JP2010142727A - Electric deionized water producing apparatus - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide an electric deionized water producing apparatus (EDI) capable of achieving an energy-saving ability in operation, and further obtaining deionized water of excellent quality having a high specific resistance even in treating a large amount of water. <P>SOLUTION: The EDI includes between an anode and a cathode a desalting chamber 150 having a cathode-side small desalting chamber 152 and an anode-side small desalting chamber 154 and concentrating chambers 130 on either side of the desalting chamber 150 with an anion exchange membrane 146 or a cation exchange membrane 142 in between. The anode-side small desalting chamber 154 is filled with an ion exchanger containing an anion exchanger 155 and the cathode-side small desalting chamber 152 with a mixed bed of a cation exchanger 151 and an anion exchanger containing a low-basic anion exchanger 153. A means is provided for supplying water having flowed through the cathode-side small desalting chamber 152 to the anode-side small desalting chamber 154. <P>COPYRIGHT: (C)2010,JPO&INPIT

Description

  The present invention relates to an electric deionized water production apparatus.

  As a method for producing deionized water, a method for deionizing by passing water to be treated through an ion exchange resin is conventionally known. However, in this method, when the ion exchange resin is saturated, it is necessary to regenerate with a drug. In recent years, an electric deionized water production apparatus (hereinafter referred to as EDI) that does not require regeneration with a drug has been put into practical use in order to eliminate such disadvantages in processing operations.

EDI is a pure water production apparatus that combines electrophoresis and electrodialysis. EDI is filled with an ion exchanger between an anion exchange membrane and a cation exchange membrane, an anode chamber having an anode outside the ion exchange membrane, and a cathode chamber having a cathode (hereinafter, the anode and the cathode are collectively referred to as an electrode). Device). In the method of producing deionized water by EDI, by passing water to be treated through the ion exchanger layer with a DC voltage applied to the electrodes, ion components in the water to be treated are adsorbed by the ion exchanger, and electrophoresis is performed. The ions are migrated to the membrane surface with, and electrodialyzed with an ion exchange membrane to be removed into concentrated water. In this EDI, the dissociation reaction of water proceeds due to a potential difference generated at the interface between different types of ion exchangers (hereinafter referred to as different types of ion exchanger interfaces) in the desalination chamber, and H ⁺ and OH ⁻ are generated. The ion exchanger in the desalting chamber is continuously regenerated.

Conventionally, EDI has an anionic component (Cl ⁻ , HCO ₃ ⁻ , CO ₃ ²⁻ , SiO ₂ (silica often takes a special form, so that it is displayed differently from general ions). )) And cation components (Na ⁺ , Ca ²⁺ , Mg ^2+, etc.) must be removed in one desalting chamber, so that the ion exchanger filled in the desalting chamber is an anion exchanger and a cation exchanger. It is often filled in a mixed bed form or multiple bed form. In general, it is known that when the ion exchanger in the desalting chamber is filled in a mixed bed configuration, the electrical resistance is higher than that in a single bed configuration. When the electrical resistance of the desalination chamber is high, the current value to be applied when treating water with high ionic component concentration as the treated water or when increasing the flow rate of the treated water per desalting chamber When the EDI is operated at a higher value, the operating voltage generally increases in accordance with Ohm's law (E = IR). As a result, the operation of EDI increases the power consumption represented by current × voltage, resulting in high energy.

In response to these problems, various attempts have been made to reduce the electrical resistance of EDI in order to operate EDI with energy saving. For example, it is disclosed that an anion exchanger filled in a desalted chamber in a mixed bed form can include a type II strong basic anion exchanger or a weak basic anion exchanger to reduce electrical resistance (for example, Patent Documents 1 to 3). In addition, as an anion exchanger filled in the desalination chamber in a mixed bed form, a combination of a type I strong base (strongest base) type anion exchanger and a type II strong base anion exchanger can be used at a low voltage. An invention for obtaining deionized water with good resistance and good water quality is disclosed (for example, Patent Document 4). Furthermore, an EDI having a two-salt chamber structure is disclosed that drastically improves the EDI structure, reduces the number of concentration chambers per desalting chamber to about half of the conventional one, and can significantly reduce the electrical resistance of EDI. (For example, Patent Document 5).
Special Table 2000-504273 Japanese translation of PCT publication No. 2001-5000783 Special table 2002-535128 gazette Japanese Patent No. 3895180 Japanese Patent No. 3385553

However, further energy saving during EDI operation, increased throughput, and improved deionized water quality are required. In order to save energy of EDI, even if the proportion of type II strong base anion exchanger and weak base anion exchanger in the anion exchanger packed in the desalting chamber is simply increased, type II strong base anion exchange Since a body and a weakly basic anion exchanger have a low ability to adsorb ionic components, there is a concern that the performance of removing ionic components from the water to be treated is lowered and the purity of deionized water is lowered. In addition, in order to increase the throughput per desalting chamber, increasing the flow rate of the water to be treated increases the flow differential pressure, which may cause EDI damage and the like. In order to reduce the water flow differential pressure in the desalting chamber, a method of increasing the thickness of the desalting chamber can be considered, but if the desalting chamber is thickened, there is a problem that the electrical resistance increases according to the thickness. is there.
SUMMARY OF THE INVENTION Accordingly, an object of the present invention is to provide an EDI that realizes energy saving during operation and that can obtain deionized water of good water quality with high specific resistance even by mass treatment.

