JP5295927B2 - Electric deionized water production equipment - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide electric deionized water making apparatus capable of making effective use of a hydrogen ion or hydroxide ion generated in an anode chamber or cathode chamber by ensuring good water quality of water to be treated. <P>SOLUTION: The electric deionized water making apparatus is disposed between the cathode chamber E1 and cathode side concentration chamber C1, made adjacent to a cathode side concentration chamber through a second anion exchange membrane a2, made adjacent to the cathode chamber through a third anion exchange membrane a3, charged with at least an anion exchanger, disposed between a sub anion desalting chamber S2 through which the water to be treated passes or the anode chamber E2 and an anode side condensation chamber C2, made adjacent to the anode side condensation chamber through a second cation exchange membrane c2, made adjacent to the anode chamber through a third cation exchange membrane c3, charged with at least a cation exchanger, and has at least either one sub cation desalting chamber S1 through which the water to be treated passes. The inflow directions of the water to be treated flowing into the sub desalting chambers S1, S2 and electrode water flowing into the electrode chambers E2, E1 adjacent to the sub desalting chamber are the same. <P>COPYRIGHT: (C)2011,JPO&amp;INPIT

Description

  The present invention relates to an electrical deionized water production apparatus, and more particularly to a configuration for passing electrode water through an electrode chamber.

As a deionized water production apparatus, a production apparatus that performs deionization by passing water to be treated through an ion exchanger is known. In this apparatus, when the ion exchange group of the ion exchanger is saturated and the desalting performance is deteriorated, it is necessary to regenerate with a chemical such as acid or alkali. That is, the anion and cation adsorbed on ion exchange groups, acid or alkali from the H ^+, OH ^- and replacing processing is required. In recent years, in order to eliminate such disadvantages in operation, an electric deionized water production apparatus (hereinafter sometimes referred to as a deionized water production apparatus) that does not require regeneration by a chemical agent has been put into practical use.

  The deionized water production apparatus is an apparatus that combines electrophoresis and electrodialysis. In the deionized water production apparatus, an ion exchanger is filled between an anion exchange membrane and a cation exchange membrane to form a main desalting chamber, and a concentration chamber is provided outside the anion exchange membrane and the cation exchange membrane, respectively, and further outside the chamber. This is an apparatus in which an anode chamber having an anode and a cathode chamber having a cathode are arranged.

In order to produce deionized water by the deionized water production apparatus, water to be treated is passed through the main demineralization chamber with a DC voltage applied to the electrodes. The ionic component in the water to be treated is adsorbed by the ion exchanger in the demineralization chamber and subjected to deionization (demineralization) treatment. In the desalting chamber, the applied voltage causes water decomposition at the interface between the anion exchanger and the cation exchanger in the desalting chamber to generate hydrogen ions and hydroxide ions (2H ₂ O → H ⁺ + OH ⁻ ). The ion component adsorbed on the ion exchanger is exchanged with the hydrogen ions and hydroxide ions to be released from the ion exchanger. The liberated ion component is electrophoresed to the ion exchange membrane, electrodialyzed on the ion exchange membrane, and discharged into the water flowing through the concentration chamber. Thus, in the deionized water production apparatus, hydrogen ions and hydroxide ions continuously act as acid and alkali regenerators for regenerating the ion exchanger. For this reason, the regeneration by the medicine is basically unnecessary, and the continuous operation can be performed without the regeneration of the ion exchanger by the medicine.

The electrolysis reaction of water occurs in the anode chamber and the cathode chamber of the deionized water production apparatus, and this reaction also generates hydrogen ions and hydroxide ions (2H ₂ O → O ₂ + 4H ⁺ + 4e ⁻ / 2H). ₂ O + 2e ⁻ → H ₂ + 2OH ⁻ ). Therefore, attempts have been made to use hydrogen ions generated in the anode chamber and hydroxide ions generated in the cathode chamber for the regeneration of the ion exchanger. Abundant hydrogen ions and hydroxide ions are generated in the anode and cathode chambers. If these can be used effectively, the applied voltage between the anode and cathode of the deionized water production system can be reduced and the power used. The amount can be reduced.

  Patent Document 1 discloses a deionized water production apparatus that uses an anode chamber and a cathode chamber as main demineralization chambers. The anode chamber is filled with a cation exchanger, and the cathode chamber is filled with an anion exchanger. For this reason, the hydrogen ions generated in the anode chamber can regenerate the cation exchanger, and the hydroxide ions generated in the cathode chamber can regenerate the anion exchanger.

Japanese Patent No. 3793229

  The anode chamber and the cathode chamber contain gas components and oxidizing substances generated by water electrolysis. For this reason, when the anode chamber and the cathode chamber are used as the main desalting chamber as described in Patent Document 1, these substances may be contained in the deionized water to be treated. When such a phenomenon occurs, there is a possibility that the desired water quality cannot be obtained when the deionized water production apparatus is used for the purpose of producing pure water because oxidation deterioration of the functional material proceeds.

  The present invention makes it possible to ensure good water quality of the water to be treated, and to utilize at least one of hydrogen ions and hydroxide ions generated in the anode chamber or the cathode chamber for regeneration of the ion exchanger. An object of the present invention is to provide an electric deionized water production apparatus capable of reducing power consumption.

  The electric deionized water production apparatus of the present invention comprises a pair of electrode chambers, each comprising an anode chamber and a cathode chamber, through which electrode water flows, and a cation exchanger and an anion exchanger. Is located between the pair of electrode chambers and the main desalting chamber through the first cation exchange membrane. Located between the adjacent cathode-side concentrating chamber and the pair of electrode chambers, on the anode chamber side of the main desalting chamber, adjacent to the main desalting chamber via the first anion exchange membrane And an anode side concentrating chamber. The electric deionized water production apparatus is also located between the cathode chamber and the cathode side concentrating chamber, is adjacent to the cathode side concentrating chamber via the second anion exchange membrane, and is connected to the cathode via the third anion exchange membrane. A secondary anion desalting chamber, which is adjacent to the chamber and filled with at least an anion exchanger and in which the water to be treated flows, or located between the anode chamber and the anode-side concentrating chamber, and the anode side through the second cation exchange membrane At least one of the secondary cation desalting chambers adjacent to the concentrating chamber, adjacent to the anode chamber through the third cation exchange membrane, filled with at least a cation exchanger, and in which the water to be treated flows. Has a room. The inflow directions of the water to be treated flowing into the sub-desalting chamber and the electrode water flowing into the electrode chamber adjacent to the sub-desalting chamber are the same.

