WO1997046491A1 - Procede de production d'eau deionisee par une technique de deionisation electrique - Google Patents

Procede de production d'eau deionisee par une technique de deionisation electrique Download PDF

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Publication number
WO1997046491A1
WO1997046491A1 PCT/JP1996/001517 JP9601517W WO9746491A1 WO 1997046491 A1 WO1997046491 A1 WO 1997046491A1 JP 9601517 W JP9601517 W JP 9601517W WO 9746491 A1 WO9746491 A1 WO 9746491A1
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WO
WIPO (PCT)
Prior art keywords
water
chamber
treated
concentration
deionized water
Prior art date
Application number
PCT/JP1996/001517
Other languages
English (en)
Japanese (ja)
Inventor
Yasutaka Shinmei
Koichi Hosoda
Makio Tamura
Katsumi Okugawa
Original Assignee
Organo Corporation
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority to JP31921894A priority Critical patent/JP3305139B2/ja
Priority claimed from JP31921894A external-priority patent/JP3305139B2/ja
Application filed by Organo Corporation filed Critical Organo Corporation
Priority to PCT/JP1996/001517 priority patent/WO1997046491A1/fr
Publication of WO1997046491A1 publication Critical patent/WO1997046491A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
    • B01D61/44—Ion-selective electrodialysis
    • B01D61/46—Apparatus therefor
    • B01D61/48—Apparatus therefor having one or more compartments filled with ion-exchange material, e.g. electrodeionisation
    • 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
    • C02F1/4604—Treatment of water, waste water, or sewage by electrochemical methods for desalination of seawater or brackish water
    • 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
    • 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 relates to a deionized water production method for efficiently producing deionized water used in various industries such as a semiconductor manufacturing industry, a pharmaceutical industry, and a food industry, or a research facility, by an electrodeionization method.
  • a deionization chamber is formed by filling an ion exchange resin between a cation exchange membrane and an anion exchange membrane, and a concentration chamber is provided on both outer sides of the deionization chamber.
  • the chamber and the concentrator are placed between the positive and negative electrodes, and the water to be treated flows into the desalination chamber and the concentrated water flows into the concentrator while voltage is applied.
  • the impurity ion is electrically suctioned and moved to a concentration chamber to produce deionized water.
  • the ion exchange resin is not saturated with ions, so that the drug is not saturated. Has the advantage of not requiring regeneration, but on the other hand, since a high voltage is applied, there is the problem of increased production costs in terms of power consumption, and how to reduce power consumption Is an important issue.
  • the desalting chamber is filled with an ion exchanger, and since this ion exchanger functions as a kind of conductor, the conductivity of the enrichment chamber is important from the viewpoint of improving the conductivity. It becomes a factor, and it is necessary to increase the conductivity of the enrichment chamber in order to reduce the applied voltage and solve the problems.
  • the first approach is to reduce the flow rate of the concentrate.
  • the practical flow ratio of treated water and concentrated water is 3: 1 to 5 : 1, and as a result, the treated water becomes pure water.
  • the concentration of impurity ions in the concentrated water was 4 to 6 times. Therefore, the first attempt is to increase the concentration ratio by reducing the flow rate of the concentrated water, thereby increasing the electrical conductivity, and thereby reducing the applied voltage.
  • the second approach is to increase the ion concentration of the concentrated water by circulating and reusing the concentrated water, thereby increasing the conductivity.
  • This method requires a tank for temporarily storing the concentrated water and a pump for sending and circulating the concentrated water from the tank, which has the disadvantage that the equipment becomes large and the operation management becomes complicated.
  • the third attempt is to increase the conductivity by adding chemicals such as salts and acids to the concentrated water, but new equipment must be provided to supply the chemicals, and the equipment is also large. And operation management becomes complicated.
  • the fourth attempt is to increase the conductivity by filling the concentration chamber with ion-exchange resin, or it is difficult to fill with ion-exchange resin due to the small thickness of the concentration chamber, and the feasibility is poor. . If this were to be achieved, the thickness of the enrichment chamber would need to be increased, resulting in a problem that the equipment would become larger.
  • the present inventors have conducted intensive studies to solve the above-mentioned problems, and as a result, the ions moving to the concentration chamber by increasing the flow ratio and the linear velocity of the water to be treated and the concentrated water as compared with the conventional case. And increased the conductivity of the enrichment chamber.