  The EDI of the present invention comprises a small desorption divided by an anion exchange membrane on the anode side, a cation exchange membrane on the cathode side, and an intermediate ion exchange membrane provided between the anion exchange membrane and the cation exchange membrane. A salt chamber is filled with an ion exchanger to form a desalting chamber, a concentration chamber is provided on both sides of the desalting chamber via the anion exchange membrane or the cation exchange membrane, and the desalting chamber and the concentration chamber In the electric deionized water production apparatus in which is disposed between the cathode and the anode, the ion exchanger filled in the anode-side small desalination chamber partitioned by the anion exchange membrane and the intermediate ion exchange membrane is: An ion exchanger containing an anion exchanger and filled in the cathode-side small desalting chamber partitioned by the cation exchange membrane and the intermediate ion exchange membrane is a weakly basic anion exchanger, a medium basic anion exchanger, II Strongly basic anion exchange It is a mixed bed form of an anion exchanger containing at least one selected from the group consisting of the following (hereinafter sometimes referred to as a low basic anion exchanger) and a cation exchanger, and circulates through the cathode-side small desalting chamber Water feeding means is provided for flowing the treated water into the anode-side small desalting chamber. The total of the weakly basic anion exchanger, medium basic anion exchanger, and type II strongly basic anion exchanger contained in the anion exchanger filled in the cathode-side small desalting chamber is 50 volumes of the anion exchanger. Preferably, the ion exchanger filled in the small anode-side desalination chamber is preferably in the form of a single bed of anion exchanger, and the intermediate ion exchange membrane is an anion exchange membrane. preferable.

  According to the EDI of the present invention, deionized water with good water quality can be obtained which realizes energy saving during operation and has high specific resistance even by mass treatment.

  The principle of energy saving and water quality improvement during operation in the EDI of the present invention will be described with reference to FIG. FIG. 1 is a partial cross-sectional view of a desalting chamber 150 for explaining the flow of ion components in the EDI of the present invention. As shown in FIG. 1, the desalting chamber 150 includes a cathode side small desalting chamber 152 and an anode side small desalting chamber 154. Concentration chambers 130 are provided on both sides of the desalting chamber 150, and the desalting chamber 150 and the concentration chamber 130 are disposed between the cathode and the anode. The cathode-side small desalting chamber 152 is partitioned by a cation exchange membrane 142 and an intermediate ion exchange membrane 144, and is formed by filling a cation exchanger 151 and a low basic anion exchanger 153 in a mixed bed form. The anode-side small desalting chamber 154 is partitioned by an intermediate ion exchange membrane 144 and an anion exchange membrane 146, and an anion exchanger 155 is filled in a single bed form.

The method for producing deionized water will be described with reference to an example in which the intermediate ion exchange membrane 144 is an anion exchange membrane. First, a DC voltage is applied between the cathode and the anode, and the water to be treated A is circulated through the cathode-side small desalting chamber 152. While the water to be treated A flows through the cathode-side small desalting chamber 152, cation components such as Na ⁺ and Ca ²⁺ in the water to be treated A are adsorbed on the cation exchanger 151, and the adsorbed cation components are attracted to the cathode. Then, it passes through the cation exchange membrane 142 and moves to the concentration chamber 130. In addition, anion components such as Cl ⁻ and HCO ₃ ^— in the water to be treated A are adsorbed by the low basic anion exchanger 153. The adsorbed anion component is attracted to the anode, passes through the intermediate ion exchange membrane 144, and moves to the anode-side small desalting chamber 154. However, since the low basic anion exchanger 153 has low anion component adsorption power, the adsorbed anion component is easily desorbed and flows out of the cathode-side small desalting chamber 152 while remaining in the treated water B.

  The treated water B is caused to flow into the anode side small desalination chamber 154. The treated water B that has flowed into the anode-side small desalting chamber 154 flows while diffusing in the anion exchanger 155. During this time, the anion component in the water to be treated B is adsorbed by the anion exchanger 155 and removed. The adsorbed anion component is attracted to the anode, passes through the anion exchange membrane 144, and moves to the concentration chamber 130. In this way, the cation component is removed from the water to be treated A in the cathode-side small desalination chamber 152, the anion component is removed in the anode-side small desalination chamber 154, and becomes deionized water C. 154 flows out. During this time, the dissociation reaction of water proceeds at the heterogeneous ion exchanger interface of the desalting chamber 150.

  The low basic anion exchanger 153 is said to undergo a water dissociation reaction at a different ion exchanger interface at a lower voltage than those having a high basicity such as type I strong base (strongest base) anion exchanger. ing. Furthermore, since the cathode-side small desalting chamber 152 is in a mixed-bed form, there are many different types of ion exchanger interfaces between the cation exchanger 151 and the low basic anion exchanger 153, and the electricity in the cathode-side small desalting chamber 152 is The resistance is more greatly affected by the water dissociation reaction that occurs at the interface of the different ion exchangers. For this reason, the anion exchanger used in the cathode-side small desalting chamber 152 is a low basic anion exchanger, so that the heterogeneous ion exchanger interface is formed by the low basic anion exchanger 153 and the cation exchanger 151. The water dissociation reaction can proceed at a low voltage, and the EDI can be operated at a low voltage. As a result, energy saving can be achieved. In addition, by reducing the electrical resistance of the cathode-side small desalination chamber 152 in the mixed bed form, which causes an increase in electrical resistance, the desalination chamber increases the amount of water to be treated per desalting chamber. Even if the thickness is increased, a large amount of water to be treated can be treated at a low voltage.

  Since the low basic anion exchanger 153 has low anion component adsorption power, many anion components remain in the water to be treated B. Since the EDI of the present invention has a two-desalination chamber structure, the treated water B flowing through the cathode-side small desalting chamber 152 is treated again in the anode-side small desalting chamber 154, so that The remaining anion component can be highly removed. For this reason, deionized water C with good water quality can be obtained.

