WO2006062176A1 - Appareil electrique de production de liquide desionise et procede de production de liquide desionise - Google Patents

Appareil electrique de production de liquide desionise et procede de production de liquide desionise Download PDF

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Publication number
WO2006062176A1
WO2006062176A1 PCT/JP2005/022600 JP2005022600W WO2006062176A1 WO 2006062176 A1 WO2006062176 A1 WO 2006062176A1 JP 2005022600 W JP2005022600 W JP 2005022600W WO 2006062176 A1 WO2006062176 A1 WO 2006062176A1
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WIPO (PCT)
Prior art keywords
liquid
region
desalting
ion exchanger
ion
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PCT/JP2005/022600
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English (en)
Japanese (ja)
Inventor
Hisashi Mizuochi
Koji Yamanaka
Naoyuki Tajima
Hiroshi Inoue
Akira Nakamura
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Organo Corporation
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Publication of WO2006062176A1 publication Critical patent/WO2006062176A1/fr

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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
    • B01J47/06—Column or bed processes during which the ion-exchange material is subjected to a physical treatment, e.g. heat, electric current, irradiation or vibration
    • B01J47/08—Column or bed processes during which the ion-exchange material is subjected to a physical treatment, e.g. heat, electric current, irradiation or vibration subjected to a direct electric current
    • 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
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
    • C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
    • C02F1/4695—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis electrodeionisation
    • 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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination

Definitions

  • the present invention uses ion exchange membranes used in various industries such as semiconductor manufacturing industry, pharmaceutical industry, food industry, power plant, laboratory, etc. using deionized liquid or in manufacturing sugar liquid, juice, wine, etc.
  • the present invention relates to an electric deionization liquid production apparatus and a deionization liquid production method with a simplified apparatus structure.
  • a conventional electric deionized liquid production apparatus basically has a mixed ion exchange resin layer of an anion exchange resin and a cation exchange resin as an ion exchanger in a gap formed by a cation exchange membrane and an anion exchange membrane. Filling it into a deionization chamber, allowing the liquid to be processed to pass through the ion exchange resin layer, and applying a direct current to the flow of the liquid to be processed through the ion exchange membrane in the vertical direction, A deionized liquid is produced while electrically removing ions in the liquid to be treated in the concentrated liquid flowing outside the two ion exchange membranes.
  • Japanese Patent Application Laid-Open No. 2000-033 3 4 5 60 discloses a deionization chamber filled with a monolithic organic porous ion exchanger (hereinafter, also simply referred to as “monolith”).
  • monolithic organic porous ion exchanger hereinafter, also simply referred to as “monolith”.
  • the deionized water is removed to remove ionic impurities in the water to produce deionized water, and a DC electric field is applied to the deionized chamber to adsorb to the monolith.
  • the application of the DC electric field is performed in such a way that a number of deionization chambers are arranged in parallel if the ions to be eliminated migrate in the direction opposite to the direction of water flow in the monolith. It is disclosed that the structure of the apparatus can be simplified and material costs, processing costs, and assembly costs can be reduced.
  • Patent Document 1 Japanese Patent Laid-Open No. 2 00 3-3 3 4 5 6 0 (Claim 1, Paragraph No. 0 0 3 0)
  • an object of the present invention is to further simplify the structure of the apparatus than the conventional one without using an ion exchange membrane, and to prevent the occurrence of scale, and an apparatus for producing an electric deionized liquid and a deionized liquid. It is to provide a manufacturing method.
  • a desalting region filled with an ion exchanger and a part of the liquid to be processed disposed adjacent to the ion exclusion side of the desalting region are
  • an electro-deionized liquid production system equipped with a permeating liquid permeation area a part of the liquid to be treated introduced into the desalting area is allowed to pass through the liquid permeation area to be electrophoretically excluded. If the structure discharges together with impurities into the electrode chamber or the concentration chamber, the device structure can be further simplified than the conventional one without using an ion exchange membrane.
  • the inventors have found that the generation of scale can be prevented by the diluting effect of the permeate to be treated, and have completed the present invention.
  • the present invention includes a desalting region filled with an ion exchanger, a liquid permeable region through which a part of the liquid to be disposed disposed adjacent to the ion exclusion side of the desalting region, and the desalting region.
