vinylidene fluoride resin having a specific molecular weight characteristic into a hollow fiber shape together with a plasticizer and a good solvent of the vinylidene fluoride resin, and then perform extraction removal and stretching of the plasticizer.
- a plasticizer and a good solvent of the vinylidene fluoride resin
- Patent Documents 7 to 10 and others there is a strong demand for further improvement with respect to the overall performance including the filtration performance and mechanical performance required when the porous membrane is used as a filter permeation membrane.
- MF microfiltration
- the average pore size is 0.25 ⁇ m or less, and there is little contamination (clogging) with organic substances during continuous filtration operation of turbid water, and a high water permeability is maintained. It is desirable.
- the porous membrane disclosed in the following Patent Document 6 has an excessive average pore diameter
- the hollow fiber porous membrane disclosed in the following Patent Document 8 has a problem in maintaining the amount of water permeation in the continuous filtration operation of muddy water. Remain.
- JP-A 63-296940 JP 2005-220202 A Japanese Patent Laid-Open No. 3-215535 JP 7-173323 A WO01 / 28667A WO02 / 070115A WO2005 / 099879A WO2007 / 010932A WO2008 / 117740A Specification of PCT / JP2009 / 071450
- the present invention has a surface pore size, liquid permeability (water permeability) and mechanical strength suitable for separation applications, particularly (filter) water treatment, and has a good fluid permeability maintenance performance even during continuous separation treatment.
- An object of the present invention is to provide a vinylidene fluoride resin porous membrane.
- a further object of the present invention is to prevent contamination even during continuous filtration of turbid water, maintain a good water permeability and, if necessary, easily reduce the filtrate pressure increased by continuous filtration by chemical treatment.
- An object of the present invention is to provide a vinylidene fluoride resin porous membrane having excellent reproducibility.
- a further object of the present invention is to provide an efficient method for producing the above-mentioned vinylidene fluoride resin porous membrane and a method for producing filtered water using the same.
- the present invention is intended to achieve the above-mentioned object mainly by controlling the physical fine structure in the vicinity of the surface of the porous film to be treated.
- the present inventors achieved this object through analysis using a focused ion beam / scanning electron microscope (hereinafter referred to as “FIB-SEM”).
- FIB-SEM focused ion beam / scanning electron microscope
- the fact that the liquid treatment performance of the porous membrane is influenced by the microstructure of the surface to be treated can be easily inferred.
- the conventional SEM method conventionally used for such structural analysis is unsatisfactory for the above-mentioned purpose.
- the first reason is that the observation object in the normal SEM method is a sample cross section exposed by cutting with a microtome, but the cross-section is damaged by rubbing with the microtome, and the fine structure is lost.
- FIB-SEM method is similar to the normal SEM method in that a sample cross section (about 10 ⁇ 10 ⁇ m) exposed by microtome cutting or mechanical polishing is irradiated with a focused ion beam (FIB) such as Ga (gallium). Since the SEM observation is performed on the sample surface after the thickness of about 20 nm of the cross-sectional surface layer disturbed by the microtome or the like is removed, the cross-sectional observation of the original structure of the sample is possible.
- FIB focused ion beam
- the update of the sample cross-section by FIB irradiation can be repeatedly performed approximately 20 nm at almost the same location, so that a three-dimensional analysis of the vicinity of the surface layer of the vinylidene fluoride resin porous membrane is possible by stacking plane images at the same location. Become.
- the vinylidene fluoride resin porous membrane of the present invention has a surface pore size P1 of 0.30 ⁇ m or less that has already been confirmed by normal SEM observation.
- the vinylidene fluoride resin porous membrane of the present invention has an average diameter of network resin fibers of 100 nm or less and pores in a portion having a thickness of 10 ⁇ m continuous from one surface measured by a focused ion beam / scanning electron microscope.
- the rate A1 is 60% or more
- the one-surface-side surface pore diameter P1 is 0.3 ⁇ m or less.
- the part having a thickness of 10 ⁇ m continuous from one surface having the above-described fine structure may be referred to as “one surface (treated water) side surface layer” or simply “surface layer”.
- the vinylidene fluoride resin porous membrane of the present invention has the surface layer having the above-mentioned fine structure, in addition to the fine particle blocking performance understood by a small surface pore diameter, contamination during liquid treatment (especially filtered water) operation. It has been confirmed that (clogging) prevention and regeneration performance when necessary are extremely excellent.
- the mechanism that the present inventors presume to explain this point is described below.
- the MBR method membrane separation activated sludge method in which the porous membrane of the present invention, which is an MF (microfiltration) membrane, exhibits particularly excellent suitability. ) As an example.
- the main membrane dirt components in the MBR method are (a) a suspended matter having a particle size of several ⁇ m to several hundreds of ⁇ m, and (b) a particle size distribution having a peak at 0.2 ⁇ m to 0.5 ⁇ m as an example. And (c) several mg / L to several tens mg / L of dissolved organic components contained in the water to be treated. (I) Suspended particles are pressed against the membrane surface during filtration, and this pressing force increases as the water flux to be treated passing through the membrane surface increases, and the porosity in the vicinity of the surface layer of the porous membrane of the present invention is high.
- A1 acts in the direction of reducing the water flux to be treated passing through the membrane surface, and hence the pressing force of the suspended particles on the membrane surface.
- the pressing force of the suspended solid particles on the membrane surface is small, the suspended solid particles and the membrane flow together with the upward flow. It is understood that the possibility of being removed from the surface is great.
- the surface pore size of the membrane is larger than that of the colloidal particles, the colloidal particles fit completely into the pores or bridge inside the membrane, resulting in clogging of the membrane, resulting in a significant increase in filtration resistance.
- the porous membrane of the present invention having a surface pore diameter of 0.3 ⁇ m or less is less likely to cause clogging due to such colloidal particles.
- the above-mentioned (a) suspended particles and (b) colloidal particles may be deposited on the film surface to form a compacted cake layer, but the porous film of the present invention is unlikely to form such a cake layer. Has been confirmed (see Examples below).
- (C) The dissolved organic component in the water to be treated is adsorbed over the entire surface of the membrane including the inside of the pores over time, gradually reducing the pores, and increasing the filtrate pressure.
- CIP Clean In Place, in-device cleaning or chemical injection backwashing, in which a chemical solution is injected from the filtered water side for several minutes to several tens of minutes. It is possible to efficiently remove dissolved components adsorbed by the method, and in particular, it has been confirmed that the CIP treatment proceeds very smoothly in the porous membrane of the present invention with little cake layer formation (described later). See Examples).
- the method for producing filtrate of the present invention applies the porous membrane of the present invention to the MBR method and / or the CIP method, and more specifically uses the vinylidene fluoride resin porous membrane of the present invention.
- the water to be treated is filtered, filtration and aeration of the surface of the porous membrane to be treated are performed simultaneously or alternately, and if necessary, the filtered water side of the vinylidene fluoride resin porous membrane
- the method further includes the step of injecting a chemical solution from the step of cleaning the film.
- a plasticizer that forms a melt-kneaded composition before cooling by melt-kneading with the vinylidene fluoride-based resin. More specifically, it is compatible with the vinylidene fluoride resin under heating (melt kneading composition formation temperature) and is almost equivalent to the crystallization temperature Tc (° C.) of the vinylidene fluoride resin alone in the melt kneading composition.
- a relatively large amount of a polyester plasticizer that gives a crystallization temperature Tc ′ (° C.) of the resin is melt-kneaded with a high molecular weight vinylidene fluoride resin, and the formed film is cooled and solidified from one side, and then plasticized. It has been found that it is preferable to form an asymmetric reticulated resin porous membrane by extracting the agent. From this viewpoint, a small amount of a plasticizer that lowers the Tc of the vinylidene fluoride resin as in Patent Document 4 is added; a spherulite is formed using a plasticizer that decreases the Tc of the vinylidene fluoride resin as in Patent Document 5.
- a composition obtained by adding 50 to 80% by weight of a plasticizer and melt-kneading is melt-extruded into a film shape, and preferentially cooled and solidified from one side with a liquid inert to vinylidene fluoride resin.
- the plasticizer has compatibility with the vinylidene fluoride resin at the formation temperature of the melt-kneaded composition
- the vinylidene fluoride resin Is a polyester plasticizer that gives a crystallization temperature substantially equal to the crystallization temperature of the vinylidene fluoride resin alone to the kneaded product
- a porous membrane after extraction of the plasticizer is at least 5 ⁇ m from the outer surface, and the membrane thickness It is characterized in that it comprises the step of stretching in a state of selectively moistened to 1/2 or less of the depth.
- the method for producing a vinylidene fluoride resin porous membrane of the present invention described above is a heat-induced phase separation method using a difference between a high crystallization temperature and a cooling temperature of a melt-kneaded product of a vinylidene fluoride resin and a polyester plasticizer. It is a manufacturing method of the vinylidene fluoride resin porous membrane by this.
- a vinylidene fluoride resin solution as disclosed in Patent Document 1 or 2 is brought into contact with a coagulating liquid (generally a non-solvent of vinylidene fluoride resin) to be solidified.
- a coagulating liquid generally a non-solvent of vinylidene fluoride resin
- FIG. 2 is a FIB-SEM binarized image showing a cross-sectional structure of the hollow fiber porous membrane obtained in Example 1.
- FIG. 2 is a FIB-SEM binarized image showing a cross-sectional structure of the hollow fiber porous membrane obtained in Comparative Example 1.
- FIG. 7 is a FIB-SEM binarized image showing a cross-sectional structure of a hollow fiber porous membrane used in Comparative Example 2.
- the porous membrane of the present invention can be formed on either a flat membrane or a hollow fiber membrane, but is preferably formed as a hollow fiber membrane that can easily increase the membrane area per liquid treatment (filtration) device.