  • the flow ratio and the linear velocity of the water to be treated and the concentrated water are also factors related to the quality of the treated water, and if these values are too large, the quality of the treated water may be reduced. Therefore, the present inventors have further studied in consideration of this point, and as a result, regarding the flow ratio of the treated water and the concentrated water, the flow ratio of the treated water to the concentrated water is 6: 1 to 12: 1.
  • the present invention enhances the conductivity of the concentrating chamber to improve the current efficiency, thereby realizing a reduction in the applied voltage. It is intended to provide. Disclosure of the invention
  • a desalting chamber is formed by filling an ion exchanger between a cation exchange membrane and an anion exchange membrane, and concentration chambers are provided on both sides of the desalination chamber via the cation exchange membrane and the anion exchange membrane.
  • the desalination chamber and the concentration chamber are placed between the anode and the cathode,
  • the water to be treated flows into the deionization chamber while applying pressure, and the concentrated water flows into the concentration chamber to remove impurity ions in the water to be treated.
  • the treated water and the concentrated water are desalted in a desalting chamber, respectively, so that the flow rate ratio of the treated water and the concentrated water is 6: 1 to 12: 1 and the linear velocity of the treated water and the concentrated water is 75 to 15 Om / hr. It is designed to flow into the concentration chamber.
  • the thickness of the desalting chamber is preferably set to 7-1 O mm, and the thickness of the concentrating chamber is preferably set to 0.5 to 2 mm. .
  • the water to be treated and the concentrated water flow into the desalting chamber and the concentrating chamber at a specific flow ratio and linear velocity, respectively, so that the impurity ions removed in the desalting chamber move to the enriching chamber.
  • the conductivity of the concentration chamber is increased, and the electric resistance of the entire apparatus can be reduced.
  • the water to be treated is supplied at a larger flow rate ratio than before, the amount of deionized water produced by the same-scale apparatus increases, and as a result, the apparatus does not need to be enlarged. There is an effect that a larger amount of processing can be performed than before.
  • FIG. 1 is a schematic longitudinal sectional view showing an example of an electric deionized water producing apparatus used for carrying out the method of the present invention.
  • the present invention is to produce deionized water by an electric deionization method.
  • desalination is performed by filling an ion exchanger between a cation exchange membrane and an anion exchange membrane.
  • the cation exchange membrane and the anion exchange membrane An electric deionized water production device including a concentration chamber provided on both sides of the desalting chamber and an anode and a cathode disposed on both outer sides of the chamber is used.
  • FIG. 1 One configuration example of such an electric deionized water producing apparatus is shown in FIG.
  • the present invention will be described in detail by taking as an example the case of producing deionized water using the apparatus shown in FIG.
  • the desalination chamber 1 is manufactured as one module product. That is, a cation exchange membrane 4 and an anion exchange membrane 5 are respectively adhered to both sides of a frame 3 made of, for example, a synthetic resin formed in a four-circle frame shape, and an ion exchanger such as an ion exchange resin 6 (cation exchange).
  • the deionization module 7 is manufactured by filling resin and anion exchange resin), and the ion exchange resin filling portion in the deionization module 7 is configured as a desalination chamber 1.
  • a plurality of the above-mentioned deion modules 7 are arranged in parallel at a distance.
  • a spacer 8 made of a water-tight member such as a rubber packing formed in a four-circle frame is interposed between the deionization modules 7 and 7, and the space thus formed is referred to as a concentration chamber 2.
  • a flow path forming material such as an ion exchange fiber or a synthetic resin net is usually provided in the internal space of the concentration chamber 2. Is satisfied.
  • An anode 9 and a cathode 10 were arranged on both sides of the alternately arranged body of the desalting chamber 1 and the concentration chamber 2 as described above, and although not shown, partition membranes were provided near the anode 9 and the cathode 10, respectively.
  • the space between the partition membrane and the anode 9 is configured as an anode chamber 11, and the space between the partition membrane and the cathode 10 is configured as a cathode chamber 12.
  • 13 is the treated water inflow line
  • 14 is the deionized water outflow line
  • 15 is the concentrated water inflow line
  • 16 is the concentrated water outflow line
  • 17 is the electrode water inflow line
  • 18 is the electrode water Outflow line.
  • the water to be treated flows into the desalination chamber 1 from the water inflow line 13 to be treated
  • the concentrated water flows into the desalination chamber 1 from the concentrated water inflow line 15.
