WO2004020095A1 - イオン吸着モジュール及び水処理方法 - Google Patents
イオン吸着モジュール及び水処理方法 Download PDFInfo
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- WO2004020095A1 WO2004020095A1 PCT/JP2003/008903 JP0308903W WO2004020095A1 WO 2004020095 A1 WO2004020095 A1 WO 2004020095A1 JP 0308903 W JP0308903 W JP 0308903W WO 2004020095 A1 WO2004020095 A1 WO 2004020095A1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
- B01D15/08—Selective adsorption, e.g. chromatography
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/28—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
- B01J20/28054—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties characterised by their surface properties or porosity
- B01J20/28078—Pore diameter
- B01J20/28083—Pore diameter being in the range 2-50 nm, i.e. mesopores
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/28—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
- B01J20/28054—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties characterised by their surface properties or porosity
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/28—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
- B01J20/28054—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties characterised by their surface properties or porosity
- B01J20/28078—Pore diameter
- B01J20/28085—Pore diameter being more than 50 nm, i.e. macropores
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J39/00—Cation exchange; Use of material as cation exchangers; Treatment of material for improving the cation exchange properties
- B01J39/08—Use of material as cation exchangers; Treatment of material for improving the cation exchange properties
- B01J39/16—Organic material
- B01J39/18—Macromolecular compounds
- B01J39/20—Macromolecular compounds obtained by reactions only involving unsaturated carbon-to-carbon bonds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J41/00—Anion exchange; Use of material as anion exchangers; Treatment of material for improving the anion exchange properties
- B01J41/08—Use of material as anion exchangers; Treatment of material for improving the anion exchange properties
- B01J41/12—Macromolecular compounds
- B01J41/14—Macromolecular compounds obtained by reactions only involving unsaturated carbon-to-carbon bonds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J47/00—Ion-exchange processes in general; Apparatus therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J47/00—Ion-exchange processes in general; Apparatus therefor
- B01J47/02—Column or bed processes
- B01J47/026—Column or bed processes using columns or beds of different ion exchange materials in series
- B01J47/028—Column or bed processes using columns or beds of different ion exchange materials in series with alternately arranged cationic and anionic exchangers
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J47/00—Ion-exchange processes in general; Apparatus therefor
- B01J47/12—Ion-exchange processes in general; Apparatus therefor characterised by the use of ion-exchange material in the form of ribbons, filaments, fibres or sheets, e.g. membranes
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- 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
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
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- 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
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
- C02F2001/422—Treatment of water, waste water, or sewage by ion-exchange using anionic exchangers
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- 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
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
- C02F2001/425—Treatment of water, waste water, or sewage by ion-exchange using cation exchangers
Definitions
- the present invention relates to an ion adsorption module having an extremely short ion exchange zone and a water treatment method.
- Ion exchangers are represented by high-molecular synthetic resins generally referred to as ion-exchange resins. If classified according to product shape, granular or flake-like ion-exchange resins, membrane-like ion-exchange membranes, and fibrous It can be classified as ion exchange fiber.
- Ion exchange resins include cation exchange resins and anion exchange resins. These are further divided into strongly acidic cation exchange resins, weakly acidic cation exchange resins, strongly basic anion exchange resins, and weakly basic anion exchange resins, depending on the degree of acidity and basicity of the ion exchange groups.
- Strong acid cation exchange resin is a sulfonic acid group in the functional group - has (R- S0 3 H +), weakly acidic cation exchange resin is a carboxylic acid functional group (R- C00-H +), phospho phospho groups ( R- P (0) (0—H + ) 2 ), phosphinic acid group (R-PH (0) (0—H +)), arsenite group
- R-OAsO-H + and those having a phenoxide group (R-C 6 H 40- H +) are known.
- Form I shows a slightly stronger basicity than form II.
- Weakly basic anion exchange tree Fats have primary to tertiary amines, and many types are known depending on the type of amine.
- ion-exchange resins are basically classified into four types based on their acidity or basicity.
- the polymer bases that constitute them are styrene-based, phenol-based, acrylic-based, Synthetic polymers such as methacrylic are used, and the matrix structure is classified into gel, expanded network gel (porous), and MR (macroporous) depending on the synthesis method.
- Gel-type ion-exchange resins are, for example, functional groups introduced into a copolymer having a three-dimensional network structure obtained by copolymerizing styrene and divinylbenzene (DVB) in the presence of a catalyst and a dispersant. It is an ion exchange resin obtained by the above.
- Porous ion-exchange resin is a polymer in the presence of an organic solvent capable of swelling the copolymer, which swells and expands the resulting copolymer and compares it to the gel form in the copolymer.
- This is an ion-exchange resin obtained by producing a copolymer with a larger space (gel porosity) and introducing functional groups into it.