  • An electrode disposed on both sides of the salt region and the liquid permeation region, a liquid inflow pipe to be treated for passing the liquid to be treated, an electrode chamber or a concentration chamber for discharging the liquid that has permeated from the liquid permeation region,
  • a desalting solution outlet pipe for discharging desalted solution from the desalting region; and at least a porous ion exchanger in the liquid permeation region.
  • a deionized liquid production apparatus is provided.
  • the present invention also provides a desalting solution by passing a processing solution through a desalting region filled with an ion exchanger and adsorbing and removing ionic impurities in the processing solution.
  • an electric deionization liquid production apparatus that removes adsorbed ionic impurities by electrophoretic application by applying an electric field to the desalting region, at least adjacent to the ion exclusion side of the desalting region A part of the liquid to be treated introduced into the desalting region is allowed to pass through the porous ion exchanger, and is discharged into the electrode chamber or the concentration chamber together with the ionic impurities that are electrophoretically excluded.
  • a method for producing a deionized liquid is provided.
  • the structure of the apparatus can be further simplified than the conventional one without using an ion exchange membrane, In the liquid permeation region, scale can be prevented from being generated due to the dilution effect of the liquid to be treated.
  • FIG. 1 is a schematic diagram showing the structure of an electrical deionized liquid production apparatus according to the first embodiment of the present invention
  • FIG. 2 is an electrical diagram of the second embodiment of the present invention
  • FIG. 3 is a schematic diagram showing the structure of the deionized liquid production apparatus
  • FIG. 3 is a schematic diagram showing the structure of the electric deionized liquid production apparatus of the third embodiment of the present invention
  • FIG. 5 is a schematic diagram showing the structure of an electrical deionized liquid production apparatus according to a fourth embodiment of the present invention, and FIG. 5 shows a desorption used in the electrical deionized liquid production apparatus of FIG.
  • FIG. 6 is a schematic diagram showing the structure of the electrical deionized liquid production apparatus of Example 2, and FIG.
  • FIG. 7 is a diagram illustrating the filling state of the ion region and the liquid permeable region.
  • FIG. It is a figure explaining the filling state of the deionization area
  • the ion exchanger filled in the demineralization zone is not particularly limited, and is filled in the conventional EDI demineralization chamber.
  • Examples of such an ion exchanger include monoliths, granular ion exchange resins, and mixtures of monoliths and granular ion exchange resins.
  • the monolith is an open cell having a mesopore having an average diameter of 1 to 100 ⁇ m, preferably 10 to 100 ⁇ m in the wall of the mac mouth pores connected to each other.
  • the total pore volume is 1 to 50 ml / g, preferably 4 to 20 ml / g, the ion exchange groups are uniformly distributed, and the ion exchange capacity is 0.5 mg equivalent / g dry porous. The thing more than a solid body is mentioned. Further, the flow resistance of the monolith is made smaller than that of the porous ion exchanger loaded in the liquid permeation region. When the porous ion exchanger is a monolith, the average diameter of the mesopore is set to be smaller than the average diameter of the monolith loaded in the desalting region.
  • the liquid permeation region is loaded with a porous ion exchanger, and is disposed adjacent to the ion exclusion side of the desalting region.
  • a porous ion exchanger When a part of the liquid to be treated permeates, it is electrophoretically excluded. This is a region through which ionic impurities are transmitted.
  • the porous ion exchanger loaded in the liquid permeation region is particularly limited as long as it retains its shape, electrophoretically excludes ions, and allows a part of the liquid to be treated to permeate.
  • examples include monoliths, fibrous porous ion exchangers, and particle agglomerated porous ion exchangers. Of these, monoliths have a uniform distribution of ion exchange groups and prompt ion exclusion. Is preferable.
  • fibrous porous ion exchanger examples include, for example, single fibers and woven fabrics and non-woven fabrics that are aggregates of single fibers described in JP-A-5-64726, and radiation graft polymerization to these processed products. And an ion-exchange group introduced and processed and molded.
  • particle agglomerated porous ion exchanger examples include thermoplastic polymers and thermosetting resins described in, for example, JP-A Nos. 10-1 9 2 7 1 6 and 10-1 9 27 17.
  • Polymer mixing point Examples include those obtained by bonding ion-exchange resin particles using a remer or a crosslinkable polymer and then processing and molding.
  • the monolith loaded in the liquid permeation region is the same as the monolith exemplified as the ion exchanger in the desalination region, but no flow rate adjusting means is provided in the permeate flow path as will be described later.