  • Electrode water flows into the concentration chamber 2 and flows into the anode chamber 11 and the cathode chamber 12 through the electrode water inflow lines 17 and 17, respectively.
  • the concentrated water the same water as the water to be supplied to the desalination chamber 1 is usually supplied.
  • a voltage is applied between the anode 9 and the cathode 10, and a direct current flows in a direction perpendicular to the flow direction of the water to be treated and the concentrated water.
  • the flow rate of the to-be-treated water in the desalination chamber 1 needs to be larger than the flow rate of the concentrated water in the concentrating chamber 2.
  • the flow ratio of the to-be-treated water to the concentrated water is 6: 1 to 12: 1.
  • the flow rate ratio of the water to be treated and the concentrated water is generally 3: 1 to 5: 1, and the flow rate of the water to be treated in the present invention is greatly increased in comparison with the conventional flow rate ratio.
  • the flow ratio is set to 6: 1 to 12: 1 because the ion concentration of the concentrated water in the concentration chamber 2 can be sufficiently increased if the flow rate of the water to be treated is less than 6 times the flow rate of the concentrated water. Therefore, if the flow rate of the water to be treated exceeds 12 times the flow rate of the concentrated water, the efficiency of deionization is reduced and the quality of the deionized water is reduced. This is because there is a risk of lowering.
  • the present invention does not suffice if the flow rate ratio satisfies the condition of 6: 1 to 12: 1. Even if the water to be treated flows into the desalination chamber 1 within the above flow rate ratio, if the flow rate in the desalination chamber 1 is too slow, the same amount of It is necessary to increase the thickness to increase the cross-sectional area of water in the desalination chamber 1. However, if the thickness of the desalination chamber 1 is too large, it is not preferable because the current efficiency deteriorates. Therefore, in the present invention, the treatment flowing in the B salt chamber 1
  • the linear velocity of the water is an important factor together with the flow ratio. In the present invention, the linear velocity of the water to be treated in the desalting chamber 1 is set to 75 to 15 Om / hr, preferably 90 to 12 Om / hr.
  • the linear velocity is set to 75 to 15 OmZhr, as described above, when the linear velocity is less than 75 mZhr, when the same amount of demineralized water is to be obtained, the thickness of the desalination chamber 1 is increased. The current efficiency becomes worse,
  • the pressure loss in the desalting chamber 1 will be too large, which is not preferable, and the time during which the water to be treated is in contact with the ion exchange resin will be short, and the deionization efficiency will be reduced. This is because there is a possibility that the quality of deionized water will be reduced.
  • the thickness of the desalination chamber 1 required to obtain the same amount of desalinated water decreases as the numerical value increases.
  • a higher linear velocity is preferable, or the upper limit of the linear velocity is 15 Om / hr in order to perform treatment without lowering the quality of deionized water.
  • the linear velocity of the concentrated water in the concentration chamber 2 is also set to 75 to 15 OmZhr. Although this numerical range is the same as the linear velocity of the water to be treated, both need not necessarily have the same numerical value.
  • a preferred range for the linear velocity of the retentate is 75-0 OmZhr.
  • the linear velocity of the concentrated water is less than 75 m / hr, sufficient turbulence cannot be generated in the concentrated water flowing through the concentration chamber 2.
  • a concentration gradient of ions moving from the desalting chamber occurs, and cations such as Na ions, Ca ions, and Mg ions are distributed most in the vicinity of the anion exchange membrane 5 and C 1 ions Such anions are distributed most in the vicinity of the cation exchange membrane 4. Therefore, in the case of a hardness component such as Ca ion and Mg ion, there is a possibility that a phenomenon called scale precipitation may occur in the enrichment chamber. In order to prevent such scale deposition and obtain a uniform ion concentration, it is necessary to generate sufficient turbulence in the concentrated water. In order to achieve this, the linear velocity must be 75 m / hr or more.
  • the water to be treated and the condensed water are supplied to the desalting chamber 1 and the condensing chamber 2 under the above conditions.
  • the treated water flowing from the treated water inflow line 13 flows down the desalination chamber 1 in a downward flow, and when passing through the packed bed of the ion exchange resin 6, impurity ions are removed.
  • This deionized water flows out of the deionized water outflow line 14.
  • the concentrated water flowing from the concentrated water inflow line 15 flows into the concentration chamber 2 in the upward flow and rises.