  According to the present invention, a secondary anion desalination chamber is provided between the cathode chamber and the cathode side enrichment chamber, or a secondary cation desalination chamber is provided between the anode chamber and the anode side enrichment chamber, or both of them are Is provided. The hydroxide ions generated in the cathode chamber move to the secondary anion desalting chamber through the third anion exchange membrane. In the secondary anion desalting chamber, the anion component of the treated water that has flowed in is adsorbed by the anion exchanger, and the anion exchanger that has adsorbed the anion component is regenerated by the hydroxide ions that have moved from the cathode chamber. The water to be treated also flows into the main desalting chamber, and the anion component is adsorbed on the anion exchanger. In the main desalting chamber, water is dissociated into hydrogen ions and hydroxide ions by the water splitting reaction in the main desalting chamber, so that the anion exchanger with adsorbed anion components is the water produced in the main desalting chamber. Regenerated by oxide ions.

  Hydrogen ions generated in the anode chamber move to the secondary cation desalting chamber through the third cation exchange membrane. In the secondary cation desalting chamber, the cation component of the treated water that has flowed in is adsorbed by the cation exchanger, and the cation exchanger that has adsorbed the cation component is regenerated by the hydrogen ions that have moved from the anode chamber. In the main desalting chamber, the cation exchanger on which the cation component is adsorbed is regenerated by hydrogen ions generated by the water splitting reaction in the main desalting chamber.

  Thus, in addition to hydrogen ions and hydroxide ions generated by the water splitting reaction in the main desalting chamber, at least one of hydroxide ions generated in the cathode chamber or hydrogen ions generated in the anode chamber One of them can be effectively used for regeneration of the ion exchanger. In addition, since the anode chamber and the cathode chamber are separated from the secondary cation desalting chamber or the secondary anion desalting chamber into which the water to be treated flows, and the third cation exchange membrane or the third anion exchange membrane, the anode chamber In addition, the quality of the water to be treated is prevented from being deteriorated by the gas component and the oxidizing substance contained in the cathode chamber.

  In addition, in a configuration in which a sub-desalting chamber is provided adjacent to the electrode chamber, the ionic component contained in the electrode water moves to the adjacent sub-desalting chamber, and the water to be treated from which the cation component and the anion component have been removed. May contaminate. When the ion component contained in the electrode water enters the electrode chamber, it moves to the adjacent sub-desalting chamber by the potential between the anode chamber and the cathode chamber. This movement of the ionic component occurs as soon as the electrode water enters the electrode chamber, and it is considered that many ionic components move to the sub-desalting chamber near the entrance of the electrode chamber. According to this embodiment, the inflow directions of the water to be treated flowing into the sub-desalination chamber and the electrode water flowing into the electrode chamber adjacent to the sub-desalination chamber are the same. That is, when the secondary anion demineralization chamber is provided, the direction of the water to be treated flowing in the secondary anion demineralization chamber and the flow of the electrode water flowing in the cathode chamber adjacent thereto are the same. Similarly, when the secondary cation demineralization chamber is provided, the flow direction of the water to be treated flowing in the secondary cation demineralization chamber and the electrode water flowing in the anode chamber adjacent thereto are the same. Because of this configuration, most of the ionic components that move to the secondary desalting chamber flow into the vicinity of the inlet of the secondary desalting chamber. For this reason, ionic components are sufficiently removed in the secondary desalting chamber, and finally discharged through the concentration chamber to the outside of the system. In this way, the quality of the treated water is also prevented from deteriorating by aligning the flow directions of the sub-desalting chamber and the electrode chamber.

  According to the present invention, it is possible to ensure good water quality of the water to be treated, and at least one of hydrogen ions and hydroxide ions generated in the anode chamber or the cathode chamber is used for regeneration of the ion exchanger. Thus, an electric deionized water production apparatus capable of reducing power consumption can be provided.

It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on one Embodiment of this invention. It is a partial view of the deionized water manufacturing apparatus which shows the structure from which the flow direction of electrode water is the same as the flow direction of a subdemineralization chamber, and a different structure. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on other embodiment of this invention. It is a schematic block diagram of the deionized water manufacturing apparatus which concerns on a comparative example. It is a graph which shows the performance of the deionized water manufacturing apparatus of an Example and a comparative example.

  Hereinafter, some embodiments of the electric deionized water production apparatus of the present invention will be described with reference to the drawings.

  FIG. 1 is a schematic configuration diagram of a deionized water production apparatus according to an embodiment of the present invention. The deionized water production apparatus 1 includes a main demineralization chamber D and a main demineralization chamber D between a pair of electrode chambers E1 and E2 including an anode chamber E2 having an anode 4 and a cathode chamber E1 having a cathode 5. A pair of concentrating chambers C1, C2 located on both sides, a secondary anion desalting chamber S2 positioned between the concentrating chamber C1 and the cathode chamber E1, and a secondary cation desalting chamber positioned between the concentrating chamber C2 and the anode chamber E2. S1 is provided, and these chambers are partitioned by ion exchange membranes a1 to a3 and c1 to c3. In the following description, the concentrating chamber adjacent to the main desalting chamber D on the cathode side is referred to as the cathode concentrating chamber C1, and the concentrating chamber adjacent to the main desalting chamber D on the anode side is referred to as the anode concentrating chamber C2.

  The cathode side concentrating chamber C1 is adjacent to the main desalting chamber D via the first cation exchange membrane c1, and the anode side concentrating chamber C2 is adjacent to the main desalting chamber D via the first anion exchange membrane a1. Yes. The secondary cation desalting chamber S1 is adjacent to the anode concentration chamber C2 via the second cation exchange membrane c2, and is adjacent to the anode chamber E2 via the third cation exchange membrane c3. The secondary anion demineralization chamber S2 is adjacent to the cathode-side concentration chamber C1 via the second anion exchange membrane a2, and is adjacent to the cathode chamber E1 via the third anion exchange membrane a3.

  The main desalting chamber D has a main cation desalting chamber D1 adjacent to the first cation exchange membrane c1, and a main anion desalting chamber D2 adjacent to the first anion exchange membrane a1. The main cation desalting chamber D1 and the main anion desalting chamber D2 are adjacent to each other through the intermediate ion exchange membrane 3.

The main cation desalting chamber D1 is filled with at least a cation exchanger, and mainly cation components (Na ⁺ , Ca ²⁺ , Mg ^2+, etc.) in the water to be treated are removed. Examples of the cation exchanger include ion exchange resins, ion exchange fibers, and monolithic porous ion exchangers, and the most versatile ion exchange resin is preferably used. Examples of the cation exchanger include weakly acidic cation exchangers and strongly acidic cation exchangers. The main cation desalting chamber D1 may be further filled with an anion exchanger. Examples of the filling form of the ion exchanger filled in the main cation desalting chamber D1 include a single bed form of the cation exchanger, a mixed bed form of a cation exchanger and an anion exchanger, or a multiple bed form.