- MR-type ion-exchange resin is a copolymer as an aggregate of small spherical gel particles by performing copolymerization in the presence of an organic solvent that is a solvent for the monomer and acts as a precipitant for the copolymer. That is, it is an ion exchange resin obtained by producing a matrix having macropores between the particles and introducing a functional group into the matrix.
- porous ion exchangers having continuous pores are also known.
- a porous body having a particle aggregation type structure is disclosed in F. Svec, Science, 273, 205 to 211 (1996).
- JP-A-10-216717, JP-A-10-192717, JP-A-10-192716 and JP-A-8-252579 disclose a mixture of a cation exchange resin and an anion exchange resin.
- a particle-aggregated porous ion exchanger in which the particles are bound by using a binder polymer is described.
- particle-aggregated porous ion exchangers are organic Using a binder polymer, fine particles or a granular ion exchange resin with ion exchange groups introduced in advance, or by filling the fine particles into a certain mold and melting them by heating to combine them with the porous structure None, and in some cases, the binder polymer is manufactured by introducing ion-exchange groups into a part of the polymer.
- the above-mentioned particle-aggregated porous ion exchanger has a small pore volume and a large mesopore due to the particle-agglomerated structure, so that there is a limitation in performing a large-flow treatment at a low pressure. Further, in the above-mentioned particle aggregate type porous body, ion exchange groups and the like are not uniformly distributed in the porous body.
- the ion exchange group does not exist in the binding polymer part, or even if it exists, the structure of the polymer matrix and ion exchange group differs from that of the ion exchange resin part,
- the density of exchange groups is lower than that of the ion-exchange resin part, and the whole is not a homogeneous ion exchanger.
- the adsorbed ions easily diffuse in the flow direction in the module, and the ion exchange zone, which is a mixed region of the ion-adsorbed portion and the non-adsorbed portion in the module, becomes longer, causing a small amount of adsorbed ions to leak.
- the problem is that the frequency of module replacement increases.
- the ion adsorption tower module that has been widely used in the past is filled with a granular mixed ion-exchange resin, and water to be treated is passed through the ion-exchange resin packed bed to remove ionic impurities.
- the operation of filling the granular mixed ion-exchange resin into the tower requires a supply means for transporting and supplying the granular mixed ion-exchange resin-containing slurry, and also prevents the slurry from leaking out of the tower. Filling is necessary, and the filling operation is not easy.
- the regeneration of the granular ion-exchange resin is performed in the upward flow.
- an object of the present invention is to provide an ion adsorption module in which the ion exchanger is extremely easy to fill and the packed bed does not move even in the upward flow. Even if it rises, the length of the ion-exchange zone can be kept short, the volume of the ion exchanger can be reduced, and a small amount of adsorbed ions will not leak, reducing the frequency of regeneration and improving the processing efficiency. It is an object of the present invention to provide an ion adsorption module and a water treatment method that can be used. Disclosure of the invention
- water to be treated preferably water to be treated previously treated with a granular ion exchange resin conventionally used in general
- a granular ion exchange resin conventionally used in general
- an organic porous material having a specific structure. If the contact treatment is carried out with a porous ion exchanger, the length of the ion exchange zone can be kept short even if the flow rate increases, and the volume of the ion exchanger can be reduced, and no trace of adsorbed ions will occur. Therefore, they have found that the frequency of reproduction is reduced and that the processing efficiency can be improved, and the present invention has been completed.
- the present invention (1) provides a container having at least an opening into which water to be treated flows, and a mesopore having an average diameter of 1 to 1000 m in the walls of the connected macropore and macropore filled in the container. It has an open-cell structure with a total pore volume of lm1 / g to 50m1 / g, ion exchange groups are uniformly distributed, and ion exchange capacity is 0.5mg equivalent / g dry pore. It is intended to provide an ion-adsorbing module including an organic porous ion exchanger having a three-dimensional network structure that is at least a porous body.
- the porous ion exchanger can be easily produced as a block shape that fits in a filling container, for example, and can be easily filled.
- the present invention can be applied to any of the continuous water flow treatment method generally used in conventional modules and the batch treatment method in which the water is introduced into the water in a storage container or a storage tank.
- the length of the ion exchange zone can be kept short even if the flow rate increases with a compact device. The volume of the solution can be reduced, and a small leak of adsorbed ions does not occur, so that the frequency of regeneration is reduced and the processing efficiency can be improved.
- the present invention (3) is characterized in that the organic porous ion exchanger is an organic porous cation exchanger and an organic porous anion exchanger, and the organic porous cation exchanger and the organic porous ion exchanger are
- An object of the present invention is to provide the ion adsorption module obtained by stacking and filling an anion exchanger. According to the present invention, the packing of the porous ion exchanger is easier, and the packed bed does not move even if it is placed in an upward flow at the time of regeneration.
- the present invention (4) provides a granular ion-exchange resin packed layer, an open-cell structure having macropores connected to each other, and mesopores having an average diameter of 1 to 1000 xm in the walls of the macropores.