  • the monolith has a smaller mesopore average diameter than the monolith used in the desalination zone. Specifically, the average diameter is 1 to 100 m, preferably 1 to 20 m, in the wall of the macropore and the mac mouth pore that are connected to each other.
  • a monolith having a small average mesopore diameter can be obtained by a method such as increasing the amount of the surfactant added or increasing the agitation during the production.
  • the flow rate adjusting means include a flow rate adjusting valve and an orifice.
  • an ion exchange membrane has been attached to the ion rejection side of the desalting zone.
  • the hardness component concentration in the treated water and the applied current density there is a problem of scale generation on the ion exchange membrane surface on the concentration chamber side. It was.
  • the liquid permeation region of the present invention a part of the liquid to be treated permeates, so that the dilution effect can prevent the generation of scale.
  • the liquid that has passed through the liquid-permeable region flows into the electrode chamber or the concentration chamber as it contains ionic impurities, it is not necessary to supply a separate electrode solution or concentrated solution.
  • the ion-exclusion side is the cathode side of the desalting region when removing the cationic impurities, and the anode side of the desalting region when removing the anionic impurities, and the cationic impurities and the anionic impurities are simultaneously removed. When removing, both the cathode side and the anode side.
  • the flow resistance of the porous ion exchanger loaded in the liquid permeation region is larger than the flow resistance of the ion exchanger charged in the desalting region, but without providing a separate special channel distribution means, This is preferable in that most of the liquid to be treated that has flowed into the desalting area flows out of the desalting area as a deionized liquid from the desalting area, and a part of the liquid to be treated permeates into the liquid permeation area. If flow rate adjusting means is provided in the flow path of the effluent permeated from the liquid permeation region, the flow rate of the permeated liquid and the deionized liquid can be adjusted to a desired ratio by the flow rate adjusting means.
  • the flow resistance of the porous ion exchanger loaded in the liquid permeation region is the same as that of the ion exchanger filled in the desalination region. It may be the same as the fluid flow resistance.
  • a monolith is used for both the desalting region and the liquid permeation region
  • a single monolith processed into a shape extending over the desalting region and the liquid permeation region can be used. This is advantageous in that it is not necessary to separately manufacture the desalination zone monolith and the liquid permeation zone monolith.
  • the flow rate ratio of the permeate passing through the liquid permeation region to the flow rate of the liquid to be treated is, for example, 2 to 30%, preferably 4 to 30%. If this ratio is less than 2%, the diluting effect is reduced and it becomes difficult to prevent the generation of scale, and if it exceeds 30%, it is not preferable because the yield of the desalted solution is reduced.
  • the form in which the liquid permeation region is disposed adjacent to the ion rejection side of the desalting region is not particularly limited, but the form in which the monoliths are disposed adjacent to each other is preferable in terms of quick ion exclusion. .
  • the monoliths are arranged adjacent to each other, the monolith for the arrangement desalting region and the monolith for the liquid permeation region are arranged in close contact with each other in the electric field application direction.
  • the monolith and the ion exchange resin are arranged adjacent to each other, or the mixture of the monolith and the ion exchange resin in the desalination region is a sponge, so the two phases do not mix and the phases are mixed. Can be formed Monkey.
  • the electric deionized liquid production apparatus of the present invention in the case of a gas-on cell or a cation cell, it is arranged adjacent to the side opposite to the ion exclusion side of the desalting region. It may be another liquid permeable region through which a part passes, or a conventional ion exchange membrane. When this liquid permeation region is provided, the liquid that has permeated from this liquid permeation region flows into the electrode chamber or the concentration chamber. This eliminates the need for an ion exchange membrane, thereby simplifying the device structure and reducing the manufacturing cost.
  • an electrode solution or a concentrate is separately supplied to the electrode chamber or the concentration chamber adjacent to the ion exchange membrane, as in the case of the conventional EDI.
  • the porous ion exchanger loaded in the other liquid permeable region include the same porous ion exchangers loaded in the liquid permeable region.
  • FIG. Fig. 1 shows a schematic diagram of a two-cell EDI that uses a cation cell ((A) in the figure) and an anion cell ((B)) to remove anionic impurities in the liquid to be treated.
  • FIG. 1 shows a schematic diagram of a two-cell EDI that uses a cation cell ((A) in the figure) and an anion cell ((B)) to remove anionic impurities in the liquid to be treated.