The main anion demineralization chamber D2 is filled with at least an anion exchanger and mainly contains anion components (Cl ⁻ , CO ₃ ²⁻ , HCO ₃ ⁻ , SiO ₂ (silica can take a special form) in the water to be treated. Since there are many, it is set as a display different from a general ion.) Etc.) are removed. Examples of the anion exchanger include ion exchange resins, ion exchange fibers, monolithic porous ion exchangers, etc., and the most versatile ion exchange resins are preferably used. Examples of the anion exchanger include weakly basic anion exchangers and strong basic anion exchangers. The main anion desalting chamber D2 may be further filled with a cation exchanger. Examples of the packed form of the ion exchanger filled in the main anion desalting chamber D2 include a single bed form of the anion exchanger, a mixed bed form of an anion exchanger and a cation exchanger, or a multiple bed form.

  The intermediate ion exchange membrane 3 is selected in consideration of the quality of the water to be treated, the water quality required for the deionized water, the type of ion exchanger filled in the main cation demineralization chamber D1 or the main anion demineralization chamber D2, and the like. Can do. The intermediate ion exchange membrane 3 may be either an anion exchange membrane or a single membrane of a cation exchange membrane, or a composite membrane having both an anion exchange membrane and a cation exchange membrane.

  In this way, the main desalting chamber D is divided into two small desalting chambers, a main cation desalting chamber D1 and a main anion desalting chamber D2, and a concentrating chamber is adjacent to each outside (two main desalting chambers). Configuration) is capable of multi-stage treatment of water to be treated, and is effective in improving deionization performance. In addition, since it is not necessary to provide a concentration chamber between the main cation demineralization chamber D1 and the main anion demineralization chamber D2, the applied voltage between the anode and the cathode can be suppressed, the power consumption can be reduced, and the operation cost can be reduced. Is possible.

  The main desalting chamber D may be a conventionally known main desalting chamber. In the configuration of one main desalting chamber, the main desalting chamber is filled with a cation exchanger and an anion exchanger, and cation removal and anion removal are performed in one desalting chamber. The cation exchanger and the anion exchanger are desirably packed in a mixed bed form or a multi-bed form. The structure of one main desalination chamber is simple, and such a configuration can be adopted depending on the required water quality.

  The cathode concentration chamber C1 is provided to take in the cation component discharged from the main cation demineralization chamber D1 and the anion component discharged from the auxiliary anion demineralization chamber S2, and to release them out of the system. The anode side concentrating chamber C2 is provided to take in the anion component discharged from the main anion desalting chamber D2 and the cation component discharged from the auxiliary cation desalting chamber S1, and to release them out of the system. The concentration chamber supply water flows into the concentration chambers C1 and C2, and the concentration chamber supply water becomes concentrated water containing a cation component and an anion component and is discharged from the concentration chambers C1 and C2. In order to suppress the electrical resistance of the deionized water production apparatus 1, the concentration chambers C1 and C2 may be filled with an ion exchanger.

  The sub cation demineralization chamber S1 has the same configuration as the main cation demineralization chamber D1, but only the cation exchanger is filled with a single bed.

  The secondary anion desalting chamber S2 has the same configuration as the main anion desalting chamber D2, but only the anion exchanger is filled with a single bed.

The anode chamber E2 accommodates the anode 4. The anode 4 is made of a metal net or plate. When the water to be treated contains Cl ⁻ , chlorine is generated at the anode 4. For this reason, it is desirable to use a material having chlorine resistance for the anode 4, and examples thereof include a metal such as platinum, palladium, iridium, or a material obtained by coating titanium with these metals.

  The cathode chamber E1 accommodates the cathode 5. The cathode 5 is made of a metal net or plate, and for example, a stainless steel net or plate can be used.

  Electrode water flows into the anode chamber E2 and the cathode chamber E1. As will be described later, these electrode waters generate hydrogen ions and hydroxide ions by electrolysis in the vicinity of the electrodes. In order to suppress the electrical resistance of the deionized water production apparatus 1, the anode chamber E2 and the cathode chamber E1 are preferably filled with an ion exchanger. By filling the ion exchanger, the movement of hydrogen ions to the secondary cation desalting chamber S1 and the movement of hydroxide ions to the secondary anion desalting chamber S2 described later are smoothly performed.

  Examples of the ion exchanger filled in the anode chamber E2 and the cathode chamber E1 include ion exchange resins, ion exchange fibers, monolithic porous ion exchangers, etc., and the most general-purpose ion exchange resins are preferably used. The anode chamber E2 is filled with a single bed of a cation exchanger such as a weak acid cation exchanger or a strong acid cation exchanger. The cathode chamber E1 is filled with a single bed of anion exchangers such as a weakly basic anion exchanger and a strongly basic anion exchanger. Accordingly, as described above, the movement of hydrogen ions to the secondary cation desalting chamber S1 and the movement of hydroxide ions to the secondary anion desalting chamber S2 are performed smoothly.

  Each electrode chamber E1, E2, main cation demineralization chamber D1, main anion demineralization chamber D2, each concentration chamber C1, C2, sub cation demineralization chamber S1, and sub anion demineralization chamber S2 each have a plate with an opening. It is provided in the inside of the frame 2 which is a shape member. In FIG. 1, the frame body 2 is shown integrally, but actually, a separate frame body is provided for each room, and the frame bodies are provided in close contact with each other. The frame 2 is not particularly limited as long as it has insulating properties and does not leak treated water. For example, resin such as polyethylene, polypropylene, polyvinyl chloride, ABS, polycarbonate, m-PPE (modified polyphenylene ether) Can be mentioned.

  Several flow paths U1 to U5 and L1 to L5 are provided for communication between rooms, or for supply and discharge of treated water, concentration chamber supply water, electrode water, and the like.

  One end of the flow path L1 located in the lower part of the deionized water production apparatus 1 is connected to the supply side of the water to be treated, and the other end side branches in the middle, so that the main cation demineralization chamber D1 and the sub cation demineralization chamber Connected to S1. The flow path U1 located in the upper part of the deionized water production apparatus 1 is connected to the main cation demineralization chamber D1 and the sub cation demineralization chamber S1, merges in the middle, and is connected to one end of the transition pipe Y. The other end of the crossover pipe Y is connected to a flow path L2 located at the lower part of the deionized water production apparatus 1, and the flow path L2 is branched in the middle so that the main anion demineralization chamber D2 and the secondary anion demineralization chamber Connected to S2. The flow path U2 located in the upper part of the deionized water production apparatus 1 is connected to the main anion demineralization chamber D2 and the subanion demineralization chamber S2, merges in the middle, and is connected to the discharge side of the treated water. .

  The flow path U3 located in the upper part of the deionized water production apparatus 1 is connected to the supply side of the concentrating chamber supply water, and is branched halfway on the other end side to connect to the cathode side concentrating chamber C1 and the anode side concentrating chamber C2. Has been. The flow path L3 located in the lower part of the deionized water production apparatus 1 is connected to the cathode-side concentrating chamber C1 and the anode-side concentrating chamber C2, merges on the way, and is connected to the concentrated water discharge side. In FIG. 1, the flow paths U <b> 1 to U <b> 3, L <b> 1 to L <b> 3 are located outside the frame body 2 for convenience of illustration, but these flow paths U <b> 1 to U <b> 3, L <b> 1 to L <b> 3 are built in the frame body 2. It is advantageous.