- the total pore volume is from lm1 / g to 50m1 / g, the ion exchange groups are uniformly distributed, and the ion exchange capacity is 0.5mg equivalent / g or more.
- the present invention provides an ion-adsorbing module in which an organic porous ion-exchanger packed layer having the following is laminated in this order from the upstream side.
- the present invention (5) provides the ion adsorption module, wherein the ion adsorption module is disposed downstream of the ion adsorption module filled with a granular ion exchange resin. According to the present invention, the same effect as the above invention (4) is obtained.
- the present invention (6) has an open-cell structure having an interconnected macropore and a mesopore having an average diameter of 1 to 1000 m in the wall of the macropore, and a total pore volume of lm 1 / g to 50 m. 1 / g, ion-exchange groups are uniformly distributed, and ion-exchange capacity is 0.5 mg equivalent / g or more.
- An object of the present invention is to provide a water treatment method in which ionic substances in the water to be treated are adsorbed and removed by contact with water. According to the present invention, the same effects as those of the inventions (1) to (3) can be obtained.
- the present invention (7) provides the water treatment method, wherein the water to be treated is treated water previously treated with a granular ion exchange resin. According to the present invention, the same effects as (4) and (5) can be obtained.
- FIG. 1 is a diagram showing the relationship between the Na ion load / total exchange capacity and the Na ion concentration of the treated water in the water flow test 1
- Fig. 2 is the silica load / total
- FIG. 3 is a diagram showing a relationship between an exchange capacity and a silica concentration of treated water
- FIG. 3 is a diagram showing a relationship between a water passage speed, an exchange zone length, and a Na ion concentration of treated water in a water passage test 1.
- a basic structure of an organic porous ion exchanger (hereinafter, also referred to as a porous ion exchanger) to be filled is defined by macropores connected to each other and the inside of the walls of the macropores. It has an open cell structure having mesopores with a diameter of 1 to 1000 m, preferably 10 to 100/1 m. That is, the open-cell structure usually has macropores having an average diameter of 2 to 5000 m and macropores overlapping each other, and this overlapping portion has a mesopore that serves as a common opening, and most of the open-pore structure is used. You.
- the porous ion exchanger In an open pore structure, when water flows, a flow path is formed in a bubble structure formed by the macropores and the mesopores. If the average diameter of the mesopores is less than 1 zm, the pressure loss during water flow will increase.On the other hand, if the average diameter of the mesopores is greater than 1000 m, it will be difficult to form a uniform water flow path. I don't like it.
- the structure of the porous ion exchanger has an open cell structure as described above, the pore volume and specific surface area can be significantly increased. Further, the porous ion exchanger is a porous body having a total pore volume of lm1 / g to 50m1 / g.
- the total pore volume is less than lm 1 / g, the amount of water per unit cross-sectional area decreases, and it is not preferable because the amount of water cannot be increased.
- the total pore volume exceeds 50 m 1 / g, the proportion of the skeleton portion of the polymer or the like is reduced, and the strength of the porous body is significantly reduced, which is not preferable.
- An organic polymer material having a chemical constraint point such as a crosslinked structure or a physical constraint point such as a crystal part is used as a material of a skeleton portion forming an open cell structure.
- the polymer material When the polymer material is a polymer having a crosslinked structure, the polymer material preferably contains 5 to 90 mol% of the crosslinked structure unit based on all the constituent units constituting the polymer material. If the cross-linking structural unit is less than 5 mol%, the mechanical strength is insufficient, which is not preferable. It is not preferable because introduction of an exchange group becomes difficult and ion exchange capacity is reduced.
- the type of the polymer material examples thereof include styrene polymers such as polystyrene, poly (methyl styrene), and polyvinyl benzyl chloride and cross-linked products thereof; polyolefins such as polyethylene and polypropylene, and cross-linked products thereof.
- Polyhalogenated olefins such as polyvinyl chloride and polytetrafluoroethylene; cross-linked products thereof; nitrile polymers such as polyacrylonitrile and cross-linked products thereof; (meth) acrylics such as polymethyl methacrylate and polyethyl acrylate -Based polymers and their crosslinked products; styrene-divinylbenzene copolymer, vinylbenzyl chloride-divinylbenzene copolymer and the like.
- the above-mentioned polymer may be a homopolymer obtained by polymerizing a single monomer, a copolymer obtained by polymerizing a plurality of monomers, or a blend of two or more polymers. There may be.
- styrene-divinylbenzene copolymer and vinylbenzyl-clawlide-divinylbenzene copolymer are preferred materials because of their ease of introduction of ion-exchange groups and high mechanical strength.