  An example of an embodiment of the present invention will be described with reference to FIG. 2, but the present invention is not limited to the following embodiment. FIG. 2 is a cross-sectional view of the EDI 10 according to the embodiment of the present invention. As shown in FIG. 2, the EDI 10 has a plurality of desalting chambers 50 sandwiched between the concentration chambers 30 between a cathode 22 and an anode 62.

  The desalting chamber 50 includes a cathode-side small desalting chamber 52 and an anode-side small desalting chamber 54. In the cathode-side small desalination chamber 52, a cation exchange membrane 42, a frame 51, and an intermediate ion exchange membrane 44 are arranged in this order from the cathode 22 side, and an opening of the frame 51 is filled with an ion exchanger. . In the anode-side small desalination chamber 54, an intermediate ion exchange membrane 44, a frame 53, and an anion exchange membrane 46 are arranged in this order from the cathode 22, and the opening of the frame 53 is filled with an ion exchanger. . Thus, the desalting chamber 50 is substantially bisected in the thickness direction by the intermediate ion exchange membrane 44. The desalting chamber 50 is adjacent to the cathode-side small desalting chamber 52 and the anode-side small desalting via the intermediate ion-exchange membrane 44. A salt chamber 54 is provided.

  A treated water inflow line 55 and a treated water outflow line 56 are connected to the cathode-side small desalination chamber 52. The treated water outflow line 56 is connected to the treated water inflow line 57 by a pipe (not shown). A treated water inflow line 57 and a deionized water outflow line 58 are connected to the anode side small desalination chamber 54. The “water supply means” includes a treated water outflow line 56, a treated water inflow line 57, and piping (not shown) that connects the treated water outflow line 56 and the treated water inflow line 57. The cathode 22 and the anode 62 are connected to a power source (not shown).

  In the cathode chamber 20, a cathode 22, a frame body 21, and a partition film 24 are sequentially arranged from the cathode 22 side. An electrode water inflow line 23 and an electrode water outflow line 25 are connected to the cathode chamber 20. In the anode chamber 60, the partition film 24, the frame body 61, and the anode 62 are sequentially arranged from the cathode 22 side. An electrode water inflow line 63 and an electrode water outflow line 65 are connected to the anode chamber 60.

  The concentration chamber 30 is formed by disposing a frame 31 on both sides of the desalting chamber 50 via a cation exchange membrane 42 or an anion exchange membrane 46. A concentrated water inflow line 33 and a concentrated water outflow line 35 are connected to the concentration chamber 30.

  Roughly classified as ion exchange membranes, a homogenous membrane formed by impregnating a raw material monomer solution into a reinforcing body and then polymerized to form a homogeneous whole, and a non-homogeneous material obtained by grinding and pulverizing together with a polyolefin resin capable of dissolving and molding the ion exchange resin There are two types of membranes. The cation exchange membrane 42 and the anion exchange membrane 46 in this embodiment are not particularly limited, and should be selected according to the suitability of EDI production, the quality of water to be treated, the quality of water required for deionized water, the amount of treatment, and the like. Can do.

  The intermediate ion exchange membrane 44 is selected in consideration of the quality of water to be treated, the water quality required for deionized water, the type of ion exchanger filled in the cathode side small desalination chamber 52 or the anode side small desalination chamber 54, and the like. be able to. The intermediate ion exchange membrane 44 may be either an anion exchange membrane or a single membrane of a cation exchange membrane, or a composite membrane in which both an anion exchange membrane and a cation exchange membrane are arranged. Among them, it is preferable to use an anion exchange membrane or a single membrane of a cation exchange membrane, or a bipolar membrane. From the viewpoint of efficiently removing an anion component in the water to be treated, a single membrane of an anion exchange membrane should be used. Is more preferable. In addition, a composite membrane means what has an area | region where an ion exchange membrane differs in polarity. For example, a mosaic film or a bipolar film can be used. The ratio of the anion exchange membrane to the cation exchange membrane in the composite membrane can be appropriately set depending on the quality of the water to be treated and the purpose of treatment.

  Examples of the ion exchanger filled in the cathode-side small desalting chamber 52 include ion exchange resins, ion exchange fibers, and monolithic porous ion exchangers. Among these, the most general use ion exchange resins are used. preferable.

  The filling form of the ion exchanger filled in the cathode-side small desalting chamber 52 is a mixed bed form of an anion exchanger and a cation exchanger. The filling ratio of the anion exchanger and the cation exchanger can be set in consideration of the quality of the water to be treated, the water quality required for deionized water, the amount of treated water, and the like. For example, anion exchanger: cation exchanger = 10 : It is preferable to set in the range of 90-80: 20 (volume ratio), and it is more preferable to set in the range of 30: 70-50: 50. This is because the cation component in the for-treatment water can be efficiently removed in the cathode-side small desalting chamber 52 within the above range. The “mixed bed form” refers to a state in which an anion exchanger and a cation exchanger are mixed and packed in an arbitrary ratio.

  The anion exchanger filled in the cathode-side small desalting chamber 52 is selected from the group consisting of weakly basic anion exchangers, low basic anion exchangers, medium basic anion exchangers, and type II strongly basic anion exchangers. It contains at least one kind. By including the low basic anion exchanger, in the cathode side small desalting chamber 52, the interface between the cation exchanger and the low basic anion exchanger, or the interface between the cation exchange membrane 42 and the low basic anion exchanger. Thus, water splitting is performed efficiently and the EDI 10 can be operated at a low voltage. The ratio of the low basic anion exchanger in the anion exchanger filled in the cathode-side small desalting chamber 52 can be set in consideration of the quality of the water to be treated, the water quality required for the deionized water, the amount of the treated water, and the like. . For example, the proportion of the low basic anion exchanger contained in the anion exchanger filled in the cathode-side small desalting chamber 52 is preferably more than 50% by volume, more preferably 70% by volume or more, and 90% by volume. % Is more preferable, and may be 100% by volume. This is because the voltage in the cathode-side small desalting chamber 52 can be greatly reduced at the above ratio.