  Flow paths L4 and U4 are connected to the anode chamber E2, and electrode water flows into the anode chamber E2 from the flow path L4 connected to the lower portion of the anode chamber E2, and is connected to the upper portion of the anode chamber E2. It is discharged from the anode chamber E2 through U4. Channels L5 and U5 are connected to the cathode chamber E1, and electrode water flows into the cathode chamber E1 from the channel L5 connected to the lower part of the cathode chamber E1, and is connected to the upper part of the cathode chamber E1. It is discharged from the cathode chamber E1 through U5. That is, the inflow directions of the water to be treated flowing into the sub-desalting chambers S1, S2 and the electrode water flowing into the electrode chambers E2, E1 adjacent to the sub-desalting chambers S1, S2 are the same. Specifically, the inflow direction of the water to be treated flowing into the secondary cation desalting chamber S1 and the electrode water flowing into the anode chamber E2 adjacent to the secondary cation desalting chamber S1 are the same, and the secondary anion desalting chamber S2 The inflow directions of the water to be treated flowing into the cathode water and the electrode water flowing into the cathode chamber E1 adjacent to the secondary anion demineralization chamber S2 are the same.

  Next, the flow of water to be treated and the principle of deionization will be described with reference to FIG.

  In advance, the concentration chamber supply water is supplied from the flow path U3 to the concentration chambers C1 and C2, and is discharged from the flow path L3. Electrode water is supplied to the electrode chamber E1 from the flow path L5 and discharged from the flow path U5. Similarly, electrode water is supplied to the electrode chamber E2 from the flow path L4 and discharged from the flow path U4. A predetermined voltage is applied between the anode 4 and the cathode 5. In this state, water to be treated is caused to flow in parallel from the flow path L1 into the main cation desalting chamber D1 and the sub cation desalting chamber S1. The cation component is removed from the water to be treated in the main cation demineralization chamber D1 and the sub cation demineralization chamber S1.

Specifically, a cation component such as Na ⁺ is adsorbed on the cation exchanger filled in the main cation demineralization chamber D1 in the main cation demineralization chamber D1. In the main cation desalting chamber D1, a reaction in which water is dissociated into hydrogen ions (hereinafter referred to as H ⁺ ) and hydroxide ions (hereinafter referred to as OH ⁻ ) by water splitting reaction proceeds continuously. Yes. H ⁺ is exchanged with a cation component such as Na ⁺ adsorbed on the cation exchange resin, and the cation exchanger filled in the main cation desalting chamber D1 is regenerated. The removed cations such as Na ⁺ are attracted to the cathode 5 side by the potential between the anode 4 and the cathode 5, pass through the first cation exchange membrane c 1, flow into the cathode side concentrating chamber C 1, and discharged outside the system. The

In the secondary cation desalting chamber S1, cation components such as Na ⁺ are adsorbed on the cation exchanger filled in the secondary cation desalting chamber S1. In the anode chamber E2, a reaction in which oxygen gas and H ⁺ are generated from water by an electrolysis reaction (2H ₂ O → O ₂ + 4H ⁺ + 4e ⁻ ) proceeds continuously. Oxygen gas rises in the anode chamber E2 and is discharged out of the deionized water production apparatus 1 together with the electrode water. H ⁺ flows into the secondary cation desalting chamber S1 through the third cation exchange membrane c3. H ⁺ flowing into the secondary cation desalting chamber S1 is exchanged with the cation component adsorbed on the cation exchanger, and the cation exchanger is regenerated. The removed cation component such as Na ⁺ is attracted to the cathode 5 side by the potential between the anode 4 and the cathode 5, passes through the second cation exchange membrane c2, flows into the anode side concentrating chamber C2, and is discharged outside the system. Is done.

Thus, the water to be treated from which the cation component such as Na ⁺ has been removed merges in the flow path U1 and flows into the flow path L2 through the transition pipe Y. The treated water that has flowed into the flow path L2 flows in parallel into the main anion demineralization chamber D2 and the subanion demineralization chamber S2. The anion component is removed from the water to be treated in the main anion demineralization chamber D2 and the subanion demineralization chamber S2.

Specifically, an anion component such as Cl 2 ⁻ is adsorbed to the anion exchanger filled in the main anion desalting chamber D2 in the main anion desalting chamber D2. In the main anion demineralization chamber D2, OH ⁻ is continuously generated by the same water splitting reaction as occurs in the main cation demineralization chamber D1. OH ⁻ is exchanged with an anion component such as Cl 2 ⁻ adsorbed on the anion exchange resin to regenerate the anion exchanger. The removed anion component such as Cl ⁻ is attracted to the anode 4 side by the potential between the anode 4 and the cathode 5, passes through the first anion exchange membrane a 1, flows into the anode side concentration chamber C 2, and is discharged outside the system. Is done.

In sub anion depletion chamber S2, Cl ^- anion components, etc., are adsorbed to the anion exchanger filled in the sub anion depletion chamber S2. In the cathode chamber E1, a reaction in which hydrogen gas and OH ⁻ are generated from water by an electrolysis reaction (2H ₂ O + 2e ⁻ → H ₂ + 2OH ⁻ ) proceeds continuously. Hydrogen gas rises in the cathode chamber E1, and is discharged out of the deionized water production apparatus 1 together with the electrode water. OH ⁻ flows into the secondary anion desalting chamber S2 through the third anion exchange membrane a3 and is exchanged with the anion component adsorbed on the anion exchanger, thereby regenerating the anion exchanger. Removed Cl ^- anion components such as the anode 4, are attracted to the anode 4 side by the potential between the cathode 5 passes through the second anion exchange membrane a2 flowing into the cathode side concentrating compartment C1. The treated water from which the anion components have been removed in the main anion demineralization chamber D2 and the subanion demineralization chamber S2 joins in the flow path U2, and is deionized water and discharged out of the deionized water production apparatus 1.

  Concentration chamber supply water supplied to the cathode-side enrichment chamber C1 and the anode-side enrichment chamber C2 through the flow path U3 is a main cation demineralization chamber D1, a main anion demineralization chamber D2, a sub-cation demineralization chamber S1, and a sub-anion. The cation component and the anion component discharged from the demineralization chamber S2 are taken in and discharged to the outside of the deionized water production apparatus 1 through the flow path L3 located at the lower part of the deionized water production apparatus 1.

In this way, the cation component is removed from the water to be treated in the main cation demineralization chamber D1 and the sub cation demineralization chamber S1, and the cation exchanger in the main cation demineralization chamber D1 is generated in the main cation demineralization chamber D1. reproduced by H ⁺ was a cation exchanger of the secondary cation depletion chamber S1 is reproduced by the H ⁺ generated in the anode chamber E2. Similarly, the anion component was removed from the water to be treated in the main anion desalting chamber D2 and the secondary anion desalting chamber S2, and the anion exchanger in the main anion desalting chamber D2 was generated in the main anion desalting chamber D2. Regenerated by OH ^−, the anion exchanger in the secondary anion desalting chamber S2 is regenerated by OH ⁻ generated in the cathode chamber E1. Therefore, H ⁺ and OH ⁻ generated in the electrode chambers (cathode chamber E1 and anode chamber E2) and discarded without being used in the past can be effectively used for regeneration of the ion exchanger.