  • an electric deionized liquid production apparatus 10 is composed of a cation cell 10 a and an anion cell 10 b.
  • the cation cell 10 a is permeated through a weakened thione region 1 a filled with a cation exchanger and a part of the liquid to be treated arranged adjacent to the ion exclusion side (cathode side) of the weakened thione region 1 a.
  • An anode chamber 7 into which the permeated liquid flows and a weak thiol liquid outflow pipe 12 for discharging the weak thiol liquid from the weak thiol region 1a are provided.
  • the cation cell 10 a is a conventional cation cell in which the ion exchange membranes provided on both sides of the desalting chamber are omitted, and a liquid permeable region in which a cation monolith is loaded is attached to the ion exchange membrane part.
  • the cation cell 10 a can be formed from a member having a very simple structure in which the weak thione region 1 a, the liquid permeable region 2 a, the liquid permeable region 3 a, and the electrode can be disposed at predetermined positions.
  • the electrical deionized liquid production system can reduce the parts and assembly costs from this point as well as the possibility of leakage of the liquid to be processed by eliminating the joints, pipes and joints. In addition, the safety of the equipment and the stability of operation can be improved.
  • the flow resistance of the cation monolith forming the liquid permeation region 2 a and the liquid permeation region 3 a is larger than the flow resistance of the cation exchanger filled in the weak thione region 1 a. .
  • the liquid to be treated is allowed to flow from the vicinity of the cathode side of the weakened thione area 1a, and the liquid to be treated is allowed to flow out from the vicinity of the anode side of the weakened thione area 1a almost diagonally to the inlet of the liquid to be treated.
  • the difference between the anion cell 10 b and the cation cell 10 a is that the desalination area is filled with an anion exchanger, and the liquid permeation area 2 b and the liquid permeation area 3 b are filled with an anion monolith,
  • the liquid to be treated was introduced from the vicinity of the anode side of the deanion region 1b, and the treatment liquid was caused to flow out from the vicinity of the cathode side of the deanion region 1b on the diagonal line of the inlet of the liquid to be treated.
  • the weak thione liquid outlet pipe 12 of the cation cell 10a is connected to the liquid inlet pipe 13 to be treated of the anion cell 10b.
  • the anion cell 10 b has a very simple structure.
  • the liquid to be treated is caused to flow from the liquid inlet pipe 11 to the weakening thione region 1a.
  • the liquid to be treated which has flowed into the weak thione region 1a has a flow resistance of the cation monolith forming the liquid permeation region 2a and the liquid permeation region 3a. Since it is larger than the liquid resistance, most of the liquid to be treated flows through the weakened thione region 1a, and a part of it passes through the liquid permeable region 2a and the liquid permeable region 3a.
  • the permeate that has permeated the liquid permeation region 2a is discharged as a catholyte into the cathode chamber 6 together with the cationic impurities X + that are electrophoretically excluded.
  • the liquid permeation zone 2a a part of the liquid to be treated is always permeating, and scale generation is prevented by the dilution effect.
  • the permeated liquid that has passed through the liquid permeable region 3 a is discharged into the anode chamber 7 as an anolyte.
  • the flow path 17 in the weak force thione region 1a is schematically shown, but the actual flow is also generally similar to this.
  • the liquid to be processed from which the cationic impurities have been removed is caused to flow from the liquid inlet pipe 13 to the de-on region 1 b.
  • the liquid to be treated that has flowed into the deanion region 1 b forms a liquid permeable region 2 b and a liquid permeable region 3 b. Since the liquid flow resistance of the monolith is greater than the liquid flow resistance of the anion exchanger filled in the deionized area 1b, most of the liquid to be treated flows through the deanion area 1b, and part of the liquid is liquid. It passes through the permeation region 2b and the liquid permeation region 3b.
  • the permeated liquid that has passed through the liquid permeable region 2 b is discharged as an anolyte into the anode chamber 7 together with the anionic impurities Y— that are electrophoretically excluded.
  • the liquid permeation region 2b like the cation cell 10a, a part of the liquid to be treated is always permeated, and scale generation is prevented by the dilution effect.
  • the permeated liquid that has permeated through the liquid permeable region 3 b is discharged into the cathode chamber 6 as a catholyte.
  • the flow path 18 in the deanion region 1 b is schematically shown, but the actual flow is also generally similar to this.