- the vinylidene fluoride resin as the main film raw material is a homopolymer of vinylidene fluoride, that is, polyvinylidene fluoride, a copolymer with other monomers copolymerizable with vinylidene fluoride, or a mixture thereof. And those having a weight average molecular weight of 300,000 or more, particularly 500,000 to 800,000 are preferably used.
- the monomer copolymerizable with vinylidene fluoride one or more of ethylene tetrafluoride, hexafluoropropylene, ethylene trifluoride, ethylene trifluoride chloride, vinyl fluoride and the like can be used.
- the vinylidene fluoride resin preferably contains 70 mol% or more of vinylidene fluoride as a structural unit. Among them, it is preferable to use a homopolymer composed of 100 mol% of vinylidene fluoride because of its high crystallization temperature Tc and high mechanical strength.
- the relatively high molecular weight vinylidene fluoride resin as described above can be obtained by emulsion polymerization or suspension polymerization, particularly preferably suspension polymerization.
- the vinylidene fluoride resin has a considerably large molecular weight of 300,000 or more, preferably 500,000 or more as described above.
- the resin has a melting point Tm2 (° C.) and is crystallized by DSC measurement. It is preferable that the difference Tm2 ⁇ Tc from the temperature Tc (° C.) has good crystal characteristics represented by 32 ° C. or less, more preferably 30 ° C. or less, and still more preferably 28 ° C. or less.
- the original melting point Tm2 (° C.) of the resin is distinguished from the melting point Tm1 (° C.) measured by subjecting the obtained sample resin or the resin forming the porous film to the temperature rising process by DSC as it is. It is. That is, generally-available vinylidene fluoride resins exhibit a melting point Tm1 (° C.) different from the original melting point Tm2 (° C.) due to the heat and mechanical history received during the manufacturing process or thermoforming process.
- the original melting point Tm2 (° C.) of the resin is found again in the DSC temperature raising process after the obtained sample resin is once subjected to a predetermined heating and cooling cycle to remove heat and mechanical history. It is defined as the melting point (endothermic peak temperature accompanying crystal melting), and the details of the measurement method will be described prior to the description of Examples described later.
- the above-mentioned vinylidene fluoride resin satisfying the condition of Tm2-Tc ⁇ 32 ° C. is preferably selected from the above-mentioned vinylidene fluoride resin species as a raw material, and has a weight average molecular weight of 200,000 to 670,000, Preferably 300,000-650,000, more preferably 400,000-600,000 medium high molecular weight vinylidene fluoride resin for matrix (PVDF-I) 25-98 wt%, preferably 50-95 wt%, more preferably Fluoride for crystal property modification having an ultra-high molecular weight of 60 to 90% by weight and having a weight average molecular weight of 1.8 times or more, preferably 2 times or more, and 1.2 million or less of a medium high molecular weight vinylidene fluoride resin.
- PVDF-I matrix
- Fluoride for crystal property modification having an ultra-high molecular weight of 60 to 90% by weight and having a weight average molecular weight of 1.8 times or more
- the vinylidene resin (PVDF-II) is provided as a mixture of 2 to 75% by weight, preferably 5 to 50% by weight, and more preferably 10 to 40% by weight.
- the medium high molecular weight component keeps the molecular weight level of the entire vinylidene fluoride resin high, and gives a hollow fiber porous membrane excellent in strength and water permeability. In other words, it acts as a matrix resin component.
- the ultra high molecular weight component is combined with the above medium high molecular weight component to crystallize the kneaded product with the crystallization temperature Tc of the raw material resin (generally about 140 ° C. for vinylidene fluoride homopolymer) and the plasticizer described later.
- the viscosity of the melt-extruded composition is increased and reinforced to enable stable extrusion in the form of hollow fibers.
- Tc preferential cooling from the outer surface of the hollow fiber membrane formed by melt extrusion promotes the reduction of the membrane surface pore diameter, and the cooling from the inside of the membrane to the inner surface is slower than the membrane surface. It becomes possible to accelerate the solidification of the vinylidene fluoride resin and to suppress the growth of spherulites.
- Tc is preferably 143 ° C. or higher, more preferably 145 ° C. or higher.
- the Tc of the vinylidene fluoride resin used does not substantially change during the production process of the hollow fiber membrane. Therefore, the obtained hollow fiber porous membrane can be measured as a sample by the DSC method described later.
- the Mw of the ultra high molecular weight vinylidene fluoride resin (PVDF-II) is less than 1.8 times the Mw of the medium high molecular weight resin (PVDF-I), it is difficult to sufficiently suppress the formation of spherulites. If it exceeds 10,000, it is difficult to uniformly disperse in the matrix resin.
- any of the above-mentioned medium and ultra high molecular weight vinylidene fluoride resins can be obtained by emulsion polymerization or suspension polymerization, particularly preferably suspension polymerization.
- the amount of the ultra high molecular weight vinylidene fluoride resin is less than 2% by weight, the effect of suppressing spherulite and the effect of thickening and reinforcing the melt-extruded composition are not sufficient, while if it exceeds 75% by weight, the vinylidene fluoride is added. There is a tendency that the phase separation structure of the base resin and the plasticizer becomes excessively fine, and the water permeability of the resulting porous membrane decreases, and further, stable film formation becomes difficult due to the occurrence of melt fracture during processing. .
- a plasticizer is added to the above-mentioned vinylidene fluoride resin to form a raw material composition for film formation.
- the hollow fiber porous membrane of the present invention is mainly formed from the above-mentioned vinylidene fluoride resin, but in addition to the above-mentioned vinylidene fluoride resin, at least the plasticizer is used as a pore-forming agent for the production. It is preferable.
- the plasticizer is compatible with the vinylidene fluoride resin at the melt kneading temperature. However, the crystallization temperature Tc (° C.) of the vinylidene fluoride resin alone is added to the melt kneaded product with the vinylidene fluoride resin.
- a crystallizing temperature Tc ′ (° C.) that is substantially the same as (ie, within ⁇ 5 ° C., preferably within ⁇ 4 ° C., more preferably within ⁇ 2 ° C.).
- a plasticizer those selected from polyester-based plasticizers composed of dibasic acid and glycol are generally used. Particularly, the number average molecular weight (saponification value and hydroxyl value measured in accordance with JIS K0070) is used. (Based on calculation) is preferably 1200 or more, more preferably 1500 or more, and still more preferably 1700 or more. As the molecular weight of the polyester plasticizer increases, the compatibility with the vinylidene fluoride resin tends to increase.
- the plasticizer can be extracted and removed in the extraction step described later. Since it may take time, a plasticizer having a number average molecular weight exceeding 10,000 is not preferable.
- a viscosity measured at a temperature of 25 ° C. in accordance with JIS K7117-2 (cone-flat plate viscometer used) is often used, and 1000 mPa ⁇ s. Above, what is 1000 Pa.s or less is preferable.
- the dibasic acid component constituting the polyester plasticizer is preferably an aliphatic dibasic acid having 4 to 12 carbon atoms.
- Examples of such an aliphatic dibasic acid component include succinic acid, maleic acid, fumaric acid, glutamic acid, adipic acid, azelaic acid, sebacic acid, and dodecanedicarboxylic acid.
- succinic acid maleic acid, fumaric acid, glutamic acid, adipic acid, azelaic acid, sebacic acid, and dodecanedicarboxylic acid.
- aliphatic dibasic acids having 6 to 10 carbon atoms are preferable in terms of obtaining a polyester plasticizer having good compatibility with vinylidene fluoride resins, and adipic acid is particularly preferable from the viewpoint of industrial availability. .
- These aliphatic dibasic acids may be used alone or in combination of two or more.
- the glycol component constituting the polyester plasticizer is preferably a glycol having 2 to 18 carbon atoms, such as ethylene glycol, 1,2-propylene glycol, 1,2-butanediol, 1,3-butanediol, 4-butanediol, 2-methyl-1,3-propanediol, neopentyl glycol, 1,5-pentanediol, 1,6-hexanediol, 2,2-diethyl-1,3-propanediol, 2,2,4 -Trimethyl-1,3-pentanediol, 2-ethyl-1,3-hexanediol, 1,9-nonanediol, 1,10-decanediol, 2-butyl-2-ethyl-1,5-propanediol, Aliphatic dihydric alcohols such as 1,12-octadecanediol and polyalkylene glycols such as di
- a monohydric alcohol or a monovalent carboxylic acid is used to seal the molecular chain terminal of the polyester plasticizer.
- monohydric alcohols include butyl alcohol, hexyl alcohol, isohexyl alcohol, heptyl alcohol, octyl alcohol, isooctyl alcohol, 2-ethylhexyl alcohol, nonyl alcohol, isononyl alcohol, 2-methyloctyl alcohol, decyl alcohol, isodecyl.
- Examples thereof include monohydric alcohols having 2 to 22 carbon atoms such as alcohol, undecyl alcohol, dodecyl alcohol, tridecyl alcohol, tetradecyl alcohol, hexadecyl alcohol, and octadecyl alcohol.
- monohydric alcohols having 2 to 22 carbon atoms such as alcohol, undecyl alcohol, dodecyl alcohol, tridecyl alcohol, tetradecyl alcohol, hexadecyl alcohol, and octadecyl alcohol.
- isononyl alcohol is particularly preferable from the viewpoint of the compatibility with the vinylidene fluoride resin and the balance of the Tc ′ suppression tendency.
- monohydric alcohols may be used alone or in combination of two or more.
- monovalent carboxylic acid include aliphatic monovalent carboxylic acids having 6 to 22 carbon atoms derived from animal and vegetable oils and fats, or acetic acid, butyric acid, isobutyric acid, heptanoic acid, isooctanoic acid, and 2-ethyl.