Since the generation efficiency of H ⁺ and OH ⁻ in the anode chamber E2 and the cathode chamber E1 is high, a sufficient amount of H ⁺ and OH ⁻ moves to the secondary cation desalting chamber S1 and the secondary anion desalting chamber S2 even if the potential is low. To do. For this reason, the applied voltage between electrodes can be suppressed and the operating cost of the deionized water manufacturing apparatus 1 can be reduced.

  In the present embodiment, the secondary cation desalting chamber S1 and the secondary anion desalting chamber S2 are provided as new desalting chambers, but it is not necessary to add a new concentration chamber accordingly. That is, the secondary cation demineralization chamber S1 is simply provided between the anode side enrichment chamber C2 and the anode chamber E2, and the secondary anion desalination chamber S2 is simply provided between the cathode side concentration chamber C1 and the cathode chamber E1. The number of concentration chambers can be relatively reduced. This not only reduces the size and cost of the device, but also reduces the applied voltage and operating costs.

  In this embodiment, the water to be treated is caused to flow in and out of the main cation demineralization chamber D1 and the sub cation demineralization chamber S1 in parallel, and similarly, the water to be treated is discharged into the main anion demineralization chamber D2 and the sub anion demineralization chamber S2. Inflow and outflow in parallel. This configuration is advantageous particularly when the processing capacity of the apparatus is large. Hereinafter, the main cation demineralization chamber D1 will be described as an example. In order to increase the processing capacity, it is common to provide a plurality of main cation demineralization chambers D1 and connect them in parallel as in the embodiment described later. It is. However, when the main cation demineralization chamber D1 and the sub cation demineralization chamber S1 connected in parallel are connected in series, the total flow rate of water to be treated passing through the plurality of main cation demineralization chambers D1 and the sub cation demineralization chamber S1. It is necessary to match the flow rate of the water to be treated passing through. This is because the secondary cation desalting chamber S1 needs to be adjacent to the anode chamber E2, and in principle, only one can be provided. For this reason, when the total flow rate of the main cation demineralization chamber D1 increases, it is necessary to process the same flow rate as the total flow rate of the main cation demineralization chamber D1 in one sub-cation demineralization chamber S1. When the water flow rate is increased without changing the size of the secondary cation demineralization chamber S1, the water flow differential pressure, that is, the pressure loss generated in the secondary cation demineralization chamber S1 increases in proportion to the water flow rate. Therefore, even if it is going to increase the processing capacity of an apparatus, a big restriction | limiting arises from a viewpoint of the water flow differential pressure | voltage of sub-cation desalination chamber S1.

  From the above, in order to increase the water flow rate of the secondary cation desalting chamber S1, there is no practical method other than increasing the width of the secondary cation desalting chamber S1 in the voltage application direction. However, when the main cation demineralization chamber D1 and the sub cation demineralization chamber S1 connected in parallel are connected in series, the total width of the main cation demineralization chamber and the width of the sub cation demineralization chamber S1 both increase. The width increases at a rate that exceeds the rate of increase in processing capacity. As a result, the separation distance between the cathode and the anode is increased, and not only the apparatus size is increased, but also the applied potential between the anode and the cathode is increased, and the influence on the operating cost is inevitable.

  In this embodiment, since the water to be treated is caused to flow in and out of the main cation demineralization chamber D1 and the sub cation demineralization chamber S1 in parallel, the water flow rate in the sub cation demineralization chamber S1 is the main cation demineralization chamber D1. It does not depend on the water flow rate. In other words, since the water to be treated is distributed to the sub cation demineralization chamber S1 and the main cation demineralization chamber D1, an increase in water flow differential pressure in the sub cation demineralization chamber S1 can be easily avoided. Further, by connecting the main cation demineralization chamber D1 and the sub cation demineralization chamber S1 in parallel, the water flow differential pressure of the entire apparatus can be suppressed as compared with the case of connecting them in series. In addition, since it is not necessary to increase the size of the secondary cation desalting chamber S1 in accordance with the increase in the water to be treated, the applied voltage between the anode and the cathode can be suppressed. This is a particularly significant advantage in a deionized water production apparatus in which a large number of main demineralization chambers are arranged. The same applies to the main anion desalting chamber D2 and the secondary anion desalting chamber S2.

  Moreover, in this embodiment, as above-mentioned, the inflow direction of the to-be-processed water which flows into sub desalting chamber S1, S2 and the electrode water which flows into electrode chamber E2, E1 adjacent to sub desalting chamber S1, S2 is the same. It is. The effect of this configuration will be described with reference to FIG. FIG. 2A is a partial configuration diagram showing a part from the anode chamber E2 to the anode side concentrating chamber C2 of the deionized water production apparatus of the comparative example, and FIG. 2B shows a similar range. It is a partial block diagram of this embodiment taken out and shown. In these drawings, thick white arrows indicate the directions in which electrode water, water to be treated, and the like flow through the chambers.

Referring to FIG. 2A, the electrode water contains a cation component (Na ⁺ is shown as an example), and when the electrode water flows into the anode chamber E2, the cation component is the anode 4 and the cathode 5. Due to the potential between them, it is attracted to the cathode 5 side and moves to the secondary cation desalting chamber S1 through the third cation exchange membrane c3. However, the electrode water in the anode chamber E2 and the water to be treated in the secondary cation demineralization chamber S1 flow in opposite directions (counterflow). This indicates that the inflow position of the electrode water in the anode chamber E2 is the secondary cation desorption. It means that there is a positional relationship adjacent to the discharge position of the water to be treated in the salt chamber S1. For this reason, the cation component moved to the secondary cation demineralization chamber S1 is discharged from the secondary cation demineralization chamber S1 without being removed in the secondary cation demineralization chamber S1. As a result, the cation component contained in the electrode water is mixed into the water to be treated, and the quality of the water to be treated is deteriorated.

On the other hand, referring to FIG. 2 (b), the electrode water in the anode chamber E2 and the water to be treated in the sub-cation demineralization chamber S1 flow in the same direction. , Adjacent to the inflow position of the water to be treated in the sub cation demineralization chamber S1. For this reason, the cation component moved to the secondary cation demineralization chamber S1 is removed together with the cation component contained in the water to be treated in the secondary cation demineralization chamber S1, and discharged to the anode side concentration chamber. Thereby, deterioration of the water quality of the to-be-processed water by the cation component contained in electrode water is suppressed. Above, Cl ^- is exactly the same applies to the anion components such.