  • both the cation cell 1 0 a and the anion cell 1 0 b use an ion exchange membrane at all. Therefore, the device structure can be greatly simplified and the manufacturing cost can be reduced.
  • the generation of scale that could not be avoided by conventional EDI is transmitted. This can be prevented by the dilution effect of the liquid to be treated.
  • FIG. Fig. 2 shows a cation cell 20 a (in the figure, (A)) that removes cationic impurities in the liquid to be treated and an anion cell 20 b (in the figure, (B)) that removes anionic impurities.
  • FIG. 2 shows a schematic diagram of another EDI of the 2-cell type used.
  • FIG. 2 the same components as those in FIG. 1 are denoted by the same reference numerals, description thereof is omitted, and different points are mainly described. That is, FIG. 2 differs from FIG.
  • cation cell 20 a has a cation exchange on the anode side of the weakened thione region 1 a.
  • Membrane 5 is provided to prevent liquid permeation between the weakened thione region 1a and the anode chamber 7.
  • a cation exchange membrane 5 is provided on the cathode side of the deanion region 1b. However, there is no permeation of liquid between the deanion region 1 b and the cathode chamber 6.
  • both the caton cell 20 a and the anion cell 20 b are compared with the conventional EDI. Since the ion exchange membrane can be halved, the device structure can be simplified and the manufacturing cost can be reduced. In addition, the liquid permeation region 2 a on the cathode side of the cathode cell 20 a and the liquid permeation region 2 b on the anode side of the anion cell 20 b transmit the generation of scales that could not be avoided by conventional EDI. This can be prevented by the dilution effect of the liquid to be treated.
  • anolyte of the cation cell 20a and the catholyte of the anion cell 20b are the permeate that has permeated from the permeation regions 2a and 2b, a separate liquid feed pump or the like can be omitted.
  • FIG. Fig. 3 is a schematic diagram of a single cell type EDI that simultaneously removes force thionic impurities and anionic impurities.
  • FIG. 3 the same components as those in FIG. 1 are denoted by the same reference numerals, description thereof is omitted, and differences are mainly described. That is, in FIG. 3, the difference from FIG. 1 is that the cell structure is a single-cell cation / anion cell 30. In the desalted region 1c, there are cation exchangers and anion exchangers.
  • the liquid permeation region 2 a on the cathode side of the desalination region 1 c is loaded with a cation monolith, and the liquid permeation region 3 b on the anode side of the desalination region 1 c It is in the point where the anion monolith was loaded.
  • Processed liquid inflow pipe 1 1 Processed into the desalting zone 1 c through the process 1 Since the liquid resistance of the cation monolith and the anion monolith forming the liquid permeation region 2 a and the liquid permeation region 3 b is larger than that of the mixed ion exchanger filled in the desalting region 1 c, Most of the liquid to be treated flows through the desalting region 1c, and part of the solution passes through the liquid permeation region 2a and the liquid permeation region 3b.
  • the permeate that has permeated the liquid permeation region 2a is discharged as a catholyte into the cathode chamber 6 together with the cationic impurities X + that are electrophoretically excluded. Further, the permeated liquid that has permeated through the liquid permeable region 3 b is discharged into the anode chamber 7 as an anolyte.
  • the flow path 17 in the desalination zone 1 c is schematically shown. The actual flow is also almost the same as this.
  • the ion exchange membrane can be omitted as compared with the conventional EDI, so that the structure of the apparatus can be simplified and the production cost can be reduced. Further, in the liquid permeation region 2 a on the cathode side and the liquid permeation region 3 b on the anode side of the cation / anion cell 30 , the generation of scale, which could not be avoided by conventional EDI, is reduced. This can be prevented by the dilution effect.
  • FIG. 4 is a schematic diagram of EDI in which a plurality of desalting chambers for removing cationic impurities and anionic impurities simultaneously are arranged in parallel.
  • FIG. 4 the same components as those in FIG. 1 are denoted by the same reference numerals, description thereof is omitted, and different points are mainly described. That is, FIG. 4 differs from FIG. 1 in that the basic structure of the desalting cell disposed between the electrodes is different.
  • the number of demineralization chambers ld and Id is not limited to this, and may be one or three or more.
  • the liquid to be treated is caused to flow into the desalting areas 1 d and 1 d from the liquid to be treated inflow pipe 1 1.