- Synthetic monovalent carboxylic acids having 2 to 18 carbon atoms such as xanthic acid, nonanoic acid and isostearic acid, as well as benzoic acid, toluic acid, dimethyl aromatic monocarboxylic acid, ethyl aromatic monocarboxylic acid, cumic acid, tetramethyl aromatic mono Aromatic carboxylic acids such as carboxylic acid, naphthoic acid, biphenyl carboxylic acid, and furoic acid can be used, and these may be used alone or in combination of two or more.
- compatibility inhibitors include dibasic acids such as aromatic dibasic acids such as phthalic acid and trimellitic acid, or aliphatic dibasic acids such as adipic acid, and monohydric alcohols having 2 to 22 carbon atoms.
- a monomeric plasticizer that is incompatible with the vinylidene fluoride resin is preferably used.
- a monomeric ester plasticizer comprising an aliphatic dibasic acid having 6 to 10 carbon atoms, particularly adipic acid, and a monohydric alcohol having 2 to 22 carbon atoms, particularly a monohydric alcohol having 6 to 18 carbon atoms.
- a monomeric ester plasticizer comprising an aliphatic dibasic acid having 6 to 10 carbon atoms, particularly adipic acid, and a monohydric alcohol having 2 to 22 carbon atoms, particularly a monohydric alcohol having 6 to 18 carbon atoms.
- the polyester plasticizer at least one of the dibasic acid constituting the polyester plasticizer, and the monohydric alcohol having a carbon chain portion in common with the glycol and the end-capped monohydric alcohol
- Monomeric ester plasticizers composed of a dibasic acid and a monohydric alcohol are preferred.
- diisononyl adipate DINA
- Such a monomeric ester plasticizer should determine the addition amount according to the Tc ′ lowering power of the polyester plasticizer to be used, and does not impair the compatibility with the vinylidene fluoride resin. If possible, it is preferable to obtain the addition amount experimentally so that the reduction force can be suppressed as much as possible.
- the Tc ′ lowering power of the polyester plasticizer is the chemical structure of the constituent components such as the dibasic acid component, glycol component and monohydric alcohol component constituting the polyester plasticizer, and the number average molecular weight (degree of polymerization) and molecular weight. This is because the influence of distribution and the like is complicated, and it is impossible to predict in general.
- the total amount of the monomeric ester plasticizer and the polyester plasticizer is As a standard, it is preferable to use a mixture of 2 to 30% by weight, more preferably 5 to 25% by weight, and most preferably 8 to 20% by weight.
- the monomeric ester plasticizer is based on the total amount of the polyester plasticizer, Preferably 5 to 50% by weight, more preferably 10 to 45% by weight, and most preferably 15 to 40% by weight are used in combination.
- the conversion temperature Tc ′ can be preferably 140 ° C. or higher, more preferably 143 ° C. or higher, and most preferably 145 ° C. or higher. In general, it is difficult to realize Tc ′ exceeding 170 ° C.
- a solvent or a monomeric ester plasticizer that is compatible with the vinylidene chloride resin can be added.
- An example of such a solvent is propylene carbonate, and an example of a monomeric ester plasticizer is dialkylene glycol dibenzoate composed of glycol and benzoic acid.
- the amount used is the total amount with the plasticizer. It is preferable to keep it at 10% by weight or less, particularly 5% by weight or less.
- a polyester plasticizer (or a mixture of a polyester plasticizer and a compatibility inhibitor) is melted and kneaded with a vinylidene fluoride resin in an extruder so that the polyester plasticizer is clear (that is, visible to the naked eye). It is necessary to have compatibility with the vinylidene fluoride resin to such an extent that a molten mixture is obtained which does not leave a dispersion that gives a turbidity of However, the formation of the melt-kneaded product in the extruder includes factors other than the properties derived from the raw materials, such as mechanical conditions, and in the sense of eliminating these factors, the compatibility determination method described later in the present invention. To determine compatibility.
- the raw material composition for forming the porous film comprises a plasticizer (a compatibility inhibitor (monomeric) in addition to a polyester plasticizer) with respect to 20 to 50% by weight, preferably 25 to 40% by weight of a vinylidene fluoride resin.
- a plasticizer a compatibility inhibitor (monomeric) in addition to a polyester plasticizer
- it is preferably contained in an amount of 50 to 80% by weight, preferably 60 to 85% by weight.
- a water-insoluble solvent or the like added as necessary is used in a form in which a part of the plasticizer is replaced in consideration of the melt viscosity and the like of the raw material composition under melt kneading.
- the amount of the plasticizer is too small, it is difficult to obtain an increase in the porosity of the target surface layer of the present invention, and if it is too large, the melt viscosity is excessively lowered, and in the case of a hollow fiber, it tends to be crushed. Moreover, there exists a possibility that the mechanical strength of the porous film obtained may fall.
- a biaxial kneading extruder is used, and the vinylidene fluoride resin (preferably comprising a mixture of a main resin and a crystal characteristic modifying resin) is
- the plasticizer and the like are supplied from the upstream side of the extruder, supplied downstream, and made into a homogeneous mixture before being discharged through the extruder.
- This twin-screw extruder can be controlled independently by dividing it into a plurality of blocks along its longitudinal axis direction, and appropriate temperature adjustment is made according to the contents of the passing material at each site.
- the die or nozzle temperature Td is preferably higher than the crystallization temperature Tc ′ of the composition by 30 ° C.
- the melt-extruded hollow fiber membrane is then inert to vinylidene fluoride resin at -40 to 90 ° C., preferably 0 to 90 ° C., more preferably 5 to 60 ° C. (ie, non-solvent and non-reactive). It is introduced into a cooling bath made of a liquid (preferably water) and cooled preferentially from its outer surface to form a solidified film. At that time, in forming the hollow fiber membrane, a hollow fiber membrane having an enlarged diameter is obtained by cooling while injecting an inert gas such as air or nitrogen into the hollow portion. This is advantageous for obtaining a hollow fiber porous membrane having a small decrease in the amount of water per area (WO 2005 / 03700A).
- cooling from one side by a chill roll is also used in addition to a cooling bath shower. If the cooling medium temperature is less than ⁇ 40 ° C., the solidified film becomes brittle, making it difficult to take it out. If the temperature is less than 0 ° C., condensation or frost tends to occur due to moisture in the atmosphere. There is a difficult point. On the other hand, when the temperature exceeds 90 ° C., it becomes difficult to form a porous film having a small pore size distribution with a small pore size on the surface of the water to be treated, which is the object of the present invention.
- the difference Tc′ ⁇ Tq between the crystallization temperature Tc ′ of the kneaded product of the vinylidene fluoride resin and the plasticizer and the temperature Tq of the cooling inert liquid is preferably 60 ° C. or higher, more preferably 75 ° C. or higher, most preferably Preferably it is 90 degreeC or more.
- this temperature difference in order for this temperature difference to exceed 150 ° C., it is generally necessary to set the cooling liquid temperature to less than 0 ° C., which makes it difficult to use an aqueous medium as a preferable cooling liquid.
- the elapsed time from the melt extrusion until entering the cooling bath Is generally in the range of 0.3 to 10.0 seconds, particularly 0.5 to 5.0 seconds.
- the cooled and solidified film-like material is then introduced into an extraction liquid bath and subjected to extraction and removal of a plasticizer and the like.
- the extraction liquid is not particularly limited as long as it does not dissolve the polyvinylidene fluoride resin and can dissolve the plasticizer and the like.
- polar solvents having a boiling point of about 30 to 100 ° C. such as methanol and isopropyl alcohol for alcohols and dichloromethane and 1,1,1-trichloroethane for chlorinated hydrocarbons are suitable.
- the extracted film-like material is then subjected to stretching to increase the porosity and pore diameter and improve the strength.
- stretching it is possible to selectively wet from the outer surface of the membrane after extraction (porous membrane) to a certain depth and stretch in this state (hereinafter referred to as “partial wet stretching”). It is preferable for obtaining a high surface layer porosity A1. More specifically, prior to stretching, 5 ⁇ m or more from the outer surface of the porous membrane, preferably 7 ⁇ m or more, more preferably 10 ⁇ m or more, and 1 ⁇ 2 or less, preferably 1 / or less, more preferably 1 / 1 / of the film thickness.
- a depth of 4 or less is selectively wetted. If the depth to be wet is less than 5 ⁇ m, the increase in the surface layer porosity A1 is not sufficient, and if it exceeds 1/2, when the dry heat is relaxed after stretching, the drying of the wetting liquid becomes uneven and the heat treatment or relaxation Processing may be uneven.
- a solvent for wetting vinylidene fluoride resin such as methanol or ethanol or its aqueous solution
- a wettability improving liquid having a surface tension of 25 to 45 mN / m (including the case of immersion). If the surface tension is less than 25 mN / m, it may be difficult to selectively apply the wettability improving liquid to the outer surface because the penetration rate into the PVDF porous membrane is too fast.
- a surfactant solution obtained by adding a surfactant to water that is, an aqueous solution or an aqueous homogeneous dispersion of a surfactant
- the type of the surfactant is not particularly limited.
- a carboxylate type such as an aliphatic monocarboxylate, a sulfonate type such as an alkylbenzene sulfonate, a sulfate ester type such as an alkyl sulfate, Phosphate ester type such as alkyl phosphate salt; amine salt type such as alkylamine salt for cationic surfactant, quaternary ammonium salt type such as alkyltrimethylammonium salt; glycerin fatty acid for nonionic surfactant Ester type such as ester, ether type such as polyoxyethylene alkylphenyl ether, ester ether type such as polyethylene glycol fatty acid ester; for amphoteric surfactant, carboxybetaine type such as N, N-dimethyl-N-alkylaminoacetic acid betaine 2-alkyl-1-hydroxyl Le - such as glycine type and the like, such as carboxymethyl imidazo
- the surfactant preferably has an HLB (hydrophilic / lipophilic balance) of 8 or more. When the HLB is less than 8, the surfactant is not finely dispersed in water, and as a result, uniform wettability improvement becomes difficult.