  Thus, in this embodiment, the water quality fall of the to-be-processed water which may arise when an auxiliary | assistant desalination chamber and an electrode chamber adjoin can be suppressed effectively.

  Deterioration of the quality of the water to be treated is further suppressed by adjusting in advance the ion component contained in the electrode water. Specifically, the specific resistance value of the electrode water supplied to the electrode chambers E1 and E2 (specific resistance value at the entrance of the electrode chambers E1 and E2) is 0.2 MΩ · cm or more and 18.2 MΩ · cm or less. It is preferable to make adjustments.

  3A to 3S show various arrangement patterns of the main desalting chamber and the sub-desalting chamber. In these figures, the lines connected to the concentration chamber are not shown. The code | symbol of each chamber respond | corresponds to the code | symbol in the above-mentioned embodiment, and the additional concentration chamber is shown by code | symbol C3. “M” represents an ion exchange membrane, and may be either a cation exchange membrane or an anion exchange membrane. Reference numerals X, Y, and Z in the figure are connected to the end portions of the line indicated by reference symbol X, the end portions of the line indicated by reference symbol Y, and the end portions of the line indicated by reference symbol Z, respectively. It means that.

  FIG. 3A shows a simplified arrangement pattern shown in FIG. 1 for comparison with other arrangement patterns, and a description thereof will be omitted. The configuration of each chamber and the ion exchanger filled in each chamber in each embodiment after FIG. 3B are the same as those in the embodiment shown in FIG.

  FIG. 3B shows an embodiment in which treated water that has flowed out of the main anion demineralization chamber flows into the main cation demineralization chamber. The arrangement pattern of each chamber is the same as in FIG. 3A, and only the flow path configuration is different. The treated water first flows in parallel to the main anion demineralization chamber D2 and the secondary anion demineralization chamber S2, and the anion component is removed. Thereafter, the treated water is divided into the main cation demineralization chamber D1 and the sub cation demineralization chamber S1. The cation component is removed in parallel.

  FIG. 3C shows an embodiment in which the secondary cation desalting chamber is omitted in the embodiment shown in FIG. 3A. The entire amount of water to be treated flows into the main cation desalting chamber D1, and the cation component is removed. Thereafter, the water to be treated flows in parallel into the main anion demineralization chamber D2 and the subanion demineralization chamber S2, and the anion component is removed. Since the secondary cation desalination chamber is not provided, the direction of the electrode water in the adjacent anode chamber E2 may be any. Accordingly, the direction of the electrode water in the anode chamber E2 is not shown.

  FIG. 3D shows an embodiment in which the secondary anion desalting chamber is omitted in the embodiment shown in FIG. 3A. First, the water to be treated flows into the main cation demineralization chamber D1 and the sub cation demineralization chamber S1 in parallel, and the cation component is removed. Thereafter, the entire amount of the water to be treated flows into the main anion demineralization chamber D2, and the anion component is removed. Since the secondary anion demineralization chamber is not provided, the direction of the electrode water in the adjacent cathode chamber E1 may be either. Accordingly, the direction of the electrode water in the cathode chamber E1 is not shown.

  FIG. 3E shows an embodiment in which two or more main desalting chambers are provided, and both a secondary cation desalting chamber and a secondary anion desalting chamber are provided. The main desalting chambers D and D ′ and the concentrating chambers C1 to C3 are alternately provided, and the concentrating chambers C1 and C2 are provided on the cathode side and the anode side of the main desalting chamber D, respectively. Concentration chambers C2 and C3 are adjacent to the side and the anode side, respectively. For the main desalting chamber D, the concentration chamber C1 is a cathode-side concentration chamber, and the concentration chamber C2 is an anode-side concentration chamber. For the main desalting chamber D ', the concentration chamber C2 is a cathode-side concentration chamber, and the concentration chamber C3 is an anode-side concentration chamber.

  The main desalting chamber D has a main cation desalting chamber D1 and a main anion desalting chamber D2, and the first cation exchange membrane c1 is provided on the cathode side of the main cation desalting chamber D1, and The first anion exchange membrane a1 is located on the anode side. Similarly, the main desalting chamber D ′ has a main cation desalting chamber D1 ′ and a main anion desalting chamber D2 ′, and the first cation exchange membrane c1 ′ is located on the cathode side of the main cation desalting chamber D1 ′. The first anion exchange membrane a1 ′ is located on the anode side of the main anion desalting chamber D2 ′.

  The secondary anion desalting chamber S2 is adjacent to the cathode chamber E1 via the third anion exchange membrane a3, and is adjacent to the concentration chamber C1 via the second anion exchange membrane a2. The secondary cation desalting chamber S1 is adjacent to the anode chamber E2 via the third cation exchange membrane c3, and is adjacent to the concentration chamber C3 via the second cation exchange membrane c2.

  The water to be treated flows in parallel into the main cation desalting chambers D1, D1 'and the sub cation desalting chamber S1 of each main desalting chamber D, D'. In the same manner, the water to be treated from which the cation component has been removed in these rooms flows in parallel into the main anion demineralization chambers D2, D2 ′ and the secondary anion demineralization chamber S2 of each main demineralization chamber D, D ′. , The anionic component is removed. Concentrated chamber supply water is supplied in parallel to each of the concentration chambers C1 to C3, and concentrated water containing a cation component and an anion component is discharged in parallel from each of the concentration chambers C1 to C3.

  Although the number of main desalting chambers is two in this embodiment, a desired number of main desalting chambers can be installed as necessary to increase the processing capacity of the apparatus.

  FIG. 3F shows that in the embodiment shown in FIG. 3E, the water to be treated is first flowed into the main anion demineralization chambers D2, D2 ′ and the secondary anion demineralization chamber S2, and then the main cation demineralization chambers D1, D1 ′ and Embodiment which flows in parallel with cation desalting chamber S1 is shown.

  FIG. 3G shows an embodiment in which the secondary cation desalting chamber is omitted in the embodiment shown in FIG. 3E. The total amount of water to be treated flows into the main cation desalting chambers D1 and D1 'of the main desalting chambers D and D', and the cation component is removed. Thereafter, the water to be treated flows in parallel into the main anion demineralization chambers D2, D2 'and the secondary anion demineralization chamber S2 of the main demineralization chambers D, D', and the anion components are removed. Since the secondary cation desalination chamber is not provided, the direction of the electrode water in the adjacent anode chamber E2 may be any. Accordingly, the direction of the electrode water in the anode chamber E2 is not shown.

  FIG. 3H shows an embodiment in which water to be treated that has flowed out of the main anion demineralization chamber flows into the main cation demineralization chamber, contrary to FIG. 3G. Specifically, the water to be treated flows in parallel into the main anion demineralization chambers D2, D2 'and the secondary anion demineralization chamber S2 of the main demineralization chambers D, D', and the anion component is removed. Thereafter, the entire amount of water to be treated flows into the main cation desalting chambers D1 and D1 'of the main desalting chambers D and D', and the cation component is removed.