  • the liquid to be treated that has flowed into the desalting areas 1 d and 1 d is filled with the resistance of the monolith that forms the liquid permeation area 2 a and the liquid permeation area 2 b into the desalination areas 1 d and 1 d.
  • the permeated liquid that has permeated through the liquid permeable region 2 b is discharged into the anode chamber 7 and the concentrating chamber 9 as the anolyte and concentrated liquid together with the anionic impurities Y that are electrophoretically excluded.
  • the liquid permeation region 2a and the liquid permeation region 2b a part of the liquid to be treated is always permeating, and scale generation is prevented by the dilution effect.
  • the flow path 17 in the desalination region 1 d is schematically shown in the figure. The actual flow is almost the same as this.
  • the electric deionization liquid production equipment 40 in parallel with the desalination chamber all four ion exchange membranes used in the conventional EDI can be omitted, so the equipment structure can be simplified and manufactured. Cost can also be reduced.
  • the liquid permeation area 2 a on the cathode side and the liquid permeation area 2 b on the anode side allow the generation of scale that could not be avoided by conventional EDI to be treated. This can be prevented by the dilution effect.
  • the gas was sufficiently substituted with nitrogen, sealed, and allowed to stand for polymerization at 60 ° C for 24 hours.
  • the contents were taken out and Soxhlet extracted with isopropanol for 12 hours to remove unreacted monomers and sorbitan monoleate. Thereafter, it was dried under reduced pressure at 85 ° C. for a whole day and night.
  • the porous body containing 3.3 mol% of the cross-linking component made of styrene / divinylbenzene copolymer was cut and 7.9 g was sampled, and 90 ml of dichloromethane was added.
  • the internal structure of this porous body had an open-cell structure, and most of the macropores with an average diameter of 30 m overlapped.
  • the average diameter of the mesopore formed by the overlap of the mac mouth pore and the mac mouth pore was determined by the mercury intrusion method, and the mean diameter was 7.8 ⁇ m and the total pore volume was 4. Oml / g. Met.
  • P-Chloromethylstyrene 19.2 instead of styrene 19.2g g was mixed with 1.0 g of dibutenebenzene, 0.3 g of azobisoxy mouth-tolyl and 2.0 g of sorbitan monoleate, and dissolved uniformly.
  • Add the p-chloromethylstyrene / dibutenebenzene / azobisi soptite-tolyl Z sorbitan monooleate mixture to 180 ml pure water (revolution / spinning) using a planetary stirrer (, 1 00 rpm / 3 30 rpm) for 2 minutes to obtain a water-in-oil emulsion.
  • the gas was sufficiently substituted with nitrogen, sealed, and allowed to stand for polymerization at 60 ° C for 24 hours. After the completion of the polymerization, the contents were taken out and extracted with Sopropanol for 12 hours to remove unreacted monomers and sorbitan monoleate. Thereafter, it was dried under reduced pressure at 85 ° C. for a whole day and night. 6.8 g of a porous material containing 5.0 mol% of a cross-linking component composed of p-chloromethylstyrene Z divinylbenzene copolymer obtained in this manner was cut and collected, and 900 g of tetrahydrofuran was collected.
  • a cation cell 20a as shown in FIG. 5 was first produced. Obtained liquid permeability From the cation monolith for the excess region and the cation monolith for the weak force thione region, in the pure water wet state, the length (H) 50 mm, width (W) 4 Omm, thickness (L 20 mm, two rectangular parallelepiped 2 a, 1 1 a was cut out to obtain a filler that was stacked and filled in the weak thione chamber, and then in the cell container 2 0 1, in order from the cathode chamber (left side in the figure), the cation monolith for liquid permeation region 2 a and Cationic monolith for weakness cation region 1 1 a is closely packed, and cation monolith for weakness thione region 1 1 a is placed in the adjacent space on the anode side of cation exchange resin 1 2 a (Amberlite IR 1 20 B, Rohm and (Ma)
  • the cell container 20 1 has a cation monolith for weakening thione region 1 1 in the figure.
  • Treatment resin outflow pipe 1 2 is placed on the anode side upper surface where exchange resin 1 2 a is located
  • a cathode chamber was formed on the cathode side of the cell container 20 1, and a cathode made of SUS 3 04 was disposed on the outer surface of the cathode chamber, and the cation exchange resin 1 2 a
  • a cation exchange membrane Nafion 350; manufactured by DuPont
  • An anode made of a platinum-coated titanium substrate is placed on the outer surface of the cation exchange membrane.