- Particularly preferably used surfactants include nonionic surfactants having an HLB of 8 to 20, and further 10 to 18, or ionic (anionic, cationic and amphoteric) surfactants. A surfactant is preferred.
- the wettability improving liquid to the outer surface of the porous membrane by batch or continuous immersion of the porous membrane.
- This dipping process is a double-sided coating process for flat membranes and a single-sided coating process for hollow fiber membranes.
- the flat membrane batch dipping treatment is carried out by dipping the hollow fiber membranes bundled by bobbin winding or casserole winding by dipping the layers cut into appropriate sizes.
- the continuous treatment is performed by continuously immersing a long porous membrane in the treatment liquid.
- a surfactant having a relatively high HLB within the above range more specifically 8-20, more preferably 10-18, may be used to form relatively small emulsion particles. preferable.
- the penetration speed can be lowered moderately by increasing the wettability improving liquid to a high viscosity, or penetrating with a low viscosity. It is possible to increase the speed.
- the permeation rate can be moderately slowed by lowering the wettability improving liquid or the permeation at a high temperature. It is possible to increase the speed.
- the viscosity and temperature of the wettability improving liquid act in opposite directions, and can be complementarily controlled for adjusting the penetration rate of the wettability improving liquid.
- the stretching of the hollow fiber membrane is generally preferably performed as uniaxial stretching in the longitudinal direction of the hollow fiber membrane by a pair of rollers having different peripheral speeds. This is because, in order to harmonize the porosity and the strength and elongation of the vinylidene fluoride resin hollow fiber porous membrane of the present invention, the stretched fibril (fiber) portion and the unstretched node (node) portion are arranged along the stretching direction. This is because it has been found that a microstructure that appears alternately is preferable.
- the draw ratio is about 1.1 to 4.0 times, particularly about 1.2 to 3.0 times, and most preferably about 1.4 to 2.5 times. When the draw ratio is excessive, the tendency of the hollow fiber membrane to break becomes large.
- the stretching temperature is preferably 25 to 90 ° C, particularly 45 to 80 ° C. If the stretching temperature is too low, the stretching becomes non-uniform and the hollow fiber membrane is easily broken. On the other hand, if the stretching temperature is too high, it is difficult to increase the porosity even if the stretching ratio is increased. In the case of a flat membrane, sequential or simultaneous biaxial stretching is also possible.
- the crystallinity is increased by heat treatment in advance at a temperature in the range of 80 to 160 ° C., preferably 100 to 140 ° C. for 1 second to 18000 seconds, preferably 3 seconds to 3600 seconds. It is also preferable.
- the hollow fiber porous membrane of vinylidene fluoride resin obtained as described above is subjected to at least one stage, more preferably at least two stages of relaxation or constant length heat treatment in a non-wetting atmosphere (or medium).
- the non-wetting atmosphere is a non-wetting liquid having a surface tension (JIS K6768) larger than the wetting tension of vinylidene fluoride resin near room temperature, typically water or air. Gas is used.
- the relaxation treatment of the uniaxially stretched porous membrane such as the hollow fiber is carried out by first performing the above-described non-wetting, preferably heated atmosphere, disposed between the upstream roller and the downstream roller, where the peripheral speed gradually decreases. It is obtained by passing the obtained stretched porous membrane.
- the relaxation rate determined by (1 ⁇ (downstream roller peripheral speed / upstream roller peripheral speed)) ⁇ 100 (%) is preferably in the range of 0% (constant length heat treatment) to 50%, particularly 1 to 20 % Relaxation heat treatment is preferable.
- a relaxation rate exceeding 20% depends on the stretching ratio in the previous step, but is not preferable because it is difficult to achieve or even if realized, the effect of improving the water permeability is saturated or decreases.
- the first-stage constant length or relaxation heat treatment temperature is preferably 0 to 100 ° C., particularly 50 to 100 ° C.
- the treatment time may be short or long as long as the desired heat setting effect and relaxation rate are obtained. Generally, it is about 5 seconds to 1 minute, but it is not necessary to be within this range.
- the post-stage constant length or relaxation heat treatment temperature is preferably 80 to 170 ° C., more preferably 120 to 160 ° C., so that a relaxation rate of 1 to 20% can be obtained.
- the effect of the relaxation treatment described above is a remarkable effect that the substantial membrane fractionation performance is maintained in a sharp state and the water permeability of the obtained porous membrane is increased. Moreover, performing the above-mentioned one-stage and two-stage treatment under a constant length is a heat setting operation after stretching.
- the vinylidene fluoride resin porous membrane of the present invention obtained through the above-described series of steps is (a) focused ion beam scanning for a portion (surface layer) having a thickness of 10 ⁇ m continuous from one surface (surface to be treated). Measured by a scanning electron microscope (FIB-SEM) (a1) The average diameter of the reticulated resin fibers is 100 nm or less, (a2) the porosity A1 is 60% or more, and (b) the surface pore diameter P1 The main feature is a surface layer structure of 0.3 ⁇ m or less.
- the porosity A1 is preferably 65% or more, more preferably 70% or more, and the upper limit is restricted by the structural strength of the surface layer, and it is difficult to exceed 85%.
- the one-surface-side surface pore diameter P1 is usually an average diameter by surface observation by SEM, preferably 0.20 ⁇ m or less, more preferably 0.15 ⁇ m or less, and although there is no particular lower limit, it is generally less than 0.01 ⁇ m. It is difficult to do.
- FIB-SEM method The FIB used to measure (a1) the average diameter (nm) of the network-like resin fiber and (a2) the porosity A1 (%), which are the characteristics of the vinylidene fluoride resin porous membrane of the present invention described above. -An outline of the SEM method is given below.
- the hollow fiber porous membrane was dyed with ruthenium oxide, it was embedded with an epoxy resin, and a cross-sectional sample in which an annular cross section perpendicular to the longitudinal direction of the hollow fiber membrane was exposed by mechanical polishing was produced.
- This cross-sectional sample was set in a focused ion beam-scanning electron microscope (dual beam FIB / SEM combined device, “Nova200 NanoLab” manufactured by FEI), and 10 ⁇ m square from the outer surface of the hollow fiber porous membrane to a depth of 10 ⁇ m.
- the region was irradiated with a Ga (gallium) ion beam and scraped off to a thickness of 20 nanometers to form a smooth observation surface, followed by non-deposition observation at an acceleration voltage of 3 keV and an observation magnification of 10,000, and an SEM photograph was taken.
- this observation surface is again irradiated with a Ga (gallium) ion beam and scraped off to a thickness of 20 nanometers to prepare a new observation surface (10 ⁇ m square), followed by non-deposition observation at an acceleration voltage of 3 keV and an observation magnification of 10,000 times. , Took a photo. This operation was repeated 100 times, and 100 SEM photographs were taken from the first observation surface to a thickness (depth) of 2 ⁇ m every 20 nanometers.
- Number of hole branch points (pieces): Find the center line of holes from a three-dimensional observation image, branch points, that is, points where three or more are in contact, or points where the diameter of the holes is different, and end points, ie, those that are in contact with others The sum of the number of adjacent branch points and branch points, the number of adjacent branch points and end points, and the number of adjacent end points and end points was determined as the number of branch points.
- FIGS. 1-10 Examples of binarized images of SEM photographs of observation surfaces obtained by digging down to a depth of 1 ⁇ m from the start of observation are shown in FIGS.
- the hole branch point function per unit volume is as small as 25 (pieces / ⁇ m 3 ) or less. This indicates that there are few branches and independent vacancies in the existing pores, and the permeability of the water to be treated is good.
- the ratio A1 / A2 between the porosity A1 (%) of the surface layer and the porosity A2 (%) of the entire porous membrane is 0.90 or more.
- the upper limit is not particularly limited, but is generally 1.1 or less.
- the total layer porosity A2 (%) is preferably 70 to 85%, more preferably 75 to 82%.
- the average pore diameter Pm is generally 0.25 ⁇ m or less, preferably 0.20 to 0.01 ⁇ m, more preferably 0.15 to 0.05 ⁇ m, and the maximum pore diameter Pmax is generally 0.70 to 0.03 ⁇ m, preferably 0 .40 to 0.06 ⁇ m; Properties with a tensile breaking strength of 7 MPa or more and a tensile breaking elongation of 30% or more, preferably 60% or more are obtained.
- the thickness is usually in the range of about 50 to 800 ⁇ m, preferably 50 to 600 ⁇ m, particularly preferably 150 to 500 ⁇ m.
- the outer diameter of the hollow fiber is about 0.3 to 3 mm, particularly about 1 to 3 mm.
- the pure water permeation amount at a test length of 200 mm, a water temperature of 25 ° C., and a differential pressure of 100 kPa is 5 m / day or more, preferably 10 m / day or more, more preferably 15 m / day or more, and most preferably 20 m / day or more.
- the present invention when filtering the treated water using the vinylidene fluoride resin porous membrane obtained as described above, filtration and aeration of the surface of the porous membrane to be treated side by side or alternately The manufacturing method of the filtered water to perform is also included.
- the filtration of turbid water by the porous membrane of the present invention is considered to be surface filtration because the surface pore size P1 of the porous membrane to be treated is sufficiently smaller than the particle size of the suspended matter. Therefore, even if the amount of filtered water per unit membrane area (filtration flux) is increased, the local flux generated in the pores of the surface layer is ( It is believed to be low and uniform (compared to a film with a small A1). This reduces the pressing force of the suspended solid particles on the membrane surface, but further aeration of the surface of the water to be treated increases the fluidity of the suspended particles on the membrane surface, thereby increasing the suspension of the membrane surface.
- the increase in turbidity concentration is suppressed, the increase in filtration pressure over time is suppressed, and stable filtration can be continued over a long period of time.
- the filtration using the porous membrane of the present invention is preferably performed using, for example, a membrane module incorporating the porous membrane.