- the porous ion exchanger used in the present invention has a uniform distribution of ion exchange groups and an ion exchange capacity of at least 0.5 mg equivalent / g dry porous body, preferably 2.Omg equivalent / g It is a porous ion exchanger of a dry porous body or more. If the ion exchange capacity is less than 0.5 mg equivalent / g dry porous material, the ion adsorption capacity becomes insufficient and the frequency of replacing modules and the like increases, which is not preferable.
- the ion-exchange groups are uniformly distributed” means that the distribution of the ion-exchange groups is at least m-order and uniform.
- the distribution of ion-exchange groups can be confirmed relatively easily by using an electron beam microanalyzer (EPMA) or secondary ion mass spectrometry (SIMS).
- the ion exchange groups introduced into the organic porous ion exchanger include cation exchange groups such as carboxylic acid groups, iminodiacetic acid groups, sulfonic acid groups, phosphoric acid groups, aminophosphate groups, iminophosphate groups, and aromatic hydroxyl groups.
- Anion exchange groups such as quaternary ammonium group, tertiary amino group, secondary amino group, primary amino group, polyethyleneimine, tertiary sulfonium group, phosphonium group; amphoteric ion exchange groups such as betaine and sulfobetaine; iminodiacetic acid And chelating groups such as a phosphoric acid group, a phosphoric acid ester group, an amino phosphoric acid group, an imino phosphoric acid group, an aromatic hydroxyl group, an aliphatic polyol, and a polyethyleneimine. These may be used alone or in combination according to the purpose. It can be introduced into a porous ion exchanger.
- the porous ion exchanger used in the present invention needs to be a sponge structure having an open cell structure connected to the outside.
- the sponge structure referred to here is Takeuchi Yong: Properties of porous material and its applied technology, as described in P.2-5, Fuji Techno System (2000). It refers to a bubble-dispersed porous body, and is disclosed in JP-A-10-216717, JP-A-10-192717, JP-A-10-192716, and JP-A-8-252579. It has a completely different structure from the particle-agglomerated porous body.
- the porous body has a sponge structure
- the cell structure can be formed uniformly, and the total pore volume and specific surface area can be significantly increased as compared with the particle-agglomerated porous body. , Very good It is profitable.
- ion exchange groups and the like are uniformly distributed as described above, diffusion of the adsorbed ions in the flow direction in the module is small, The exchange zone is short, and it is unlikely to cause a trace leak of adsorbed ions, so that the module can be used stably for a long period of time.
- the method for producing the porous ion exchanger is not particularly limited, and includes a method in which a component containing an ion exchange group is converted into a porous ion exchanger in one step, and a method in which a porous material is converted into a component without an ion exchange group. And then introducing an ion exchange group.
- An example of a method for producing a porous ion exchanger will be described below. That is, the porous ion exchanger is obtained by mixing an oil-soluble monomer containing no ion-exchange group, a surfactant, water and, if necessary, a polymerization initiator to obtain a water-in-oil emulsion. It is produced by polymerizing this into a porous body and further introducing ion exchange groups.
- the oil-soluble monomer containing no ion-exchange group refers to a monomer that does not contain an ion-exchange group such as a carboxylic acid group and a sulfonate group, has low solubility in water, and is lipophilic.
- Some specific examples of these monomers include styrene, methylstyrene, vinyltoluene, vinylbenzyl chloride, divinylbenzene, ethylene, propylene, isobutene, butadiene, isoprene, chloroprene, vinyl chloride, vinyl bromide, vinylidene chloride, Tetrafluoroethylene, acrylonitrile, methacrylonitrile, vinyl acetate, methyl acrylate, ethyl acrylate, butyl acrylate, 2-ethylhexyl acrylate, trimethylolpropane triacrylate, butanediol diatalylate, Methyl methacrylate, ethyl methacrylate, propyl methacrylate, butyl methacrylate, 2-ethylhexyl methacrylate, cyclohexyl methyl methacrylate, benzyl methyl acrylate, benzyl methacryl
- a crosslinkable monomer such as divinylbenzene or ethylene dalicol dimethacrylate is selected as at least one component of the monomer, and its content is 1 to 90 mol% in the total oil-soluble monomer.
- the content is preferably from 3 to 80 mol%, since the mechanical strength required for introducing a large amount of ion-exchange groups in a later step can be obtained.
- the surfactant is not particularly limited as long as it can form a water-in-oil (W / 0) emulsion when an oil-soluble monomer containing no ion-exchange group and water are mixed.
- Nonionic surfactants such as sorbitan monolaurate, sorbitan monopalmitate, sorbitan monostearate, sorbitan trioleate, polyoxyethylene nonylphenyl ether, and monomonooleate; potassium oleate, Anionic surfactants such as sodium decylbenzenesulfonate and dioctyl sodium sulfosuccinate; cationic surfactants such as distearyl dimethyl ammonium chloride; and amphoteric surfactants such as lauryl dimethyl bayone Can be used.
- surfactants can be used alone or in combination of two or more.