  FIG. 3I shows an embodiment in which the secondary anion desalting chamber is omitted in the embodiment shown in FIG. 3E. The water to be treated flows in parallel into the main cation desalting chambers D1, D1 'and the sub cation desalting chamber S1 of the main desalting chambers D, D', and the cation component is removed. Thereafter, the entire amount of water to be treated flows into the main anion desalination chambers D2 and D2 'of the main desalination chambers D and D', and the anion components are removed. Since the secondary anion demineralization chamber is not provided, the direction of the electrode water in the adjacent cathode chamber E1 may be either. Accordingly, the direction of the electrode water in the cathode chamber E1 is not shown.

  FIG. 3J shows an embodiment in which water to be treated that has flowed out of the main anion demineralization chamber flows into the main cation demineralization chamber, contrary to FIG. 3I. Specifically, the entire amount of water to be treated flows into the main anion desalting chambers D2 and D2 'of the main desalting chambers D and D', and the anion components are removed. Thereafter, the water to be treated flows in parallel into the main cation demineralization chambers D1, D1 'and the sub cation demineralization chamber S1 of the main demineralization chambers D, D', and the cation component is removed.

  FIG. 3K is an embodiment in which treated water flows in series in the order of a secondary anion demineralization chamber S2, a main cation demineralization chamber D1, a main anion demineralization chamber D2, and a sub cation demineralization chamber S1 in the embodiment shown in FIG. 3A. The form is shown. Although illustration is abbreviate | omitted, the order in which to-be-processed water flows in is not limited to this, You may distribute | circulate in what order. As described above, such an embodiment is disadvantageous when a large number of main desalination chambers are installed, but does not have a major disadvantage when the number of main desalination chambers is limited. . Conversely, in this embodiment, the secondary cation demineralization chamber S1 and the secondary anion demineralization chamber S2 can be used as the pre-treatment chamber or the post-treatment chamber of the main cation demineralization chamber D1 and main anion demineralization chamber D2. It is possible to further improve the water quality.

  FIG. 3L shows an embodiment in which treated water that has flowed out of the main anion desalting chamber D2 and the secondary anion desalting chamber S2 is used as electrode water in the embodiment shown in FIG. 3A. Specifically, the water to be treated flows into the main cation demineralization chamber D1 and the sub cation demineralization chamber S1, and the cation component is removed. Thereafter, the water to be treated flows into the main anion demineralization chamber D2 and the subanion demineralization chamber S2, and the anion component is removed. As a result, the water to be treated has a water quality from which the cation component and the anion component have been efficiently removed. By causing a part of such treated water to flow into the anode chamber E2 and the cathode chamber E1 as electrode water, the cation component is transferred from the anode chamber E2 to the secondary cation desalting chamber S1, and the secondary anion from the cathode chamber E1. The migration of the anion component to the desalting chamber S2 can be further suppressed.

  Furthermore, as shown in FIG. 3M, in the embodiment of FIG. 3L, the electrode water (treated water) can be circulated in series in the cathode chamber E1 and the anode chamber E2. In the illustrated example, a part of the water to be treated that has flowed out from the main anion desalting chamber D2 and the secondary anion desalting chamber S2 flows into the cathode chamber E1 as electrode water, and the electrode water flowing out from the cathode chamber E1 further flows into the anode chamber. It flows into E2. The electrode water (treated water) may flow into the anode chamber E2 first, and then flow into the cathode chamber E1. This embodiment is effective for increasing the electrode water recovery efficiency.

  The embodiment shown in FIGS. 3L and 3M is shown as an example of an embodiment in which water to be treated is used as electrode water, and various other modifications are possible. For example, each embodiment shown in FIGS. 3A to 3K and 3N to 3S can be implemented in combination with this embodiment. Water can be taken from only one of the main anion demineralization chamber D2 or the subanion demineralization chamber S2 and used as electrode water. A part or all of the water to be treated flowing out from the main cation desalting chamber D1 and the sub cation desalting chamber S1 (or either one) can be supplied to the anode chamber E2.

  In addition, the flow direction of the water to be treated in the main desalination chamber is not restricted by the flow direction of the electrode water in the electrode chamber, unlike the sub-desalination chamber. And the inflow direction of the water to be treated into the main anion demineralization chamber can be opposite to each other (counterflow). About each form of FIG. 3C, 3D, 3G, 3H, 3I, and 3J, the deformation | transformation form which made the flow direction of the to-be-processed water in the main cation demineralization chamber D1 or the main anion demineralization chamber D2 down flow (downward), 3N-3S. In these forms, either the secondary cation desalting chamber S1 or the secondary anion desalting chamber S2 is not provided. When the secondary cation desalting chamber S1 is not provided (FIGS. 3N, 3P, 3Q), the water to be treated to the main anion desalting chamber D2 flows upward, but the main cation desalting chamber D1 (FIG. 3P, In the 3Q mode, the water to be treated to the main cation desalting chamber D1 ′) flows downward. When the secondary anion desalting chamber S2 is not provided (FIGS. 3O, 3R, 3S), the water to be treated to the main cation desalting chamber D1 flows upward, but the main anion desalting chamber D2 (FIG. 3R, In the 3S form, the water to be treated to the main anion desalting chamber D2 ′) flows downward.

  Thus, when the flow direction of the water to be treated in the main cation demineralization chamber D1 and the flow direction of the water to be treated in the main anion demineralization chamber D2 are in a countercurrent relationship, the current flowing between the anode and the cathode Has the merit of being easily equalized. That is, in the main cation demineralization chamber D1 and the main anion demineralization chamber D2, more ionic components are removed on the inlet side of the demineralization chamber. Easily formed on the inlet side. When the flow direction of the water to be treated in the main cation demineralization chamber D1 and the flow direction of the water to be treated in the main anion demineralization chamber D2 are in the same direction, the resin layer portion on which the ion component is adsorbed is On the same side (lower side of desalination chamber for upward flow, upper side of desalination chamber for downward flow). The resin layer part where the ionic component is adsorbed has high electrical resistance and it is difficult for the current to flow. As a result, the current flowing between the anode and the cathode is concentrated on the outlet side of the desalination chamber where the adsorption of the ionic component is small, resulting in local In addition, the current density increases, and the performance of the device is restricted. In the embodiment shown in FIGS. 3N to 3S, since the resin layer portion on which the ionic component is adsorbed is easily formed at positions opposite to each other in the main cation desalting chamber D1 and the main anion desalting chamber D2, the current is desalted. It flows (distributed) more evenly with respect to the flow path length of the chamber, leading to an improvement in the performance of the apparatus.