  • the impurity ions in the water to be treated removed in the desalting chamber 1 are electrically attracted and move to the concentration chamber 2 through the cation exchange membrane 4 or the anion exchange membrane 5. That is, cations such as Na ions among the impurity ions are attracted to the cathode 10 side, move to the concentration chamber 2 through the cation exchange membrane 4, and anions such as C 1 ions are attracted to the anode 9 side, It moves to the concentration chamber 2 through the anion exchange membrane 5.
  • the concentrated water flowing through the concentration chamber 2 receives the moving impurity ions and flows out of the concentrated water outflow line 16 as concentrated water in which the impurity ions are concentrated. Electrode water flowing into the anode chamber 11 and the cathode chamber 12 from the electrode water inflow line 17 flows out from the electrode water outflow line 18.
  • the present invention supplies the water to be treated and the concentrated water so that the flow ratio between the flow rate of the water to be treated in the desalting chamber and the flow rate of the concentrated water in the concentration chamber becomes 6: 1 to 12: 1.
  • the water to be treated and the concentrated water are supplied so that the linear velocity becomes 75 to 15 O m / hr.
  • the amount of transfer is dramatically increased, thereby increasing the ion concentration of the concentrated water in the concentration chamber.
  • the electric resistance of the concentration chamber 2 is reduced, and the conductivity is increased.
  • the ion enrichment ratio of concentrated water is 4 to 6 if the treated water is deionized to pure water.
  • the flow rate ratio of 6 1 to 1 2 1 in the present invention what is the ion enrichment factor? ⁇ 13 times.
  • the value obtained by multiplying the conductivity of the concentrated water when supplied to the concentration chamber by the above-mentioned ion concentration magnification is substantially the conductivity of the concentrated water near the outlet of the concentration chamber. Is the conductivity of the water the conductivity of the condensed water at the time of supply? Means ⁇ 13 times.
  • the thickness of the desalting chamber 1 refers to the distance in the direction in which the cation exchange membrane 4 and the anion exchange membrane 5 face each other): t
  • the thickness of the concentration chamber 2 meaning the distance in the direction in which the cation exchange membrane 4 and the anion exchange membrane 5 face each other: t 2 is preferably 0.5 to 2 mm.
  • the deionization chamber 1 is formed by using the deionization module 7, or the method of forming the deionization chamber 1 is not limited to this, and other means may be used.
  • the apparatus shown in FIG. 1 employs a direction in which the flow direction of the water to be treated into the desalting chamber 1 and the direction of the inflow of the concentrated water into the concentration chamber 2 are opposite to each other, that is, a countercurrent type.
  • the inflow directions may be opposite to each other (countercurrent type) or may be the same direction (cocurrent type).
  • countercurrent type a direction in which the flow direction of the water to be treated into the desalting chamber 1 and the direction of the inflow of the concentrated water into the concentration chamber 2 are opposite to each other
  • cocurrent type there are the following advantages.
  • the ion concentration of the water to be treated in the desalination chamber 1 is highest near the inlet of the desalination chamber, that is, at the upper part of the desalination chamber, and decreases as it goes down.
  • the ion concentration of the concentrated water in the concentration chamber 2 is highest near the outlet of the concentration chamber, that is, in the upper part of the concentration chamber, and decreases as it goes downward.
  • the tendency of the concentration distribution between the desalting chamber 1 and the concentrating chamber 2 is consistent, and the upper part of the desalting chamber 1 and the concentrating chamber 2 In both cases, the ion concentration is the highest, and if deionization is performed at the high ion concentration, the deionization efficiency is improved and the quality of the treated water is remarkably improved. As a result, even if the flow rate of the water to be treated is increased, the impurity ions can be removed more sufficiently than in the case of the co-current type. In view of this, the counter-current type is preferred in the present invention.
  • the ion concentration of the concentrated water is the lowest near the inlet of the concentrating chamber 2 (for example, in the upper part of the concentrating chamber in Fig. 1), and becomes higher near the outlet (for example, in the lower part of the condensing chamber in Fig. 1). . Therefore, in this case, the tendency of the concentration distribution in the desalting chamber 1 and the concentrating chamber 2 is exactly opposite, and the difference in ion concentration between the desalting chamber and the concentrating chamber becomes large, and the lower part of the concentrating chamber with a high ion concentration is However, there is a risk that ions may leak to the lower part of the desalting chamber having a low ion concentration. Leakage of ions must be avoided because it causes contamination of the treated water.