- water-in-oil type emulsion refers to an emulsion in which an oil phase is a continuous phase and water droplets are dispersed therein.
- the addition amount of the above surfactants cannot be unconditionally determined because it greatly varies depending on the type of the oil-soluble monomer and the size of the target emulsion particles (macropores), but the total amount of the oil-soluble monomer and the surfactant can be unclear. Can be selected in the range of about 2 to 70%.
- methanol is used as long as micropores, which are discontinuous pores, are not formed.
- Alcohols such as toluene and stearyl alcohol; carboxylic acids such as stearic acid; and hydrocarbons such as benzene, toluene, octane, and dodecane can be coexisted in the system.
- the polymerization initiator a compound that generates a radical by heat and light irradiation is preferably used.
- the polymerization initiator may be water-soluble or oil-soluble, and may be, for example, azobisisobutyronitrile, azobiscyclohexane nitrile, azobiscyclohexanecarbonitrile, benzoyl peroxide, potassium persulfate, peroxide, etc. Ammonium sulfate, hydrogen peroxide-ferrous chloride, sodium persulfate-sodium acid sulfite, tetramethylthiuram disulfide and the like. However, in some cases, polymerization may proceed only by heating or light irradiation without adding a polymerization initiator, and therefore, it is not necessary to add a polymerization initiator in such a system.
- the mixing device for forming the emulsion there is no particular limitation on the mixing device for forming the emulsion, and a normal mixer, a homogenizer, a high-pressure homogenizer, a planetary stirring device, or the like can be used, and an emulsification that can obtain a desired emulsion particle size can be used. Conditions can be set arbitrarily.
- the polymerization conditions for polymerizing the water-in-oil emulsion thus obtained can be selected from various conditions depending on the type of the monomer and the polymerization initiator system. For example, when azobisisobutyronitrile, benzoyl peroxide, potassium persulfate, etc. are used as the polymerization initiator, the sealed container in an inert atmosphere Heat polymerization at 30 to 100 ° C for 1 to 48 hours may be used. If hydrogen peroxide-ferrous chloride, sodium persulfate-sodium sulfite is used as a polymerization initiator, an inert atmosphere is used. In the lower sealed container, the polymerization may be carried out at 0 to 30 for 1 to 48 hours. After completion of the polymerization, the content is taken out, and if necessary, a porous body is obtained by extracting with a solvent such as isopropanol for the purpose of removing unreacted monomers and surfactant.
- a solvent such as isopropan
- the method for introducing the ion-exchange groups into the porous body is not particularly limited, but an introduction method by a polymer reaction is preferable in that the ion-exchange groups can be introduced with high density and uniformity.
- a method for introducing a sulfonic acid group when the organic porous material is a styrene-divinylbenzene copolymer or the like, a sulfonation method using sulfuric acid, concentrated sulfuric acid, or fuming sulfuric acid may be used.
- a method for introducing a quaternary ammonium group if the organic porous material is a styrene-divinylbenzene copolymer or the like, a chloromethyl group is introduced with octamethylmethyl ether, and then tertiary amine is added.
- Examples of the method for introducing betaine include a method in which a tertiary amine is introduced into an organic porous material by the same method as described above, followed by a reaction with monoiodoacetic acid, and the like.
- an aliphatic polyol which is a chelate-forming group a method of reacting N-methyldalcamine or the like with an organic porous material having a co-methyl group is exemplified.
- the ion exchange group to be introduced include a cation exchange group such as a carboxylic acid group, an iminodiacetic acid group, a sulfonic acid group, a phosphate group, an aminophosphate group, an iminophosphate group, an aromatic hydroxyl group; a quaternary ammonium group and a tertiary group.
- Anion exchange groups such as amino group, secondary amino group, primary amino group, polyethylenimine, tertiary sulfonium group, phosphonium group; amphoteric ion exchange groups such as betaine and sulfobetaine; iminodivinegar Chelate forming groups such as acid groups, phosphate groups, phosphate groups, aminophosphate groups, iminophosphate groups, aromatic hydroxyl groups, aliphatic polyols, and polyethyleneimines. These can be introduced alone or in combination. A porous ion exchanger is obtained.
- a precipitant that is a poor solvent for the polymer formed by the polymerization of the oil-soluble monomer and dissolves the oil-soluble monomer in the pre-polymerization stage is added, and then the polymerization is performed.
- a water-drop emulsion may be prepared.
- minute irregularities can be formed on the surface of the flow path in the porous structure of the porous body, and the adsorption performance can be improved.
- Various precipitants can be selected depending on the type of the oil-soluble monomer.
- aliphatic hydrocarbons such as hexane, heptane, octane, isooctane, and decane; Alcohols such as 2-butanol and methyl isobutyl carbinol can be used.
- the amount of the precipitant varies depending on the content of divinylbenzene in the oil-soluble monomer, but is 10 to 70%, preferably 20 to 60% based on the total amount of the oil-soluble monomer and the precipitant. You can select from 0%.