(Example)
The effect of this invention was confirmed using the deionized water manufacturing apparatus (Example) of the structure shown in FIG. 1 and the deionized water manufacturing apparatus shown in FIG. 4 (comparative example). 4 is the same as FIGS. 3A to 3S, and the symbol X in the drawing means that the ends of the line indicated by the symbol X are connected to each other. In the comparative example, the configuration of each chamber is the same as that of the embodiment shown in FIG. 1, and the flowing direction of the electrode water is different. In the comparative example, the electrode water flows in the opposite direction (counterflow) to the water to be treated flowing through the secondary cation desalting chamber S1 and the secondary anion desalting chamber S2. In contrast, in the embodiment, as described above, the electrode water flows in the same direction as the water to be treated that flows through the secondary cation desalting chamber S1 and the secondary anion desalting chamber S2. In addition, in the example, the water to be treated flows upward in each desalting chamber, whereas in the comparative example, it flows downward in each desalting chamber.

The specifications of the deionized water production apparatus, the water flow rate, the specifications of the feed water, etc. in the examples and comparative examples are as follows. CER is an abbreviation for cation exchange resin, and AER is an anion exchange resin.
・ Cathode chamber E1: Dimension 100 × 300 × 4 mm AER filling ・ Anode chamber E2: Dimension 100 × 300 × 4 mm CER filling ・ Main cation desalination chamber D1: Dimension 100 × 300 × 8 mm CER single bed ・ Main anion desalination chamber D2 : Dimension 100 × 300 × 8 mm AER single bed / secondary cation desalination chamber S1: Dimension 100 × 300 × 8 mm CER single bed / secondary anion desalination chamber S2: Dimension 100 × 300 × 8 mm AER single bed / concentration chamber: Dimension 100 × 300 × 4mm (both rooms) AER single floor (both rooms)
・ Treatment water flow rate: 50L / h
・ Concentrated water flow: 5L / h
・ Electrode water flow rate: 10L / h
・ Desalination chamber supply water (treated water): One-stage RO permeated water 6 ± 1 μS / cm
・ Concentration chamber supply water: 1 stage RO permeated water 6 ± 1 μS / cm
-Electrode chamber supply water: Desalination chamber treated water-Applied current value: 1A
About the apparatus of an Example and a comparative example, the driving | running for 1000 hours was performed and the temporal change of the treated water quality was compared. The results are shown in FIG.

  In the Examples, it was confirmed that good treated water quality was obtained and stable characteristics were exhibited regardless of the operation time. This is considered to be the effect that the movement of the ionic component from the electrode chamber to the sub-desalting chamber is suppressed.

DESCRIPTION OF SYMBOLS 1 Deionized water production apparatus 2 Frame 3 Intermediate ion exchange membrane 4 Anode 5 Cathode D, D 'Main demineralization chamber D1, D1' Main cation demineralization chamber D2, D2 'Main anion demineralization chamber S1 Sub cation demineralization chamber S2 Secondary anion desalination chamber C1 Cathode side enrichment chamber C2 Anode side enrichment chamber E1 Cathode chamber E2 Anode chamber a1 to a3 First to third anion exchange membranes c1 to c3 First to third cation exchange membranes

Claims (10)

A pair of electrode chambers, each consisting of an anode chamber and a cathode chamber, in which electrode water flows;
A main desalting chamber that is located between the pair of electrode chambers, filled with a cation exchanger and an anion exchanger, and in which treated water flows;
A cathode-side concentrating chamber located between the pair of electrode chambers, on the cathode chamber side of the main desalting chamber, and adjacent to the main desalting chamber via a first cation exchange membrane;
An anode-side concentrating chamber located between the pair of electrode chambers, on the anode chamber side of the main desalting chamber, and adjacent to the main desalting chamber via a first anion exchange membrane;
Located between the cathode chamber and the cathode side enrichment chamber, adjacent to the cathode side enrichment chamber via a second anion exchange membrane, adjacent to the cathode chamber via a third anion exchange membrane, at least A secondary anion desalting chamber filled with an anion exchanger and located between the anode chamber and the anode side concentrating chamber through which the water to be treated flows, and the anode side concentrating chamber via a second cation exchange membrane Adjacent and adjacent to the anode chamber via a third cation exchange membrane, at least one of the auxiliary cation demineralization chambers filled with at least the cation exchanger and through which the water to be treated flows, and Have
An electric deionized water production apparatus in which the inflow direction of the water to be treated flowing into the sub-desalting chamber and the electrode water flowing into the electrode chamber adjacent to the sub-desalting chamber are the same. Water to be treated is parallel to the main desalting chamber and the secondary anion desalting chamber filled with the anion exchanger , or the main desalting chamber and the secondary cation desalting chamber filled with the cation exchanger. The electric deionized water production apparatus according to claim 1, wherein the apparatus is configured to flow in and out.   The electric deionized water production apparatus according to claim 1 or 2, wherein the electrode water is treated water that has flowed out of at least one of the main demineralization chamber and the auxiliary demineralization chamber.   The electric deionized water production apparatus according to claim 3, wherein the electrode water is configured to flow in series between the cathode chamber and the anode chamber.   The electric deionized water production apparatus according to any one of claims 1 to 4, wherein a specific resistance value at an entrance of the electrode chamber of the electrode water is 0.2 MΩ · cm or more and 18.2 MΩ · cm or less. .   The main desalting chamber is adjacent to the first cation exchange membrane and filled with at least a cation exchanger, and is adjacent to the first anion exchange membrane via the intermediate ion exchange membrane. The electric deionized water production apparatus according to claim 1, further comprising a main anion demineralization chamber adjacent to the main cation demineralization chamber and filled with at least an anion exchanger. .   Either the secondary cation demineralization chamber or the secondary anion demineralization chamber is not provided, and the inflow direction of water to be treated into the main cation demineralization chamber and the treatment into the main anion demineralization chamber The electric deionized water production apparatus according to claim 6, wherein the inflow directions of water are opposite to each other. Comprising the secondary anion desalting chamber;
Two or more main desalting chambers are provided, and the main desalting chambers and the concentration chambers are alternately positioned so that the concentration chambers are located at both ends,
The electric deionized water production according to any one of claims 1 to 7, wherein the secondary anion demineralization chamber is adjacent to the concentration chamber on the most cathode side through the second anion exchange membrane. apparatus. Comprising the secondary cation desalting chamber,
Two or more main desalting chambers are provided, and the main desalting chambers and the concentration chambers are alternately positioned so that the concentration chambers are located at both ends,
The electric deionized water production according to any one of claims 1 to 7, wherein the secondary cation demineralization chamber is adjacent to the concentration chamber on the most anode side through the second cation exchange membrane. apparatus. Comprising the secondary anion desalting chamber and the secondary cation desalting chamber;
Two or more main desalting chambers are provided, and the main desalting chambers and the concentration chambers are alternately positioned so that the concentration chambers are located at both ends,
The secondary anion desalting chamber is adjacent to the concentration chamber on the most cathode side through the second anion exchange membrane, and the secondary cation desalting chamber is on the most anode side through the second cation exchange membrane. The electric deionized water production apparatus according to claim 1, which is adjacent to the concentration chamber.

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