- membrane modules suitable for aeration of the surface of the porous membrane to be treated include those disclosed in WO2007 / 080910A1 or WO2007 / 040035A1.
- the timing of aeration when the membrane module is immersed in a tank open to the atmosphere and filtered, it is preferable to perform aeration simultaneously with the filtration. It is also preferable to intermittently stop only filtration while performing aeration continuously. In this case, the filtration is performed continuously for 3 minutes to 30 minutes, preferably 5 minutes to 15 minutes, and then the filtration is stopped for 30 seconds to 5 minutes, preferably 1 minute to 2 minutes. It is preferable to periodically repeat filtration and filtration pause with such time distribution.
- the method in which aeration acts on the membrane surface during filtration in this way is the case where the concentration of suspended solid particles is high as in the MBR method, and the MLSS (active sludge suspended solids amount) is about 3000 to 20000 mg / L. Is preferred.
- the amount of aeration is 5 to 200 m 3 / h, preferably 10 to 100 m 3 / h, more preferably 20 to 70 m 3 / h per 1 m 2 of the bottom area of the membrane module. If it is less than 5 m 3 / h, the suppression of the filtration pressure increase is not sufficient, and if it exceeds 200 m 3 / h, the effect of suppressing the increase in the filtration differential pressure is saturated.
- the amount of aeration is 20 to 400 m 3 / h, preferably 50 to 300 m 3 / h per 1 m 2 of the bottom area of the membrane module. If it is less than 20 m 3 / h, the suppression of the filtration pressure increase is not sufficient, and if it exceeds 400 m 3 / h, the effect of suppressing the increase in the filtration differential pressure is saturated.
- the present invention also includes a step of filtering treated water using the vinylidene fluoride resin porous membrane obtained as described above to obtain filtered water, and a chemical solution from the filtered water side of the vinylidene fluoride resin porous membrane. And a method for producing filtered water, comprising the step of washing the membrane by injecting water.
- the chemical solution is injected from the filtered water side surface, and in the case of a hollow fiber membrane, the reverse pressure injection from the hollow portion is performed with the membrane attached to the filtration device (CIP; CleanCIn Place). Law).
- the chemical solution is preferably injected while the membrane is immersed in the water to be treated in the apparatus and by performing aeration simultaneously or alternately with filtration, so that CIP can be performed efficiently.
- the injection of the chemical solution in the CIP method is mainly intended to remove dirt adhered to the inside of the film including the surface layer of the film, and the film cleaning effect is comprehensively combined with the removal of the film surface by aeration. This is because the operation period can be improved and the operation period can be maintained for a long time.
- an aqueous solution of an oxidizing agent such as sodium hypochlorite and hydrogen peroxide, an acid such as hydrochloric acid and citric acid, and an alkali such as sodium hydroxide is preferably used.
- the concentration of the chemical solution is 0.02 to 1% by weight as an effective chlorine concentration in the case of sodium hypochlorite, 1 to 5% by weight in the case of citric acid, and 0.5 to 2% in the case of sodium hydroxide. % Is preferred.
- Membrane cleaning by injection of a chemical solution is preferably performed when the filtration pressure rises to 60 kPa or more in immersion filtration and 150 kPa or more in pressure filtration, specifically, once every 2 weeks to 6 months. Is performed about once every 1 to 3 months.
- the chemical injection is carried out preventively before the filtration differential pressure rises significantly. Specifically, it is performed once a day to once a month, preferably once every 3 days to 2 weeks.
- the injection flux of the chemical solution may be about the same as the filtration flux or several times, and specifically about 0.3 to 10 m / day based on the surface area of the water to be treated. Since the CIP method removes the dirt of the film by chemical decomposition or dissolution action by the chemical solution, it is sufficient that the chemical solution efficiently contacts the membrane. For this reason, it is preferable to inject at a low flux as much as possible after the chemical solution comes into contact with the membrane, specifically, injection at 0.1 to 2 m / day, or the injection is stopped when the chemical solution comes into contact with the membrane. A method of holding for a certain time is also preferable.
- the contact time between the membrane and the chemical solution is 2 to 240 minutes, preferably 3 to 100 minutes, more preferably 5 to 30 minutes as a total of the injection time and the holding time per chemical solution injection.
- Crystal melting point Tm1, Tm2 and crystallization temperature Tc, Tc ′ Using a differential scanning calorimeter “DSC7” manufactured by PerkinElmer Co., Ltd., 10 mg of sample resin was set in a measurement cell, and the temperature was increased from 30 ° C. to 250 ° C. at a rate of 10 ° C./min in a nitrogen gas atmosphere. The temperature was then maintained at 250 ° C. for 1 minute, and then the temperature was decreased from 250 ° C. to 30 ° C. at a rate of 10 ° C./min to obtain a DSC curve.
- DSC7 differential scanning calorimeter
- the endothermic peak speed in the temperature rising process was the melting point Tm1 (° C.), and the exothermic peak temperature in the temperature lowering process was the crystallization temperature Tc (° C.).
- the temperature was raised again from 30 ° C. to 250 ° C. at a rate of 10 ° C./min, and the DSC curve was measured.
- the endothermic peak temperature in this reheated DSC curve was the original resin melting point Tm2 (° C.) that defines the crystal characteristics of the vinylidene fluoride resin of the present invention.
- the crystallization temperature Tc ′ (° C.) of the mixture of vinylidene fluoride resin as a film raw material and a plasticizer is the first intermediate molded body that is melt-kneaded by an extruder and then extruded from a nozzle and cooled and solidified.
- the exothermic peak temperature detected in the temperature lowering process is obtained by obtaining a DSC curve through the same heating and cooling cycle as described above using 10 mg of the sample.
- compatibility of each of the compatibility inhibitors comprising a polyester plasticizer and a monomeric ester plasticizer, or a mixture thereof (hereinafter simply referred to as “plasticizer” in this section) with respect to vinylidene fluoride resin is as follows. Determined by the method: A slurry-like mixture is obtained by mixing 23.73 g of vinylidene fluoride resin and 46.27 g of a plasticizer at room temperature. Next, the barrel of “Lab Plast Mill” (mixer type: “R-60”) manufactured by Toyo Seiki Co., Ltd. is 10 ° C. higher than the melting point of the vinylidene fluoride resin (for example, about 17 to 37 ° C. higher).
- the temperature is adjusted, and the slurry mixture is charged and preheated for 3 minutes, and then melt-kneaded at a mixer rotation speed of 50 rpm.
- the plasticizer is based on vinylidene fluoride resin. Determined to be compatible.
- the viscosity of the melt-kneaded material is high, it may appear cloudy due to entrapment of bubbles, and in that case, it is determined by deaeration appropriately by a method such as hot pressing. Once it has cooled and solidified, it is heated again to be in a molten state, and then it is determined whether or not it is clarified.
- the average pore diameter P1 of the surface to be treated (outer surface in hollow fiber) and the average pore diameter P2 in the filtrate side surface (inner surface in hollow fiber) were determined by SEM. Measured (SEM average pore diameter).
- SEM average pore diameter the measurement method will be described by taking a hollow fiber porous membrane sample as an example. SEM photography is performed on the outer surface and inner surface of the hollow fiber membrane sample at an observation magnification of 15,000 times, respectively. Next, for each SEM photograph, the hole diameter is measured for everything that can be recognized as a hole.
- the arithmetic average of the measured pore diameters is obtained and set as the outer surface average pore diameter P1 and the inner surface average pore diameter P2.
- the photograph image may be divided into four equal parts, and the above-mentioned hole diameter measurement may be performed for one area (1 ⁇ 4 screen). .
- the number of measurement holes is approximately 200 to 300.
- Sample length L 200 mm of sample hollow fiber porous membrane was immersed in ethanol for 15 minutes, then immersed in pure water for 15 minutes, wetted, and then measured at a water temperature of 25 ° C. and a differential pressure of 100 kPa per day.
- CIP recovery time MRR method-CIP processing
- the immersion type minimodule formed from the hollow fiber porous membrane sample was subjected to continuous filtration of activated sludge water at a filtration flux of 1.7 m / day, followed by chemical injection backwash (CIP )
- CIP recovery time The time required for the treatment to recover the differential pressure inside and outside the hollow fiber porous membrane to the value immediately after the start of filtration (initial value) is defined as the CIP recovery time.
- the mini module is formed by vertically fixing three hollow fiber porous membrane samples between the upper header and the lower header so that the effective filtration length per one becomes 500 mm.
- the upper header is an upper insertion port to be fixed with the upper end of the hollow fiber membrane being opened on the lower side, an internal space (flow path) for filtrate water communicating with the upper insertion port, and suction on the upper side. It has a filtrate outlet for discharging filtrate to the pump.
- the lower header has a lower insertion port for fixing the hollow fiber membrane on its upper side with its lower end closed, and an aeration nozzle that does not communicate with the lower insertion port (diameter 1 mm ⁇ 10) And an internal space (supply path) for supplying air to the aeration nozzle and an air supply port for supplying air from the air pump to the internal space.
- the upper and lower ends of the three hollow fiber membrane samples are each inserted and fixed to the upper insertion port by epoxy resin so as to be liquid-tightly connected to the upper header, and the lower header is inserted so as to be closed with the lower header. It is inserted into the mouth and fixed.
- This modularized hollow fiber membrane sample was dipped in ethanol for 15 minutes and then wetted by replacement with pure water. Then, the bottom area was approximately 30 cm 2 and the height of the water surface was approximately 600 mm. Soak the hollow fiber vertically.
- MLSS floating substance concentration
- DOC total organic concentration after filtration through a 1 ⁇ m glass filter
- 7 to 9 mg / L of activated sludge water is supplied at a rate of 0.2 L / min by a pump, and the overflow is circulated to the raw water tank. Further, air is supplied from the lower header at a rate of 5 L / min, and is constantly bubbled into the activated sludge water in the test water tank.