  • the desalting chamber 1 is filled with a cation exchange resin and an anion exchange resin, and that the water to be treated first passes through the anion exchange resin layer. Therefore, when the water to be treated flows in a downward flow as shown in FIG. 1, it is preferable that the anion exchange resin is filled in the upper part of the desalting chamber 1 and the cation exchange resin is filled in the lower part thereof ( Of course, in the case of upward flow, the order is reversed.)
  • the layer configuration of the anion exchange resin layer and the cation exchange resin layer may be two or three or more.o
  • the upper part of the desalting chamber 1 is an anion exchange resin layer
  • the lower part is a cation exchange resin layer.
  • One or more sets of this laminated part are provided repeatedly, and a mixed ion-exchange resin layer is further provided at the lower part.
  • the on-exchange resin layer is composed of two layers.
  • weak acid components contained as impurities in the water to be treated have a low degree of dissociation and are difficult to remove.
  • carbonate ions have a low degree of dissociation of carbon dioxide in water, contain a lot of free carbonic acid, and silicate ions have a very low degree of dissociation of silica, and the removal rate of both is quite low at present.
  • the removal rate of such a weak acid component can be improved. This is because when the water to be treated first comes into contact with the anion exchange resin, only the anion among the impurity ions is mainly deionized, and only the anion moves to the concentration chamber.
  • the degree of dissociation of the weak acid component is improved, the amount of the weak acid ions transferred to the concentration chamber is large, and the removal rate can be improved.
  • the water to be treated is caused to flow at a high flow ratio to increase the amount of impurity ions transferred to the enrichment chamber, so that the water to be treated is supplied first so as to pass through the anion exchange resin layer.
  • the amount of ions transferred as impurity ions increases, thereby increasing the alkalinity of the water to be treated, and has the advantage that the efficiency of removing weak acid components can be improved as compared with the conventional method.
  • the water to be treated must Most preferably, the mixture passes through the on-exchange resin layer, and then passes through the ion-exchange resin layer, which is a mixture of the cation exchange resin and the anion exchange resin. According to such a method, the removal rate of the weak acid component is further improved. Can be.
  • the mixed ion-exchange resin layer has a higher electric resistance than the anion-exchange resin layer, so that more current flows through the anion-exchange resin layer, and the ion ions are removed as impurity ions and the anion is removed. It seems that this is based on the fact that the transfer to the enrichment room proceeds efficiently.
  • the present invention provides a dividing bar in the frame 3 to provide a plurality of desalination chambers 1. It can also be split.
  • an MR type or MP type (macroporous type) ion exchange resin having a giant network structure is preferable to use as the ion exchange resin.
  • the resin is excellent in physical strength and has an advantage that bead crushing can be prevented.
  • the frame 3 constituting the desalting chamber is provided with a deionized water outlet, and when a dividing bar is provided to divide the desalting chamber into two upper and lower rooms, for example, There is a passage for treated water, and a sarannet is usually attached to these outlets and passages to prevent resin particles of the ion exchange resin from passing through.
  • a sarannet is usually attached to these outlets and passages to prevent resin particles of the ion exchange resin from passing through.
  • the present invention can address this problem by using an ion-exchange resin having a huge network structure such as the MR-type ion-exchange resin described above, but the present invention further provides the above-mentioned treated water passage in a desalination chamber.
  • Comb with a slit gap that allows ion-exchange resin particles not to pass but crushed beads to pass through the deionized water outlet It is preferable to configure as a screen.
  • both the water to be treated and the concentrated water flowed in a downward flow (that is, in parallel flow).
  • the conditions of the flow ratio of the treated water and the concentrated water, the linear velocity of the treated water and the concentrated water, and the flow rate of the obtained deionized water are as shown in Table 2.
  • those thickness t of deionized module desalting compartment used, but 8 mm, thickness t 2 of the concentrating compartment is 0. 8 mm, also in the desalting compartment of a mixture of cation exchange resin and Anion exchange resin was filled with a height of 600 mm throughout the desalting chamber.
  • the applied voltage and DC current values are as shown in Table 3.
  • the applied voltage is an applied voltage necessary for obtaining deionized water having good water quality, having a deionized water resistivity of 10 ⁇ ⁇ cm or more.