Strongly basic anion exchanger, e.g., a quaternary ammonium base _{^{(R-N + R 1 R}} 2 R 3) anion exchanger strongly basic functional group is introduced such. A quaternary ammonium base is a group I in which the group bonded to nitrogen such as tetramethylamine is only an alkyl group (for example, a methyl group), such as trimethylaminoethanol. The case where the alkanol group (for example, —C ₂ H ₄ OH or the like) is included in Form II is referred to as Form II, and Form II has a lower adsorptive power to anionic components than Form I. Such an anion exchanger into which a type I functional group is introduced is called a type I strong base (strongest base) anion exchanger, and an anion exchanger into which a type II functional group is introduced is a type II strong basic anion. It is called an exchanger. The weakly basic anion exchanger is an anion exchanger into which a weakly basic functional group such as a primary to tertiary amine is introduced. The medium basic anion exchanger has a strong basic functional group such as a quaternary ammonium base and a weak basic functional group such as a primary to tertiary amine. An anion exchanger introduced at a ratio of 5/5 to 3/7 represented by the number of groups. The low basic anion exchanger filled in the cathode-side small desalting chamber 52 may be a weak basic anion exchanger, a medium basic anion exchanger, or a type II strong basic anion exchanger alone. Two or more kinds may be used in combination.

  Among such low basic anion exchangers, Amberlite (trade name) IRA410J, Amberlite (trade name) IRA411, Amberjet (trade name) 4010 (above, ROHM And Haas Co., Ltd.), Diaion (trade name) SA20A, Diaion (trade name) SA21A, Diaion (trade name) PA408, Diaion (trade name) PA412, Diaion (trade name) PA418 (and above, Mitsubishi) Chemical Co., Ltd.), DOWEX MARATHON (trade name) A2, DOWEX (trade name) SAR, DOWEX (trade name) MSA-2 (above, manufactured by The Dow Chemical Company), Purolite (trade name) A200, Purolite (Product Name) A300, Purolite (Product Name) A510 (above, Purolite Co., Ltd.), and the like.

  Examples of the medium basic anion exchange resin include Amberlite (trade name) IRA478RF (Rohm and Haas). As the weakly basic anion exchange resin, Amberlite (trade name) IRA67, Amberlite (trade name) IRA96SB, Amberlite (trade name) XT6050RF (above, manufactured by Rohm and Haas), Diaion (trade name) WA10 , Diaion (trade name) WA20, Diaion (trade name) WA21J, Diaion (trade name) WA30 (above, manufactured by Mitsubishi Chemical Corporation), DOWEX MARATHON (trade name) WBA, DOWEX MARATHON (trade name) WBA2, DOWEX (product name) 66 (above, manufactured by The Dow Chemical Company), Purolite (product name) A845, Purolite (product name) A847, Purolite (product name) A830, Purolite (product name) A100, Purolite ( Product name) A103S (above, manufactured by Purolite).

  The kind of cation exchanger filled in the cathode-side small desalting chamber 52 is not limited, and either a strong acid cation exchanger or a weak acid cation exchanger may be used. In addition, the cation exchanger with which the cathode side small desalting chamber 52 is filled may use a strong acid cation exchanger or a weak acid cation exchanger alone, or two or more kinds in combination.

  Among such cation exchangers, Amberlite (trade name) IR120B, Amberlite (trade name) IR124 (above, manufactured by Rohm and Haas), DOWEX MARATHON (trade name) C are used as strongly acidic cation exchange resins. (The Dow Chemical Company).

  Examples of the ion exchanger filled in the anode-side small desalting chamber 54 include ion exchange resins, ion exchange fibers, and monolithic porous ion exchangers. Among these, the most general use ion exchange resins are used. preferable.

  The ion exchanger filled in the anode side small desalting chamber 54 includes an anion exchanger. That is, the filling form of the ion exchanger filled in the anode side small desalting chamber 54 can be a single bed form of an anion exchanger or a mixed bed form of an anion exchanger and a cation exchanger. This is because the anode-side small desalting chamber 54 mainly removes anion components in the water to be treated that could not be removed by the cathode-side small desalting chamber 52. Especially, it is preferable that the filling form of the ion exchanger in the anode side small desalting chamber 54 is a single bed form of the anion exchanger. This is because by making the anode side small desalting chamber 54 a single-bed form of the anion exchanger, the movement direction of the ionic component in the anode side small desalting chamber 54 is one direction, the electrical resistance is reduced and the voltage is lowered. . When the anode-side small desalination chamber 54 is in a mixed bed configuration, the ratio of the anion exchanger to the cation exchanger can be set in consideration of the quality of the water to be treated and the water quality required for deionized water. For example, the ratio of the anion exchanger to the ion exchanger filled in the anode-side small desalting chamber 54 is preferably 50% by volume or more and less than 100% by volume, and preferably 80% by volume or more and less than 100% by volume. More preferred.

  The anion exchanger filled in the anode-side small desalting chamber 54 can be determined in consideration of the quality of the water to be treated and the quality required for the deionized water, and is an I-type strong base (strongest base) anion exchanger, Any of type II strong basic anion exchanger, medium basic anion exchanger, and weak basic anion exchanger can be used. In addition, the anion exchanger with which the anode side small desalting chamber 54 is filled may be used alone or in combination of two or more.