- a chemical container filled with sodium hypochlorite aqueous solution (effective chlorine concentration 3000 ppm) is attached and operated by switching the direction of the suction pump in the reverse direction and from the filtered water outlet of the upper header.
- sodium hypochlorite aqueous solution effective chlorine concentration 3000 ppm
- the inside of the hollow fiber porous membrane was injected from the inside to the outside with a constant filtered water amount of 1.7 m / day, and the pressure difference between the inside and outside of the hollow fiber porous membrane (back washing) Record the change over time in the differential pressure. The time t until the backwash differential pressure gradually decreases and reaches the equilibrium value as the membrane cleaning progresses is measured.
- a water receiving container is attached in place of the chemical liquid container, and the suction pump is returned to its original direction to operate, and the constant filtration flux of 1.7 m / day is again applied from the outside to the inside of the hollow fiber porous membrane.
- filtration differential pressure the change with time in the differential pressure inside the hollow fiber membrane (filtration differential pressure) is measured.
- the suction is resumed and the average differential pressure value for the first 5 minutes is recorded as the post-recovery differential pressure TMP3.
- adipic acid-based polyester plasticizer polymers of adipic acid and 1,2-butanediol whose ends are sealed with isononyl alcohol; “D623N” manufactured by J. Plus, number average molecular weight of about 1800, JIS K71117-2 (cone-plate-type rotational viscometer) measured viscosity at 25 ° C. of 3000 mPa ⁇ s) and monomeric ester plasticizer diisononyl adipate (“DINA” manufactured by Jay Plus Co., Ltd.) The mixture was stirred and mixed at room temperature at a rate of 88% by weight / 12% by weight to obtain a plasticizer mixture (mixture B).
- the mixture A is supplied from the powder supply unit, and the barrel temperature is 220 ° C.
- the mixture was fed and kneaded at a barrel temperature of 220 ° C., and the mixture was extruded into a hollow fiber shape from a nozzle (190 ° C.) having a circular slit having an outer diameter of 6 mm and an inner diameter of 4 mm. At this time, the inner diameter was adjusted by injecting air into the hollow portion of the hollow fiber from the vent provided in the center of the nozzle.
- the extruded mixture is kept in a molten state, is maintained at a temperature of 50 ° C., and has a water surface at a position 280 mm away from the nozzle (that is, an air gap of 280 mm). (Retention time in cooling bath: about 6 seconds) After taking up at a take-up speed of 5.0 m / min, this was wound around a bobbin to obtain a first intermediate molded body.
- the plasticizer was extracted by immersing this first intermediate molded body in dichloromethane at room temperature for 30 minutes. At this time, the extraction was performed while rotating the bobbin so that the dichloromethane was evenly distributed over the yarn. Next, the operation of replacing the dichloromethane with a new one and extracting again under the same conditions was repeated, and extraction was performed four times in total.
- the second intermediate formed body is pulled out while rotating the bobbin, the first roll speed is set to 20.0 m / min, and the second roll is passed through the 60 ° C. water bath.
- the film was stretched 1.75 times in the longitudinal direction by setting the speed to 35.0 m / min.
- it was passed through a hot water bath controlled at a temperature of 90 ° C., and further passed through a dry heat bath controlled at a space temperature of 80 ° C. for heat treatment. This was wound up to obtain a polyvinylidene fluoride hollow fiber porous membrane (third molded body) of the present invention.
- the time required to stretch all the second intermediate molded body wound around the bobbin was about 200 minutes.
- PN150 number average molecular weight of about 1000, viscosity 500 mPa ⁇ s) and N-methylpyrrolidone (NMP)
- NMP N-methylpyrrolidone
- the mixture was stirred and mixed at room temperature at a ratio of 17.5% by weight to use a plasticizer / solvent mixture B; the mixture A and the mixture B were mixed at a ratio of 38.4% by weight / 61.6% by weight.
- Supplyed water cooling bath temperature set to 40 ° C .; stretch ratio set to 1.85 times; as heat treatment after stretching, 8% in 90 ° C. water bath Relaxation, and then it was 3% relaxation treatment in a 140 ° C. in air; give the polyvinylidene fluoride porous membrane except in the same manner as in Example 1.
- the outline of the production conditions of the above Examples and Comparative Examples and the physical properties of the obtained polyvinylidene fluoride hollow fiber porous membrane are shown together in Table 1 below.
- the hollow fiber porous membrane of Comparative Example 2 has a composite structure in which a vinylidene fluoride resin coating layer is formed on the outside with a polyester multifilament monowoven braid as a core layer, as shown in the example of Patent Document 2. Therefore, the total layer porosity A2 indicates a measured value for only the outer layer.
- FIGS. 3 to 5 binarization of the 10 ⁇ m ⁇ 10 ⁇ m visual field in the middle part (observation surface obtained by updating the surface to a depth of 1 ⁇ m for a 2 ⁇ m thick sample) when FIB-SEM measurement was performed on the hollow fiber porous membrane of each example