  • a cation cell 20 a was prepared by providing a take-out port, for the sake of simplicity, the description of the cation exchange membrane, the electrode chamber, and the electrode was omitted in FIG.
  • each of the two rectangular parallelepipeds 2 (H) 5 Omm, width (W) 40 mm, thickness (Lj 20 mm) 2 b and lib were cut out to obtain a filler to be stacked and filled in the deanion chamber, and then into the cell container 20 2, in order from the anode chamber (left side in FIG. 5), the anion monolith for liquid permeation region 2 b and the union monolith for the union region 1 1 b are intimately packed and placed in the adjacent space on the cathode side of the union region monolith for the deanion region 1 1 b.
  • Anion exchange resin 1 2 b (Amberlite IRA 40 2 BL, manufactured by Romand Haas) 80 ml volume was filled.
  • the cell container 20 2 is provided with an inflow pipe 13 for the liquid to be treated (depressurized thione liquid) on the bottom surface where the union area monolith for deanion area 1 1 b is located, and the anion replacement resin 1 2 b is A desalting solution outflow pipe 14 is attached to the upper surface on the cathode side.
  • an anode chamber was formed on the anode side of the cell container 202, and an anode made of a platinum-coated titanium substrate was further arranged on the outer surface of the anode chamber.
  • a cation exchange membrane (Naf ion 350; manufactured by DuPont) is placed in close contact with the cathode side of the anion exchange resin 12 b, and the outer surface of the cation exchange membrane is made of SUS 304.
  • An anion cell 20 b was prepared by disposing a cathode and appropriately providing a nozzle and a lead wire outlet.
  • the resulting cation cell 20 a treated liquid outflow pipe 12 is connected to the gas-on cell 20 b treated liquid inflow pipe 13, and the two electrode chambers are permeated through the other two electrode chambers. A part of the liquid was supplied.
  • the obtained electric deionized liquid production apparatus 20 was continuously supplied at a flow rate of 15 1 / h with water having a conductivity of 1305 to 111 as a liquid to be treated, and a DC current of 2.5 A was applied.
  • a current was applied in series from the thione cell to the anion cell, an operating voltage was 110 V and a treatment liquid having an electrical conductivity of 1 / i S / cm was obtained at a flow rate of 10 / h.
  • the flow rate of the permeate (catholyte) permeated through the force thione cell 20a and the flow rate of the permeate (anolyte) permeated through the gas cell 2Ob were 2.5 1 / h, respectively. .
  • Example 2 Cation and anion using a monolith prepared in the same manner as in Example 1.
  • a simultaneous processing type cell was produced.
  • the liquid permeation region cation monolith and the liquid permeation region anion monolith and the weak force thione region catholyte obtained in Example 1 were used. Cut out a rectangular parallelepiped of length (H) 50 mm, width (W) 40 mm, and thickness (L j 20 mm) in pure water wet state from the union monolith and the union monolith for the weakness thione region.
  • a flow rate adjusting valve 15 was attached to the flow path of the effluent that flowed out, and then a cathode chamber was formed on the cathode side of the cell container 20 3, and a SUS cathode was further arranged on the outer surface of the cathode chamber.
  • an anode chamber is formed on the anode side, and an anode of a platinum-coated titanium substrate is arranged on the outer surface of the anode chamber, and an appropriate nozzle or lead wire outlet is provided to provide an electrical deionized liquid production apparatus.
  • 30 a was prepared Note that, for the sake of simplicity, the description of the electrode chamber and the electrode was omitted in FIG.
  • the apparatus structure can be further simplified than the conventional one, and the generation of scale can be prevented and the method for producing the deionized liquid can be prevented. Can be provided.

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Abstract

L’invention concerne un appareil électrique de production de liquide désionisé, comprenant au moins une région de désalinisation (1c) remplie d’un échangeur d’ions ; des régions de perméation de liquide (2a,3b) placées de manière adjacente aux côtés d’élimination des ions de la région d’élimination des sels (1c) et conçues pour être traversées par une fraction d’un liquide à traiter ; des électrodes (4a,4b) placées des deux côtés des régions de perméation des liquides et de la région de désalinisation (1c) ; un tube d’entrée (11) du liquide à traiter permettant d’introduire du liquide à traiter ; des chambres à électrodes (6,7) conçues pour décharger tout liquide ayant traversé les régions de perméation des liquides (2a,3b) ; et un tube de sortie (14) du liquide débarrassé de ses sels, destiné à évacuer un liquide désalinisé de la région de désalinisation (1c), les régions de perméation des liquides (2a,3b) étant remplies d’un échangeur d’ions poreux. Il est ainsi possible d’obtenir un appareil électrique de production de liquide désionisé qui, ne comportant aucune membrane échangeuse d’ions, simplifie la structure traditionnelle de l’appareil et empêche la survenue de tartre ; et d’obtenir un procédé correspondant de production d’un liquide désionisé.