- the initial polymer of styrene and divinylbenzene becomes difficult to dissolve in oils such as oil-soluble monomers, and as a result, precipitates in the form of microparticles, and these microparticles are removed. It becomes an aggregate and develops small irregularities on the surface.
- the amount of the precipitating agent is large, many micropores are developed, but the strength tends to decrease.
- the pore size of the micropores can be controlled by appropriately selecting the amount of the precipitant and the ratio of the crosslinkable monomer to the precipitant.
- a linear polymer which is a polymer of an oil-soluble monomer may be used.
- An ion adsorption module includes a container having at least an opening into which water to be treated flows, and the porous ion exchanger filled in the container. If this container has only an opening into which water to be treated flows, it can be applied to a batch processing method in which the ion adsorption module is charged into water in a storage container or a storage tank to purify the water. However, as long as it has a treated water inflow pipe into which treated water flows, and a treated water outflow pipe from which treated water flows out, it can be applied to a continuous water flow treatment method generally used conventionally.
- the form of contact between the water to be treated and the ion adsorption module is not particularly limited as long as the water to be treated is brought into contact with the porous ion exchanger, and a simple columnar or polygonal column-shaped packed bed can be used.
- Upflow or downflow water flow external pressure method to flow water from the outside to the inner cylinder in the cylindrical packing layer, internal pressure method to flow water in the opposite direction, filling a large number of cylindrical organic porous materials, Examples thereof include a tubular system in which water is passed by an internal pressure system or an external pressure system, a flat membrane system using a sheet-shaped packed bed, and a split system in which a flat membrane is molded into a folded shape.
- the porous ion exchanger to be filled a block shape, a sheet shape, a plate shape, a columnar shape, a cylindrical shape, or the like is selected according to the shape of the container of the module adopting the adsorption mode.
- the porous ion exchanger may be a spherical or irregular granular small block of 0.1 mm to 10 mm, and this small block may be filled in a container to form a packed layer.
- Examples of the method of forming the porous ion exchanger of these various shapes include a method of cutting from a block-shaped porous ion exchanger, and a method of filling the above-mentioned emulsion into a mold of a desired shape and performing polymerization in the mold. And the like.
- the type and form of the porous ion exchanger packed in the container are not particularly limited, and can be arbitrarily determined according to the purpose of use and the type of ionic impurities to be adsorbed. Specifically, there is a form in which a porous cation exchanger and a porous anion exchanger are filled alone or mixed in a container.
- Examples of the form in which the porous ion exchanger is mixed include a form which is formed or processed into a block shape, a sheet shape, a plate shape or a column shape, and is laminated in the water-passing direction, or a small block ion exchanger. And filling the mixture.
- those obtained by laminating and filling a porous cation exchanger and a porous anion exchanger are preferable in that the preparation of the porous ion exchanger and the filling of the container are easy.
- the ion exchange module includes a layer in which a granular ion exchange resin packed layer and the porous ion exchanger packed layer are laminated in this order from the upstream side, and An ion adsorption module filled with a porous ion exchanger is disposed downstream of an ion adsorption module filled with a granular ion exchange resin.
- the former configuration can omit the connection piping compared to the latter configuration.
- the upstream granular ion exchange resin is preferably a mixed ion exchange resin of a cation exchange resin and an anion exchange resin
- the downstream porous ion exchanger is a stacked packed layer of a porous cation exchanger and a porous anion exchanger. I like it.
- the shape of the ion exchange module used in the present invention is not particularly limited, and examples thereof include a column shape, a flat shape, and a tower shape having a head portion at a lower portion.
- the flat (small drum-shaped) ion exchange module has an ion-exchanger packed bed that is short in the water flow direction and long in the direction (diameter) perpendicular to the water flow direction. Suitable for the method.
- a so-called ion exchange tower having a head portion at the lower portion is used in the case of laminating and filling the granular ion exchange resin and the porous ion exchanger in the above-mentioned other embodiment.
- a conventional ion exchange tower with a head plate in the lower part is a desalination part filled with granular ion exchange resin and a pumice stone (Tekapore) serving as a plate or distributor from the upstream to the downstream.
- a pumice stone Tekapore
- the porous ion exchanger was replaced with the end plate of the end plate part or pumice stone (Tekapore). It is only necessary to pack, which increases the efficiency of adsorption of ionic impurities in high-speed flow, reduces the number of parts in the tower because the porous ion exchanger plays the role of distributor, and enables regeneration by upward flow. The regeneration efficiency is improved without moving the packed layer.
- the porous ion exchanger can be obtained, for example, as a block shape that fits in a filling container, and can be easily filled.
- ion-exchange resin is regenerated in an upward flow, separated according to the specific gravity difference between the cation-exchange resin and the anion-exchange resin, and then regenerated with a chemical.