- the obtained SEM images (10,000 times) are shown in FIGS. 3 to 5, in each of the drawings, the left side is the outer surface side, the white part indicates the resin fiber (phase), and the black part indicates the pore (phase).
- FIG. 4 Comparative Example 1
- FIG. 5 Comparative Example 2
- the hollow fiber porous membrane of each example it is as follows when the result of having performed the filtration and CIP recovery process by MBR method is supplemented.
- Example 1 When the outer surface of the membrane was observed with SEM (5000 times) after filtration for 24 hours by MBR method, pores were confirmed on the entire surface, and no cake was observed.
- a porous membrane, a method for producing the same, and a method for producing filtered water using the MBR method and / or the CIP method using the same are provided.
- the vinylidene fluoride resin porous membrane of the present invention is suitable for (filtered) water treatment as described above, but the porosity of the dense layer that contributes particularly to separation characteristics or selective permeation characteristics has been improved.
- the porous membrane of the present invention is not limited to (filtered) water treatment, but can be used for concentration of bacteria, proteins, etc., recovery of chemically aggregated particles of heavy metals, separation membrane for oil-water separation and gas-liquid separation Also, it can be suitably used as a battery diaphragm such as a lithium ion secondary battery and a solid electrolyte support.
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Abstract
Description
本発明において、主たる膜原料であるフッ化ビニリデン系樹脂としては、フッ化ビニリデンの単独重合体、すなわちポリフッ化ビニリデン、フッ化ビニリデンと共重合可能な他のモノマーとの共重合体あるいはこれらの混合物で重量平均分子量が30万以上、特に50万~80万のものが好ましく用いられる。フッ化ビニリデンと共重合可能なモノマーとしては、四フッ化エチレン、六フッ化プロピレン、三フッ化エチレン、三フッ化塩化エチレン、フッ化ビニル等の一種又は二種以上を用いることができる。フッ化ビニリデン系樹脂は、構成単位としてフッ化ビニリデンを70モル%以上含有することが好ましい。なかでも結晶化温度Tcと機械的強度の高さからフッ化ビニリデン100モル%からなる単独重合体を用いることが好ましい。
本発明の中空糸多孔膜は、主として上記したフッ化ビニリデン系樹脂により形成されるが、その製造のためには上述したフッ化ビニリデン系樹脂に加えて、少なくともその可塑剤を孔形成剤として用いることが好ましい。本発明において可塑剤としては、溶融混練温度において、フッ化ビニリデン系樹脂と相溶性を有するが、フッ化ビニリデン系樹脂との溶融混練物に、フッ化ビニリデン系樹脂単独の結晶化温度Tc(℃)とほぼ同じ(すなわち±5℃以内、好ましくは±4℃以内、更に好ましくは±2℃以内の)結晶化温度Tc′(℃)を与えるものが用いられる。このような可塑剤としては、一般に、二塩基酸とグリコールからなるポリエステル系可塑剤から選択されたものが用いられるが、特に数平均分子量(JIS K0070に準拠して測定したケン化価および水酸基価に基づいて算定)が好ましくは1200以上、より好ましくは1500以上、更に好ましくは1700以上のものが用いられる。ポリエステル系可塑剤の分子量が増大するにつれて、フッ化ビニリデン系樹脂との相溶性は増大する傾向にあるが、過度に分子量が大であると、後述する抽出工程で可塑剤を抽出除去するのに時間を要するおそれがあるので、1万を超える数平均分子量の可塑剤は好ましくない。一般に、ポリエステル系可塑剤の重合度の指標としては、JIS K7117-2(円すい-平板型回転粘度計使用)に準拠して温度25℃で測定した粘度が使用されることも多く、1000mPa・s以上、1000Pa・s以下であるものが好ましい。
多孔膜形成用の原料組成物は、フッ化ビニリデン系樹脂20~50重量%、好ましくは、25~40重量%に対して、可塑剤(ポリエステル系可塑剤に加えて相溶性抑制剤(モノメリックエステル系可塑剤)を使用する場合はこれを含む)が、50~80重量%、好ましくは、60~85重量%を混合するのが良い。必要に応じて添加する非水溶性の溶媒等は、原料組成物の溶融混練下での溶融粘度等を考慮して、可塑剤の一部を置きかえる態様で用いられる。
バレル温度180~250℃、好ましくは200~240℃で溶融混練された溶融押出組成物は、一般に150~270℃、好ましくは170~240℃、の温度Tdで、Tダイあるいは中空ノズルから押出されて膜状化される。従って、最終的に、上記温度範囲の均質組成物が得られる限りにおいて、フッ化ビニリデン系樹脂と、可塑剤および必要に応じて加えられる非水溶性溶媒(以下、これらをまとめて「可塑剤等」と称することがある)の混合並びに溶融形態は任意である。このような組成物を得るための好ましい態様の一つによれば、二軸混練押出機が用いられ、(好ましくは主体樹脂と結晶特性改質用樹脂の混合物からなる)フッ化ビニリデン系樹脂は、該押出機の上流側から供給され、可塑剤等が、下流で供給され、押出機を通過して吐出されるまでに均質混合物とされる。この二軸押出機は、その長手軸方向に沿って、複数のブロックに分けて独立の温度制御が可能であり、それぞれの部位の通過物の内容により適切な温度調節がなされる。ダイまたはノズル温度Tdは、組成物の結晶化温度Tc’に対して、30℃以上、特に50℃以上、高いことが、好ましい。これにより、組成物がエアギャップ通過中に結晶化することなく、冷却浴中で急冷されることで微細な結晶化を生じ、網目状樹脂繊維の平均径が小さい構造が得られるからである。また、高分子量のフッ化ビニリデン系樹脂あるいは可塑剤を含む組成物のメルトフラクチャーを抑制する効果も得られる。
次いで溶融押出された中空糸膜状物を-40~90℃、好ましくは0~90℃、より好ましくは5~60℃の、フッ化ビニリデン系樹脂に対して不活性(すなわち非溶媒且つ非反応性)な液体(好ましくは水)からなる冷却浴中に導入して、その外側面から優先的に冷却して固化成膜させる。その際、中空糸膜状物形成に際しては、その中空部に空気あるいは窒素等の不活性ガスを注入しつつ冷却することにより拡径された中空糸膜が得られ、長尺化しても単位膜面積当りの透水量の低下が少い中空糸多孔膜を得るのに有利である(WO2005/03700A公報)。平膜形成のためには、冷却浴のシャワーの外、チルロールによる片側面からの冷却も用いられる。冷却媒体温度が-40℃未満では、固化した膜状物が脆化するために引取りが困難となり、また0℃未満では、大気中の水分で結露あるいは霜が発生しやすくなるため、設備が複雑になる難点がある。他方、90℃を超えると本発明の目的とする被処理水側表面側孔径が小さく傾斜孔径分布を有する多孔膜の形成が困難となる。
冷却・固化された膜状物は、次いで抽出液浴中に導入され、可塑剤等の抽出除去を受ける。抽出液としては、ポリフッ化ビニリデン系樹脂を溶解せず、可塑剤等を溶解できるものであれば特に限定されない。例えばアルコール類ではメタノール、イソプロピルアルコールなど、塩素化炭化水素類ではジクロロメタン、1,1,1-トリクロロエタンなど、の沸点が30~100℃程度の極性溶媒が適当である。
抽出後の膜状物は、次いでこれを延伸に付し、空孔率および孔径の増大並びに強伸度の改善をすることが好ましい。特に、延伸に先立って、抽出後の膜状物(多孔膜)の外表面から一定の深さまで選択的に湿潤させ、この状態で延伸すること(以下、「部分湿潤延伸」と称する)が、高い表面層空孔率A1を得る上で好ましい。より詳しくは、延伸に先立って多孔膜の外表面から5μm以上、好ましくは7μm以上、更に好ましくは10μm以上、かつ膜厚さの1/2以下、好ましくは1/3以下、更に好ましくは1/4以下の深さを選択的に湿潤するように行う。湿潤される深さが5μm未満では表面層空孔率A1の増大が十分でなく、1/2を超えると延伸後に乾熱緩和する場合に、湿潤液の乾燥が不均一になり、熱処理あるいは緩和処理が不均一になる恐れがある。
上記のようにして得られたフッ化ビニリデン系樹脂の中空糸多孔膜を、非湿潤性の雰囲気(あるいは媒体)中で少なくとも一段階、より好ましくは少なくとも二段階の緩和または定長熱処理に付すことが好ましい。非湿潤性の雰囲気は、室温付近でフッ化ビニリデン系樹脂の濡れ張力よりも大きな表面張力(JIS K6768)を有する非湿潤性の液体、代表的には水、あるいは空気をはじめとするほぼ全ての気体が用いられる。中空糸のように一軸延伸された多孔膜の緩和処理は、周速が次第に低減する上流ローラと下流ローラの間に配置された上記した非湿潤性の好ましくは加熱された雰囲気中を、先に得られた延伸された多孔膜を送通することにより得られる。(1-(下流ローラ周速/上流ローラ周速))×100(%)で定まる緩和率は、合計で0%(定長熱処理)~50%の範囲とすることが好ましく、特に1~20%の範囲の緩和熱処理とすることが好ましい。20%を超える緩和率は、前工程での延伸倍率にもよるが、実現し難いか、あるいは実現しても透水量向上効果が飽和するか、あるいは却って低下するため好ましくない。
上記一連の工程を通じて得られる本発明のフッ化ビニリデン系樹脂多孔膜は、(a)一表面(被処理水側表面)から連続する厚さ10μmの部分(表面層)について、集束イオンビーム・走査型電子顕微鏡(FIB-SEM)により測定される(a1)網目状樹脂繊維の平均径が100nm以下、且つ(a2)空孔率A1が60%以上であり、(b)一表面側表面孔径P1が0.3μm以下、という表面層構造を主要な特徴とする。
ここで上記した本発明のフッ化ビニリデン系樹脂多孔膜の特性である(a1)網目状樹脂繊維の平均径(nm)および(a2)空孔率A1(%)を測定するために用いたFIB-SEM法の概要を以下に記す。
・繊維平均径(nm):三次元観察像を用いて、繊維中の分岐点間毎に繊維を長手に垂直に切る断面積を測定し、その円相当直径を算出し、平均値として求めた;
・空孔分岐点間数(個):三次元観察像から空孔の中心線を求め、分岐点すなわち3本以上が接している点または空孔の径が異なる点、および終点すなわち他と接しない端点を求め、分岐点と分岐点が隣接する数、分岐点と終点が隣接する数、終点と終点が隣接する数の総和を分岐点間数として求めた。
パーキンエルマー社製の示差走査熱量計「DSC7」を用いて、試料樹脂10mgを測定セルにセットし、窒素ガス雰囲気中で、温度30℃から10℃/分の昇温速度で250℃まで一旦昇温し、ついで250℃で1分間保持した後、250℃から10℃/分の降温速度で30℃まで降温してDSC曲線を求めた。このDSC曲線における昇温過程における吸熱ピーク速度を融点Tm1(℃)とし、降温過程における発熱ピーク温度を結晶化温度Tc(℃)とした。引き続いて、温度30℃で1分間保持した後、再び30℃から10℃/分の昇温速度で250℃まで昇温してDSC曲線を測定した。この再昇温DSC曲線における吸熱ピーク温度を本発明のフッ化ビニリデン系樹脂の結晶特性を規定する本来の樹脂融点Tm2(℃)とした。