  Among the type I strong base (strongest base) anion exchangers, for example, Amberlite (trade name) IRA402BL, Amberjet (trade name) 4002, Amberjet (trade name) as an I-type strong base (strongest base) anion exchange resin ) 4400 (above, manufactured by Rohm and Haas), Diaion (trade name) SA10A, Diaion (trade name) SA11A, Diaion (trade name) SA12A (above, manufactured by Mitsubishi Chemical Corporation), DOWEX MARATHON ( Product name) A (made by The Dow Chemical Company), Purolite (product name) A400 (made by Purolite), and the like.

  The kind of cation exchanger filled in the anode-side small desalting chamber 54 is not limited, and either a strong acid cation exchanger or a weak acid cation exchanger may be used. In addition, the cation exchanger with which the anode side small desalting chamber 54 is filled may be used alone or in combination of two or more.

The frames 51 and 53 are not particularly limited as long as they have insulating properties and do not leak water to be treated. For example, frames made of resin such as polyethylene, polypropylene, polyvinyl chloride, ABS, polycarbonate, noryl, etc. Can be mentioned.
The thicknesses of the frames 51 and 53 are not particularly limited, and can be set according to the desired thicknesses of the cathode-side small desalting chamber 52 and the anode-side small desalting chamber 54. Moreover, when the area of the opening part of the frame bodies 51 and 53 is large, you may provide a support body in the space where the frame bodies 51 and 53 were hollowed out. By providing the support, it is possible to prevent the cation exchange membrane 42, the intermediate ion exchange membrane 44, and the anion exchange membrane 46 from being curved and the ion exchanger filling amount from becoming uneven. The support is not particularly limited as long as it is a material that has insulating properties and does not hinder the flow of water to be treated. For example, polyethylene, polypropylene, polyvinyl chloride, ABS, polycarbonate, noryl, etc., provided with slits. The resin-made support body can be mentioned.

The thickness of the cathode-side small desalting chamber 52 can be set in consideration of the quality of the water to be treated and deionized water, the amount of treated water, and the type of ion exchanger to be filled. It is preferable to set, and it is more preferable to set it as 3-30 mm. If the thickness of the cathode-side small desalting chamber 52 is too thin, the differential pressure increases due to an increase in the water flow rate (LV), causing damage to the cathode-side small desalting chamber 52 and causing operational difficulties. Absent. If the thickness of the cathode-side small desalting chamber 52 is too thick, the electric resistance increases. Here, since the cathode-side small desalting chamber 52 has a mixed bed configuration including a low basic anion exchanger, the electrical resistance is lower than that of the conventional mixed bed configuration. For this reason, in order to increase the flow rate of the water to be treated per one small desalting chamber, the thickness of the cathode-side small desalting chamber 52 can be made thicker than that of the conventional EDI. Note that LV is a flow rate per unit area and is a linear velocity expressed in m / h (the same applies hereinafter).
The thickness of the anode-side small desalting chamber 54 is set in consideration of the quality of the water to be treated and deionized water, the amount of treated water, and the type of ion exchanger to be filled, like the thickness of the cathode-side small desalting chamber 52. can do.

  The concentration chamber 30 is not particularly limited as long as concentrated water can be circulated. For example, the opening of the frame 31 has a mesh made of resin such as polyethylene, polypropylene, polyvinyl chloride, ABS, polycarbonate, noryl, and water permeability. It is possible to install a grid-like frame member, to fill the ion exchanger, or to dispose nothing. From the viewpoint of reducing electrical resistance, it is preferable that the ion exchanger is filled. In the case of filling the concentration chamber 30 with an ion exchanger, examples of the ion exchanger to be filled include an ion exchange resin, an ion exchange fiber, a monolithic porous ion exchanger, and the like. It is preferable to use a resin.

  The filling form of the ion exchanger in the concentrating chamber 30 is not particularly limited and can be determined in consideration of the quality of the water to be treated. The anion exchanger single bed form, the cation exchanger single bed form, or the anion exchange Any of the mixed bed form of the body and the cation exchanger, or the multiple bed form can be used. For example, from the viewpoint of preventing scale formation on the anion exchange membrane 46 surface of the concentration chamber 30, the anion exchanger may be filled in a single bed form. By providing the anion exchanger layer in contact with the anion exchange membrane 46, the movement of the anion component from the anode side small desalting chamber 54 to the concentration chamber 30 is promoted, and the anion component is present on the surface of the anion exchange membrane 46 on the concentration chamber 30 side. This is because the presence of a high concentration can suppress the occurrence of concentration polarization.

  The material of the frame 31 is the same as that of the frame 51. The thickness of the frame 31 can be set according to the desired thickness of the concentration chamber 30. The thickness of the concentration chamber 30 can be set in consideration of the quality of water to be treated and the quality of water required for deionized water. For example, the thickness is preferably in the range of 2 to 20 mm.

  The cathode chamber 20 only needs to have a structure in which electrode water can flow. For example, a resin mesh such as polyethylene, polypropylene, polyvinyl chloride, ABS, polycarbonate, noryl, or a grid-like frame material having water permeability may be installed in the opening of the frame body 21, The exchanger may be filled. When the cathode chamber 20 is filled with an ion exchanger, examples of the ion exchanger to be filled include an ion exchange resin, an ion exchange fiber, a monolithic porous ion exchanger, and the like. It is preferable to use a resin. Similarly to the cathode chamber 20, the anode chamber 60 may have a structure in which electrode water can flow.

  The form of filling the ion exchanger in the cathode chamber 20 is not particularly limited, and can be determined in consideration of the quality of the water to be treated. The anion exchanger single bed form, the cation exchanger single bed form, or the anion exchange Any of the mixed bed form of the body and the cation exchanger, or the multiple bed form can be used. The filling form of the ion exchanger in the anode chamber 60 is the same as the filling form of the ion exchanger in the cathode chamber 20.