- the ion adsorption module of the present invention has a problem that the ion-exchanger can be regenerated in an upward direction during regeneration of the ion exchanger. The packed bed does not move when placed in a stream.
- the water treatment method of the present invention includes a method of contacting water to be treated with the porous ion exchanger to adsorb and remove ionic impurities in the water to be treated (first water treatment method).
- the first treated water obtained by contacting the granular ion exchange resin is further contacted with the porous ion exchanger.
- This is a method of obtaining the second treated water by the above method (second method of water treatment).
- the porous ion It is suitable for a water treatment method that frequently uses a small device that can be easily filled with exchangers and that is frequently regenerated.
- the length of the ion exchange zone can be kept short even at a high flow rate, and the volume of the ion exchanger can be reduced.
- the second method of water treatment even if the amount of ionic impurities is very small, the adsorption rate is high, and leakage of the adsorbed ions hardly occurs.
- the particle size of the granular ion exchange resin is between 0.2 and 0.5, the diffusion rates inside and outside the particles are significantly different, and as the flow rate increases, it becomes a mixed area of ion-adsorbed and non-adsorbed parts.
- the length of the ion exchange zone becomes longer and a small amount of adsorbed ions leak, the total exchange capacity is large, so that ions can be roughly removed.
- an organic porous ion exchanger having a three-dimensional network structure has a small total exchange capacity but does not spread in diffusion rate, so that the ion exchange band length can be kept short even at a high flow rate.
- the ion adsorption module can be used, for example, as a substitute for a cartridge polisher used in a subsystem of a conventional ultrapure water production apparatus.
- the water to be treated is passed through, and the target ion in the water to be treated is removed.
- a method of removing the ions by adsorption and removing the ions having low adsorption selectivity into the water to be treated may be used. Specifically, removal
- the porous ion exchanger is a cation exchanger, the cation exchanger is converted into a sodium form, and then the water to be treated is passed through, and A softening method of exchanging the hardness component with sodium may be used. According to this method, the hardness component in the water to be treated can be easily removed.
- porous ion exchanger used in the ion exchange module and the water treatment method of the present invention is repeatedly used for the ion adsorption removal treatment, a regenerated treatment with a chemical can be used.
- a regeneration treatment method an ionic substance adsorbed on the porous ion exchanger is desorbed by contacting an acid with a porous cation exchanger and an alkali with a porous anion exchanger, respectively.
- the acid include hydrochloric acid, sulfuric acid, and nitric acid
- examples of the alkali include caustic soda.
- the method of contact between the drug and the porous ion exchanger is not particularly limited whether it is an ascending flow or a descending flow.Even when other ion exchangers such as granular ion exchange resin are mixed, each ion exchanger can be used. No separation operation is required.
- this porous body had an open cell structure continuous with the outside, the average cell diameter was 3 mm, and the total pore volume was 22 m 1 / g.
- the porous cation exchanger obtained in Production Example 1 was cut in a wet state and packed in a column having a diameter of 2.55 cm and a height of 30 cm. After regenerating with 1 N hydrochloric acid, it was fully washed with ultrapure water to obtain a regenerated type, and an ion adsorption module A was obtained.
- NaCl was added to pure water to obtain low-concentration simulated contaminated pure water, which was passed through the ion adsorption module A, and a module life test was performed.
- the sodium chloride concentration of the simulated contaminated pure water passing through the ion adsorption module was 25 Og / K.
- the sodium ion adsorption amount (adsorption rate) with respect to the total exchange capacity at the point where the sodium concentration exceeded 1 Lg was measured.
- Fig. 1 shows the results. From FIG. 1, the adsorption rate of the porous cation exchanger was 83%. The length of the ion exchange zone was short as indicated by the symbol a.
- porous body was taken out, washed with acetone, washed with water, and dried to obtain a porous anion exchanger.
- the ion exchange capacity of this porous body was 3.5 mg equivalent / g in terms of dry porous body, and it was confirmed by SIMS that the trimethylammonium group was uniformly introduced into the porous body. Further, this porous ion exchanger had an open cell structure continuous with the outside, the average value of the cell diameter was 3 rn, and the total pore volume was 22 m 1 / g.
- the ion adsorption module A was replaced with the ion adsorption module B, and the low concentration silica simulated contaminated water (silica concentration: 17.5 g / 1) was prepared by adding silica to pure water instead of sodium chloride simulated contaminated pure water. )), Except that the test was the same as in the water flow test 1.
- Fig. 2 shows the results. From FIG. 2, the ion adsorption rate at the point where the silica concentration of the treated water obtained by passing the water through the ion adsorption module B exceeded 1 ig / 1 was 12%.
- Example 1 was repeated except that the water flow rate (LV) to the ion adsorption module was 20 m / hr (Example 3), 5 Om / hr (Example 4) and 70 m / hr (Example 5).