  • the conductivity of the concentrated water at the concentrated water outlet was measured, and the presence or absence of scale formation of the hardness component after continuous operation for 1000 hours was observed. Conclusion The results are shown in Table 3.
  • the present invention is a comparative example, which is a conventional example, and has a device scale of 1/2 of that of Comparative Example 2, and is lower than Comparative Example 1 and Comparative Example 2; Deionized water having substantially the same amount and the same water quality as Comparative Example 2 can be obtained. Moreover, it can be seen that the scale formation of the hardness component does not occur despite the high conductivity of the concentrated water (that is, the high ion concentration of the concentrated water).
  • the present invention is useful as a deionized water production method for efficiently producing deionized water used in various industries such as the semiconductor manufacturing industry, the pharmaceutical industry, the food industry, and the like, research facilities, and the like by an electrodeionization method. .

Abstract

Les procédés classiques de production d'eau déionisée par une technique de déionisation électrique à l'aide d'un appareil de déionisation électrique pourvu de chambres de dessalement et de chambres de concentration agencées alternativement posent des problèmes car ils consomment beaucoup d'énergie, bien qu'ils soient avantageux car ils peuvent se passer de la régénération des résines échangeueses d'ions à l'aide de produits chimiques. De manière à résoudre ce problème, le procédé de l'invention consiste à alimenter en eau non traitée et en eau non concentrée, respectivement, les chambres de dessalement et les chambres de concentration de manière à ce que le rapport entre le débit d'eau non traitée et le débit d'eau non concentrée se trouve dans une plage allant de 6:1 à 12:1 et que la vitesse linéaire de deux flux d'eau se trouve dans une plaque allant de 75 à 150 m/h. Le taux et la vitesse indiqués ci-dessus sont nécessaires pour augmenter la migration d'ions d'impuretés vers les chambres de concentration afin d'accroître la conductivité de ses chambres.
PCT/JP1996/001517 1994-11-29 1996-06-03 Procede de production d'eau deionisee par une technique de deionisation electrique WO1997046491A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
JP31921894A JP3305139B2 (ja) 1994-11-29 1994-11-29 電気脱イオン法による脱イオン水の製造方法
PCT/JP1996/001517 WO1997046491A1 (fr) 1994-11-29 1996-06-03 Procede de production d'eau deionisee par une technique de deionisation electrique

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JP31921894A JP3305139B2 (ja) 1994-11-29 1994-11-29 電気脱イオン法による脱イオン水の製造方法
PCT/JP1996/001517 WO1997046491A1 (fr) 1994-11-29 1996-06-03 Procede de production d'eau deionisee par une technique de deionisation electrique

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US6284124B1 (en) 1999-01-29 2001-09-04 United States Filter Corporation Electrodeionization apparatus and method
US7658828B2 (en) 2005-04-13 2010-02-09 Siemens Water Technologies Holding Corp. Regeneration of adsorption media within electrical purification apparatuses
US7820024B2 (en) 2006-06-23 2010-10-26 Siemens Water Technologies Corp. Electrically-driven separation apparatus
US8377279B2 (en) 2003-11-13 2013-02-19 Siemens Industry, Inc. Water treatment system and method
US8585882B2 (en) 2007-11-30 2013-11-19 Siemens Water Technologies Llc Systems and methods for water treatment
US8721862B2 (en) 2001-10-15 2014-05-13 Evoqua Water Technologies Llc Apparatus for fluid purification and methods of manufacture and use thereof
US8894834B2 (en) 2003-11-13 2014-11-25 Evoqua Water Technologies Llc Water treatment system and method
US9023185B2 (en) 2006-06-22 2015-05-05 Evoqua Water Technologies Llc Low scale potential water treatment
US9592472B2 (en) 2006-06-13 2017-03-14 Evoqua Water Technologies Llc Method and system for irrigation
US10252923B2 (en) 2006-06-13 2019-04-09 Evoqua Water Technologies Llc Method and system for water treatment
US10625211B2 (en) 2006-06-13 2020-04-21 Evoqua Water Technologies Llc Method and system for water treatment
US11820689B2 (en) 2017-08-21 2023-11-21 Evoqua Water Technologies Llc Treatment of saline water for agricultural and potable use

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US7658828B2 (en) 2005-04-13 2010-02-09 Siemens Water Technologies Holding Corp. Regeneration of adsorption media within electrical purification apparatuses
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