The cathode 22 is not particularly limited as long as it functions as a cathode. For example, a plate-like stainless steel, a mesh-like stainless steel, or a noble metal such as platinum, palladium, iridium, or the noble metal is covered with titanium or the like. And a net-like or plate-like electrode. The anode 62 is not particularly limited as long as it functions as an anode. However, when Cl ⁻ is present in the electrode water, chlorine is generated in the anode, so that the anode 62 has chlorine resistance. For example, a noble metal such as platinum, palladium, iridium, or a net-like or plate-like electrode obtained by coating the noble metal on titanium or the like can be given.

  The partition membrane 24 is not particularly limited as long as it is an ion exchange membrane, and can be selected in consideration of the quality of the water to be treated, the operating conditions of the EDI 10, and the like. For example, a cation exchange membrane or an anion exchange membrane can be selected.

  The material of the frame body 21 is the same as that of the frame body 51. The thickness of the frame 21 can be set according to the desired thickness of the cathode chamber 20. The material of the frame body 61 is the same as that of the frame body 51. The thickness of the frame 61 can be set according to the desired thickness of the anode chamber 60.

  A method for producing deionized water using EDI 10 will be described with reference to FIG. First, electrode water is caused to flow into the cathode chamber 20 from the electrode water inflow line 23, and electrode water is caused to flow into the anode chamber 60 from the electrode water inflow line 63. The concentrated water is caused to flow into the concentration chamber 30 from the concentrated water inflow line 33. Then, a DC voltage is applied between the cathode 22 and the anode 62.

The treated water is caused to flow from the treated water inflow line 55 to the cathode side small desalination chamber 52. The treated water that has flowed in flows through the ion exchanger inside the cathode-side small desalting chamber 52 while diffusing, and flows out from the treated water outflow line 56. During this time, cation components such as Na ⁺ and Ca ^{2+ in the} water to be treated are adsorbed on the cation exchanger, and anion components such as Cl ⁻ and HCO ₃ ⁻ are adsorbed on the anion exchanger. At the same time, OH ⁻ and H ⁺ are generated by water splitting at the heterogeneous ion exchanger interface. The cation exchanger is regenerated by exchanging the generated H ⁺ and the cation component adsorbed on the cation exchanger. The cation component desorbed from the cation exchanger passes through the cation exchange membrane 42 and moves to the concentration chamber 30. The cation component moved to the concentration chamber 30 is taken into the concentrated water and discharged from the concentrated water outflow line 35.

The anion exchanger is regenerated by exchanging the produced OH ⁻ and the anion component adsorbed on the anion exchanger. Then, the anion component desorbed from the anion exchanger moves to the intermediate ion exchange membrane 44 side. Here, when the intermediate ion exchange membrane 44 is an anion exchange membrane, the anion component desorbed from the anion exchanger and the OH ⁻ produced in the cathode-side small desalting chamber 52 are attracted to the anode 62, and the intermediate ion exchange is performed. It passes through the membrane 44 and moves to the anode side small desalting chamber 54. In the case where the intermediate ion exchange membrane 44 is a cation exchange membrane or a bipolar membrane, the anion component desorbed from the anion exchanger and OH ⁻ are repelled by the intermediate ion exchange membrane 44 and from the treated water outflow line 56 together with the treated water. leak.

The treated water that has flowed out of the treated water outflow line 56 flows into the anode-side small desalination chamber 54 through a pipe (not shown) and the treated water inflow line 57 in order. The treated water that has flowed into the anode-side small desalting chamber 54 flows while diffusing through the ion exchanger in the anode-side small desalting chamber 54. During this time, the anion component in the water to be treated is adsorbed by the anion exchanger. The anion exchanger is regenerated by exchanging the adsorbed anion component and OH ⁻ . The anion component desorbed from the anion exchanger is attracted to the anode 62, passes through the anion exchange membrane 46, and moves to the concentration chamber 30. The anion component moved to the concentration chamber 30 is taken into the concentrated water and discharged from the concentrated water outflow line 35. Here, when the intermediate ion exchange membrane 44 is a cation exchange membrane, the cation component and H ⁺ in the anode side small desalting chamber 54 are attracted to the cathode 22 and permeate the intermediate ion exchange membrane 44 to pass through the cathode side. Move to small desalination chamber 52. In this way, the cation component and the anion component are highly removed from the water to be treated, and deionized water flows out from the deionized water outflow line 58.

The electrode water that has flowed into the cathode chamber 20 from the electrode water inflow line 23 flows through the cathode chamber 20 in an upward flow. During this time, the electrode water takes in H _{2 and the} like generated from the cathode 22 and flows out from the electrode water outflow line 25. The electrode water flowing into the anode chamber 60 from the electrode water inflow line 63 flows in the anode chamber 60 in an upward flow. During this time, the electrode water takes in Cl ₂ , O _{2 and the} like generated from the anode 62 and flows out from the electrode water outflow line 65.

  Although the to-be-processed water is not specifically limited, The water etc. which processed the water which removed the turbid component of industrial water and well water with the turbidity membrane with the reverse osmosis (RO) membrane, etc. are mentioned.