- the test was performed in the same manner as in the water test. The results are shown in FIG. FIG. 3 also shows the results of Example 1.
- Comparative Example 1 The flow rate of Comparative Example 1 was changed except that the water flow rate (LV) to the ion adsorption module was 50 m / hr (Comparative Example 3), 7 Om / hr (Comparative Example 4) and 90 m / hr (Comparative Example 5).
- the test was performed in the same manner as in the water test.
- the results are shown in FIG. FIG. 3 also shows the results of Comparative Example 1. 1 and 2 that Examples 1 and 2 have a higher adsorption rate and a slower leak than Comparative Examples 1 and 2. For this reason, useless resin can be reduced, and the volume of the ion exchange module can be reduced.
- the length of the ion exchange zone in the example is shorter than that in the comparative example because the diffusion speed does not spread even when the flow rate increases.
- the ion adsorption module of this invention packing of an ion exchanger is extremely easy, and a packed bed does not move even if it is an upward flow.
- the ion adsorption module and the water treatment method of the present invention can keep the length of the ion exchange zone short even when the flow rate increases, thereby reducing the volume of the ion exchanger, and reducing the amount of adsorbed ions. Since no leakage occurs, the frequency of regeneration is reduced, and processing efficiency can be improved.
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- Chemical & Material Sciences (AREA)
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- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Nanotechnology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
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- Treatment Of Water By Ion Exchange (AREA)
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US10/510,964 US7294265B2 (en) | 2002-08-28 | 2003-04-14 | Ion adsorption module and method for water treatment |
AU2003252498A AU2003252498A1 (en) | 2002-08-28 | 2003-07-14 | Ion adsorption module and method for water treatment |
EP03791181A EP1533033A4 (en) | 2002-08-28 | 2003-07-14 | ION ADSORPTION MODULE AND HYDRAULIC PROCESSING METHOD |
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JP2002-248504 | 2002-08-28 | ||
JP2002248504A JP4011440B2 (ja) | 2002-08-28 | 2002-08-28 | イオン吸着モジュール及び水処理方法 |
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WO2004020095A1 true WO2004020095A1 (ja) | 2004-03-11 |
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PCT/JP2003/008903 WO2004020095A1 (ja) | 2002-08-28 | 2003-07-14 | イオン吸着モジュール及び水処理方法 |
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US (1) | US7294265B2 (ja) |
EP (1) | EP1533033A4 (ja) |
JP (1) | JP4011440B2 (ja) |
KR (1) | KR100947416B1 (ja) |
CN (1) | CN1297347C (ja) |
AU (1) | AU2003252498A1 (ja) |
WO (1) | WO2004020095A1 (ja) |
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CN113757755A (zh) * | 2021-08-03 | 2021-12-07 | 孟祥磊 | 一种增紊流型集中供暖循环水管线 |
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JP5411737B2 (ja) * | 2009-03-10 | 2014-02-12 | オルガノ株式会社 | イオン吸着モジュール及び水処理方法 |
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WO2016190507A1 (ko) * | 2015-05-27 | 2016-12-01 | 전북대학교 산학협력단 | 고속 흡착 필터를 포함하는 흡착장치 |
KR20190072667A (ko) | 2016-11-14 | 2019-06-25 | 리락 솔루션즈, 인크. | 코팅된 이온 교환 입자를 이용한 리튬 추출 |
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WO2018146310A1 (en) | 2017-02-13 | 2018-08-16 | Merck Patent Gmbh | A method for producing ultrapure water |
WO2019028148A1 (en) | 2017-08-02 | 2019-02-07 | Lilac Solutions, Inc. | LITHIUM EXTRACTION WITH POROUS ION EXCHANGE BALLS |
JP7427598B2 (ja) | 2018-02-28 | 2024-02-05 | ライラック ソリューションズ,インク. | リチウム抽出用の粒子トラップを備えたイオン交換反応器 |
KR20230023714A (ko) | 2020-06-09 | 2023-02-17 | 리락 솔루션즈, 인크. | 스케일런트의 존재 하에서의 리튬 추출 |
JP2024519679A (ja) | 2021-04-23 | 2024-05-21 | ライラック ソリューションズ,インク. | リチウムを抽出するためのイオン交換装置 |
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Also Published As
Publication number | Publication date |
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JP2004082027A (ja) | 2004-03-18 |
EP1533033A1 (en) | 2005-05-25 |
US20050139549A1 (en) | 2005-06-30 |
KR20050032028A (ko) | 2005-04-06 |
KR100947416B1 (ko) | 2010-03-12 |
CN1642650A (zh) | 2005-07-20 |
EP1533033A4 (en) | 2007-12-05 |
CN1297347C (zh) | 2007-01-31 |
JP4011440B2 (ja) | 2007-11-21 |
AU2003252498A1 (en) | 2004-03-19 |
US7294265B2 (en) | 2007-11-13 |
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