ポリエステル系可塑剤およびモノメリックエステル系可塑剤からなる相溶性抑制剤のそれぞれ、またはこれらの混合物(以下、本項で単に「可塑剤」と称する)のフッ化ビニリデン系樹脂に対する相溶性は、次の方法により判定した:
フッ化ビニリデン系樹脂23.73gと、可塑剤46.27gとを、室温で混ぜ合わせてスラリー状混合物を得る。次に、東洋精機(株)製「ラボプラストミル」(ミキサータイプ:「R-60」)のバレルをフッ化ビニリデン系樹脂の融点より10℃以上高い(例えば約17~37℃高い)所定の温度に調整しておいて,上記スラリー状混合物を投入して3分間予熱し、続いてミキサー回転数50rpmで溶融混練する。混練開始後、10分以内に清澄な(すなわち目視で濁りの原因となる分散物のない程度に透明な)溶融混練物が得られる場合には、その可塑剤はフッ化ビニリデン系樹脂に対して相溶性であると判定する。なお、溶融混練物の粘度が高い場合などには気泡の抱きこみにより白濁して見えることがあるので、そのときは、適宜、熱プレスするなどの方法により脱気して判定する。一旦、冷却固化した場合には、再度加熱して溶融状態にしてから清澄か否かを判定する。
日本分光社製のGPC装置「GPC-900」を用い、カラムに昭和電工社製の「Shodex KD-806M」、プレカラムに「Shodex KD-G」、溶媒にNMPを使用し、温度40℃、流量10mL/分にて、ゲルパーミエーションクロマトグラフィー(GPC)法によりポリスチレン換算分子量として測定した。
平膜および中空糸膜を含む多孔膜の見掛け体積V(cm3)を算出し、更に多孔膜の重量W(g)を測定して次式より全層空孔率A2を求めた:
[数1]
全層空孔率A2(%)=(1-W/(V×ρ))×100
ρ:PVDFの比重(=1.78g/cm3)
なお、抽出後且つ延伸前の膜について同様の方法により測定される未延伸膜全層空孔率A0(%)と溶融押出混合物中の可塑剤(および溶媒)混合物Bの割合RB(重量%)の比A0/RBの概数は、混合物Bの孔形成効率を示すものと考えられる。
ASTM F316-86およびASTM E1294-89に準拠し、Porous Materials, Inc.社製「パームポロメータCFP-200AEX」を用いてハーフドライ法により平均孔径Pm(μm)を測定した。試液はパーフルオロポリエステル(商品名「Galwick」)を用いた。
ASTM F316-86およびASTM E1294-89に準拠し、Porous Materials, Inc.社製「パームポロメータCFP-200AEX」を用いてバブルポイント法により最大孔径Pmax(μm)を測定した。試液はパーフルオロポリエステル(商品名「Galwick」)を用いた。
平膜または中空糸状の多孔膜試料について、被処理水側表面(中空糸においては外表面)の平均孔径P1およびろ過水側表面(中空糸においては内表面)の平均孔径P2を、SEM法により測定した(SEM平均孔径)。以下、中空糸多孔膜試料を例にとって、測定法を説明する。中空糸膜試料の外表面および内表面について、それぞれ観察倍率1万5千倍でSEM写真撮影を行う。次に、それぞれのSEM写真について、孔と認識できるすべてのものについて孔径を測定する。孔径は各孔の長径と短径を測定し、孔径=(長径+短径)/2として求める。測定した孔径の算術平均を求め、外表面平均孔径P1および内表面平均孔径P2とする。なお写真内に観察される孔数が多すぎる場合には、写真画像を4等分して、その1つの区域(1/4画面)について、上記の孔径測定を行うことで簡略化してもよい。本発明の中空糸膜の外表面について1/4画面で測定する場合には、測定孔数は概ね200~300個となる。
試長L(図1参照)=200mmの試料中空糸多孔膜をエタノールに15分間浸漬し、次いで純水に15分間浸漬して湿潤化した後、水温25℃、差圧100kPaで測定した1日当りの透水量(m3/day)を、中空糸多孔膜の膜面積(m2)(=外径×π×試長Lとして計算)で除して得た。測定値は、F(100kPa,L=200mm)と表記し、単位はm/day(=m3/m2・day)で表わす。
図2に示す試験装置を用い、中空糸多孔膜試料から形成した浸漬型ミニモジュールについて、ろ過流束1.7m/dayで活性汚泥水の継続的ろ過を行った後、薬品注入逆洗(CIP)処理を行い、中空糸多孔膜内外の差圧がろ過開始直後の値(初期値)まで回復するのに要する時間をCIP回復時間と定義する。
差圧回復率=(TMP2-TMP3)/(TMP2-TMP1)
もし差圧回復率が0.95に満たない場合には次亜塩素酸ソーダ水溶液の注入をさらに10分間行った後、再度吸引ろ過してTMP3を測定して差圧回復率が0.95以上になるまでこの操作を繰り返し、時間tに加算して合計の注入時間をCIP回復時間とする。
上記CIP回復時間の測定において24時間の吸引ろ過を行った後、中空糸多孔膜試料のうちの1本を切り出し、純水で表面を洗い流した後、真空乾燥器を用いて24時間乾燥させた。次いで、走査型電子顕微鏡を用いて外表面を観察倍率5000倍で膜表面堆積物(ケーキ)の有無を観察した。
デュヌイ表面張力試験器を用いてJIS-K3362に従って輪環法により、温度25℃での湿潤処理液の表面張力を測定した。
引っ張り試験機(東洋ボールドウィン社製「RTM-100」)を使用して、温度23℃、相対湿度50%の雰囲気中で初期試料長100mm、クロスヘッド速度200mm/分の条件下で測定した。
重量平均分子量(Mw)が4.1×105のマトリクス用ポリフッ化ビニリデン(PVDF-I)(粉体)とMwが9.7×105の結晶特性改質用ポリフッ化ビニリデン(PVDF-II)(粉体)を、それぞれ75重量%および25重量%となる割合で、ヘンシェルミキサーを用いて混合して、Mwが5.4×105であるPVDF混合物(混合物A;成膜後の結晶化温度Tc=150.4℃)を得た。
混合物Aとして、PVDF-IとPVDF-IIをそれぞれ95重量%および5重量%となる割合で混合したPVDF混合物を用いたこと;混合物Bとして可塑剤としてアジピン酸ポリエステル系可塑剤(末端をオクチルアルコールで封止したアジピン酸と1,2-プロピレングリコールのポリエステル;株式会社ADEKA製「PN150」、数平均分子量約1000、粘度500mPa・s)とN-メチルピロリドン(NMP)とを、82.5重量%/17.5重量%の割合で、常温にて攪拌混合して、可塑剤・溶媒混合物Bを用いたこと;混合物Aと混合物Bを38.4重量%/61.6重量%の割合で供給したこと;水冷却浴温度を40℃にしたこと;延伸倍率を1.85倍としたこと;延伸後の熱処理として、90℃の水浴中で8%の緩和、ついで140℃の空気中で3%の緩和処理を行ったこと;以外は実施例1と同様にしてポリフッ化ビニリデン系多孔膜を得た。
特許文献2の製膜法により製造されたと推認される市販フッ化ビニリデン系樹脂中空糸多孔膜(三菱レイヨン(株)製「ステラポアーSADF2590」)を用いて物性測定を行った。
MBR法による24時間ろ過後膜の外表面をSEM(5000倍)で観察したところ、全面に開孔が確認され、ケーキは観察されなかった。
24時間ろ過後膜の外表面を観察したところ、外表面の約7割がケーキによって覆われ、開口は一部に確認できるのみであった。ろ過後の膜について、CIP処理を開始して30分後に逆洗差圧が平衡に達し、再度吸引ろ過したところ、差圧回復率が0.98であり、CIP回復時間は40分間であった。
ろ過後膜の外表面を観察したところ、全面がケーキによって覆われ、開口を確認することはほとんど出来なかった。ろ過後の膜に、CIP処理を開始して50分後に逆洗差圧が平衡に達し、再度吸引ろ過したところ、差圧回復率が1.00であり、CIP回復時間は50分間であった。
Claims (20)
- 集束イオンビーム・走査型電子顕微鏡により測定される一表面から連続する厚さ10μmの部分における網目状樹脂繊維の平均径が100nm以下且つ空孔率A1が60%以上であり、該一表面側表面孔径P1が0.3μm以下であることを特徴とする、フッ化ビニリデン系樹脂多孔膜。
- 体積1立方μmあたりの空孔分岐点間数が25個以下である請求項1に記載の多孔膜。
- 一表面側表面層空孔率A1と一表面側表面孔径P1との比A1/P1が400以上である請求項1または2に記載の多孔膜。
- 一表面側表面層空孔率A1と全層空孔率A2との比A1/A2が0.9以上である請求項1~3のいずれかに記載の多孔膜。
- 引張り破断強度が7MPa以上、引張り破断伸度が30%以上である請求項1~4のいずれかに記載の多孔膜。
- 延伸されている請求項1~5のいずれかに記載の多孔膜。
- 全体形状が中空糸膜状であり、外表面が前記一表面である請求項1~6のいずれかに記載の多孔膜。
- 請求項1~7のいずれかに記載の多孔膜の前記一表面を被処理水側表面とし、逆側表面を透過水側表面として有するろ水処理膜。
- 重量平均分子量が30万以上のフッ化ビニリデン系樹脂20~50重量%に対して可塑剤50~80重量%を添加し溶融混練して得られた組成物を膜状に溶融押出し、フッ化ビニリデン系樹脂に対して不活性な液体にて片側面から優先的に冷却して固化成膜した後、可塑剤を抽出して網目状多孔ろ水膜を回収する方法において、前記可塑剤が溶融混練組成物の形成温度においてフッ化ビニリデン系樹脂と相溶性を有し、フッ化ビニリデン系樹脂との混練物にフッ化ビニリデン系樹脂単独の結晶化温度とほぼ等しい結晶化温度を与えるポリエステル系可塑剤であり、更に可塑剤の抽出後の多孔膜を、その外表面から5μm以上、且つ膜厚さの1/2以下の深さまで選択的に湿潤させた状態で延伸する工程を含むことを特徴とする、請求項1~8のいずれかに記載のフッ化ビニリデン系樹脂多孔膜の製造方法。
- 組成物の結晶化温度Tc′、溶融押出温度Tdおよび水浴温度Tqの間に、Td-Tc′≧30℃、且つTc′-Tq≧60℃の関係が成立する請求項9に記載の製造方法。
- 前記可塑剤が数平均分子量が1200以上のポリエステル系可塑剤に加えてフッ化ビニリデン系樹脂との相溶性抑制剤を含む請求項9または10に記載の製造方法。
- 前記可塑剤が前記ポリエステル系可塑剤50~98重量%と相溶性抑制剤としてのモノメリックエステル系可塑剤2~50重量%とを含む請求項11に記載の製造方法。
- 前記ポリエステル系可塑剤の温度25℃における粘度が1000mPa・s以上である請求項9~12のいずれかに記載の製造方法。
- 前記ポリエステル系可塑剤はアジピン酸とグリコールのポリエステルである請求項9~13のいずれかに記載の製造方法。
- 前記ポリエステル系可塑剤は分子鎖末端が炭素数9~18の一価アルコールにより封止されているポリエステルである請求項9~14のいずれかに記載の製造方法。
- 前記フッ化ビニリデン系樹脂が、重量平均分子量20万~67万のマトリクス用フッ化ビニリデン系樹脂(PVDF-I)25~98重量%と、重量平均分子量がPVDF-Iの1.8倍以上120万未満を有する結晶特性改質用フッ化ビニリデン系樹脂(PVDF-II)2~75重量部との混合物である請求項9~15のいずれかに記載の製造方法。
- 前記組成物を中空糸膜状に溶融押出し、フッ化ビニリデン系樹脂に対して不活性な液体にて外表面側から優先的に冷却して固化成膜する請求項9~16のいずれかに記載の製造方法。
- フッ化ビニリデン系樹脂と可塑剤からなる前記組成物のDSC測定による結晶化温度Tc′(℃)が140℃以上である請求項9~17のいずれかに記載の製造方法。
- 請求項1に記載のフッ化ビニリデン系樹脂多孔膜を用いて被処理水をろ過するに際し、ろ過と多孔膜の被処理水側表面の曝気とを同時にまたは交互に行うろ過水の製造方法。
- 請求項1に記載のフッ化ビニリデン系樹脂多孔膜を用いて被処理水をろ過してろ過水を得る工程、および前記フッ化ビニリデン系樹脂多孔膜のろ過水側から薬液を注入して膜を洗浄する工程を含むことを特徴とするろ過水の製造方法。
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US20120103895A1 (en) | 2012-05-03 |
JPWO2011007714A1 (ja) | 2012-12-27 |
JP5576866B2 (ja) | 2014-08-20 |
CN102470328B (zh) | 2014-12-31 |
KR20120024965A (ko) | 2012-03-14 |
KR101362553B1 (ko) | 2014-02-13 |
US9096957B2 (en) | 2015-08-04 |
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