The amount of water to be treated in the cathode-side small desalination chamber 52 is not particularly limited, taking into consideration the proportion of the low basic anion exchanger in the ion exchanger to be filled, the quality of the water to be treated, and the like. Can be determined. The amount of water flow is represented by space velocity (SV), and the unit of SV is represented by L / L · h ⁻¹ , which is a flow rate (L) circulated in one hour with respect to the unit volume (L) of the ion exchanger. (The same applies hereinafter). In general, when SV is too large, in the cathode-side small desalting chamber 52, the contact time between the ion component in the water to be treated and the ion exchanger is shortened, and the ion removal performance may be deteriorated. However, the cathode-side small desalting chamber 52 is a mixed bed form containing a low basic anion exchanger and has a low electric resistance. For this reason, in the cathode-side small desalting chamber 52, a large amount of water to be treated can be treated with a high current even at a voltage equivalent to that of the desalting chamber in a mixed bed configuration not including a low basic anion exchanger. The amount of water to be treated in the cathode-side small desalination chamber 52 is preferably set in the range of SV = 100 to 1000 L / L · h ⁻¹ . The amount of water to be treated in the anode-side small desalination chamber 54 is the same as the amount of water to be treated in the cathode-side small desalination chamber 52.

  The flow rate of the concentrated water in the concentration chamber 30 is not particularly limited, and can be determined in consideration of the ability of the EDI 10, the quality of the water to be treated, and the amount to be treated. The concentrated water has the purpose of diffusing ions that have moved to the concentration chamber 30 into the concentrated water and flowing out of the EDI 10. Therefore, the flow rate of the concentrated water is preferably determined by the relationship between the flow rate of the water to be treated, the ion concentration of the water to be treated, and the production amount of the deionized water. It is preferable to determine the flow rate of the concentrated water so that the concentration ratio is 3 to 20. The concentration ratio according to the following equation (1) is defined on the assumption that the same raw water is used for the treated water and the concentrated water, and all the ions in the desalting chamber 50 are transferred to the concentration chamber 30.

  If the flow rate of the concentrated water is too small, the concentration diffusion of the ion component transferred to the concentration chamber 30 becomes uneven, the concentration polarization layer on the surface of the ion exchange membrane becomes thick, and scale may be generated. On the other hand, if the flow rate of concentrated water is too large, the recovery rate of deionized water is not preferable. The raw water used for the concentrated water is not particularly limited, and water from the same water source as the water to be treated may be used as the raw water for the concentrated water, or deionized water or pure water may be used.

The raw water of the electrode water circulated in the cathode chamber 20 is not particularly limited, and water from the same water source as the water to be treated may be used as the electrode water, or the deionized water treated in the desalting chamber 50 and the specific resistance value. 0.2 to 18.2 MΩ · cm of water may be used as electrode water. Among these, deionized water treated in the desalting chamber 50 and water having a specific resistance value of 0.2 to 18.2 MΩ · cm are preferable. The raw water of the electrode water in the anode chamber 60 is the same as the raw water of the electrode water in the cathode chamber 20. The flow rate of the electrode water in the cathode chamber 20 and the anode chamber 60 is not particularly limited, and is preferably determined according to the applied voltage or the like. If the flow rate of the electrode water is too small, it will be difficult to sufficiently discharge the generated H ₂ , O ₂ , and Cl ₂ gases, and if the flow rate of the electrode water is too large, the recovery rate is lowered, which is not preferable.

  The distribution method of the electrode water is not particularly limited. For example, the electrode water that has circulated through the cathode chamber 20 may be circulated to the anode chamber 60, or the electrode water that has circulated through the anode chamber 60 may be circulated to the cathode chamber 20. Good. Further, for example, the electrode water may be separately circulated through the cathode chamber 20 and the anode chamber 60 and drained.

The current applied to the cathode 22 and the anode 62 is set in consideration of the quality of the water to be treated and the type and filling form of the ion exchanger filled in the cathode side small desalination chamber 52 and the anode side small desalination chamber 54. be able to. For example, it is preferable to set the electric current density per area of an effective ion-exchange membrane of the desalting chamber 50 in the range of 0.1 to 10 A / dm ^2. The “area of the effective ion exchange membrane” in the desalting chamber 50 is a portion through which an electric current is passed. The cathode-side small desalting chamber 52 will be described as an example. The area of the cation exchange membrane 42 is excluded from the area of contact with the frame 51.

  As described above, since the EDI of the present invention has a two-desalination chamber structure, the number of concentrating chambers per small desalting chamber is approximately the same as the number of concentrating chambers per one desalting chamber of EDI in the desalination chamber structure. Halved. For this reason, the electrical resistance of the whole EDI can be reduced, the electrical conductivity can be improved, and the electrical resistance of the whole EDI can be reduced. The cathode-side small desalting chamber is filled with ion exchangers in a mixed bed form, but the electrical resistance is low because the anion exchanger includes a low basic anion exchanger. In addition, water splitting is efficiently performed at the interface between the low basic anion exchanger and the cation exchanger. For this reason, even if the applied current value is increased, the EDI can be operated at a low voltage. If the EDI is operated in a state where the voltage is high, the member may be deteriorated due to heat generation at the interface of the different ion exchangers, and the processing capacity of the EDI may be reduced. In particular, when the cation exchange membrane, the anion exchange membrane, or the intermediate ion exchange membrane deteriorates and is damaged, the ion component leaks between the desalting chamber and the concentration chamber, and the quality of the deionized water is lowered. In the EDI of the present invention, since the EDI can be operated at a low voltage, member deterioration due to heat generation at the interface of the different ion exchanger can be suppressed.

  The low basic anion exchanger filled in the cathode-side small desalting chamber has a low adsorptive power to the anion component, and thus the anion component often remains in the water treated by flowing through the cathode-side small desalting chamber. . In the EDI of the present invention, the water treated in the cathode-side small desalting chamber is contacted with the anion exchanger filled in the anode-side small desalting chamber and treated again to highly remove the anion component in the water to be treated. be able to. In addition, the cationic component in the water to be treated can be highly removed in the cathode-side small desalting chamber provided on the cathode side. As a result, by treating the water treated in the cathode-side small desalting chamber in the anode-side small desalting chamber, the cation component and the anion component are highly removed, and deionized water with good water quality having high specific resistance is obtained. Obtainable.