PCT/JP2005/022600 2004-12-06 2005-12-02 Appareil electrique de production de liquide desionise et procede de production de liquide desionise WO2006062176A1 (fr)

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JP2004352532A JP4721323B2 (ja) 2004-12-06 2004-12-06 電気式脱イオン液製造装置及び脱イオン液の製造方法
JP2004-352532 2004-12-06

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EP2208523A1 (fr) 2008-12-31 2010-07-21 Millipore Corporation Procédé d'électro-désionisation et dispositif avec séparation de flux hydrodinamique
WO2012082239A1 (fr) * 2010-12-14 2012-06-21 General Electric Company Appareil de désionisation par échange d'ions présentant une régénération électrique
KR20140074896A (ko) * 2011-09-16 2014-06-18 제너럴 일렉트릭 캄파니 스케일링 물질을 부동태화시키기 위한 전기 투석 방법 및 장치

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JP5019470B2 (ja) * 2007-06-12 2012-09-05 オルガノ株式会社 モノリス状有機多孔質体、その製造方法、モノリス状有機多孔質イオン交換体及びケミカルフィルター
JP5383310B2 (ja) * 2009-05-13 2014-01-08 オルガノ株式会社 脱イオンモジュール及び電気式脱イオン水製造装置
WO2010104007A1 (fr) * 2009-03-10 2010-09-16 オルガノ株式会社 Module de déionisation et dispositif électrique pour la production d'eau déionisée
JP5431197B2 (ja) * 2009-03-18 2014-03-05 オルガノ株式会社 電気式脱イオン液製造装置
JP5048712B2 (ja) * 2009-05-13 2012-10-17 オルガノ株式会社 電気式脱イオン水製造装置
JP5030181B2 (ja) * 2009-05-13 2012-09-19 オルガノ株式会社 電気式脱イオン水製造装置
JP5030182B2 (ja) * 2009-05-14 2012-09-19 オルガノ株式会社 電気式脱イオン液製造装置

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JP2002001345A (ja) * 2000-06-19 2002-01-08 Asahi Glass Co Ltd 電気再生式脱イオン水の製造方法、その製造装置及びそれらに使用するイオン交換体層
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EP2208523A1 (fr) 2008-12-31 2010-07-21 Millipore Corporation Procédé d'électro-désionisation et dispositif avec séparation de flux hydrodinamique
US8313630B2 (en) 2008-12-31 2012-11-20 Emd Millipore Corporation Electrodeionization device with hydrodynamic flow splitting
CN101898090B (zh) * 2008-12-31 2013-03-20 Emd密理博公司 采用流体动力学流体分离的电去离子方法和装置
US8652315B2 (en) 2008-12-31 2014-02-18 Emd Millipore Corporation Electrodeionization method and device with hydrodynamic flow splitting
WO2012082239A1 (fr) * 2010-12-14 2012-06-21 General Electric Company Appareil de désionisation par échange d'ions présentant une régénération électrique
US8496797B2 (en) 2010-12-14 2013-07-30 General Electric Company Electrical deionization apparatus
CN103249485A (zh) * 2010-12-14 2013-08-14 通用电气公司 带有电再生的离子交换去离子设备
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KR101838770B1 (ko) 2010-12-14 2018-03-14 제너럴 일렉트릭 캄파니 전기적 재생과 함께 이온 교환 탈이온화를 수행하는 장치
KR20140074896A (ko) * 2011-09-16 2014-06-18 제너럴 일렉트릭 캄파니 스케일링 물질을 부동태화시키기 위한 전기 투석 방법 및 장치
KR101892787B1 (ko) 2011-09-16 2018-08-28 제너럴 일렉트릭 캄파니 스케일링 물질을 부동태화시키기 위한 전기 투석 방법 및 장치

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