  The proportion of the low basic anion exchanger contained in the anion exchanger filled in the cathode-side small desalting chamber is preferably more than 50% by volume, more preferably 70% by volume or more, and further preferably 90% by volume or more. Thus, the efficiency of water splitting at the interface of the different ion exchangers can be increased even at a low voltage. Furthermore, the electric resistance of an anode side small desalination chamber can be reduced by making the ion exchanger with which an anode side small desalination chamber is filled into the single bed form of an anion exchanger. For this reason, the electrical resistance of the entire desalting chamber can be reduced, and a high current can be passed at a lower voltage. As a result, the amount of treatment per desalting chamber can be increased, the desalting chamber can be thickened, and good water quality can be maintained while suppressing an increase in the water flow differential pressure in the desalting chamber.

The present invention is not limited to the above-described embodiment.
In the above-described embodiment, the water to be treated is circulated in a downward flow in both the cathode-side small desalination chamber and the anode-side small desalination chamber. Alternatively, the flow direction may be different between the cathode-side small desalting chamber and the anode-side small desalting chamber.

  In the above-described embodiment, the concentrated water is circulated in a downward flow, but the flow direction of the concentrated water may be an upward flow or may be different for each concentration chamber. In the above-described embodiment, the electrode water is circulated in an upward flow, but the flow direction of the electrode water may be a downward flow, or may be different between the cathode chamber and the anode chamber.

  In the above-described embodiment, three desalting chambers are arranged between the cathode and the anode. However, the present invention is not limited to this, and the number of desalting chambers may be one or two. It may be four or more.

  In the above-described embodiment, the concentration chambers adjacent to each other through the partition film forming the cathode chamber are provided. However, the concentration chamber may be omitted, and the cathode chamber may also serve as the concentration chamber. Similarly, the adjacent concentrating chamber may be omitted through the partition film forming the anode chamber, and the anode chamber may also serve as the concentrating chamber.

EXAMPLES Hereinafter, although an Example is given and this invention is demonstrated concretely, it is not limited to an Example.
(Measuring method)
<Water quality evaluation: conductivity, specific resistance>
For water quality evaluation, conductivity and specific resistance were used. In the case of water containing no impurities, the theoretical value of conductivity in water at 25 ° C. is 0.055 μS / cm, and the theoretical value of specific resistance is 18.2 MΩ · cm. As for the water quality of deionized water, the specific resistance approaches 18.2 MΩ · cm, and the higher, the higher the water quality. Deionized water quality was evaluated with specific resistance.
The conductivity was measured using a conductivity meter (873CC, manufactured by FOXBORO). The specific resistance was measured using a specific resistance meter (873RS, manufactured by FOXBORO).

Example 1
3 is an intermediate ion exchange membrane similar to the EDI 10 shown in FIG. 2, and is provided with three desalting chambers divided into a cathode-side small desalting chamber and an anode-side small desalting chamber. EDI-A was obtained by preparing EDI in which a concentration chamber was provided, and a desalting chamber and a concentration chamber were disposed between the cathode and the anode according to the following specifications. In the obtained EDI-A, the proportion of the low basic anion exchanger in the anion exchanger filled in the cathode-side small desalting chamber is 100% by volume. This EDI-A was continuously operated under the following operating conditions. The water to be treated was circulated in a downward flow to the cathode-side small desalination chamber and then circulated in a downward flow to the anode-side small desalination chamber. Concentrated water was circulated and discharged to each concentrating chamber in a downward flow, and electrode water was circulated and discharged to the cathode chamber and the anode chamber respectively. After starting the operation, the operating voltage, the electrical resistance between the electrodes, and the specific resistance of deionized water were measured every 200 hours, and the results are shown in Table 1 and FIGS.

<EDI specifications>
(1) Cation exchange membrane: manufactured by Astom Co., Ltd. (2) Intermediate ion exchange membrane: manufactured by Astom Co., Ltd., anion exchange membrane (3) Anion exchange membrane: manufactured by Astom Co., Ltd. (4) Partition membrane: Partition membrane of cathode chamber; Astom Co., Ltd., anion exchange membrane, partition membrane of anode chamber; Astom Co., Ltd., cation exchange membrane (5) Cathode-side small desalination chamber: height 300 mm, width 80 mm, thickness 5 mm
(6) Anode-side small desalination chamber: height 300 mm, width 80 mm, thickness 5 mm
(7) Cathode-side small desalination chamber filled ion exchanger: type II strongly basic anion exchange resin (Rohm and Haas) 50% by volume, strongly acidic cation exchange resin (Rohm and Haas) 50% by volume mixed bed form (8) Packed ion exchanger in anode side small desalination chamber: Single bed form of type I strong base (strongest base) anion exchange resin (Rohm and Haas) (9) Concentration chamber: height 300mm, width 80mm, thickness 4mm
(10) Filling ion exchanger in the concentration chamber: single-floor form of type I strong base (strongest base) anion exchange resin (Rohm and Haas) (11) Cathode chamber: height 300 mm, width 80 mm, thickness 4mm
(12) Filling ion exchanger in cathode chamber: single-floor form of type I strong base (strongest base) anion exchange resin (13) Anode chamber: height 300 mm, width 80 mm, thickness 4 mm
(14) Filling ion exchanger in the anode chamber: single bed form of strongly acidic cation exchange resin

<Operating conditions>
(1) Conductivity of water to be treated: 10 to 15 μS / cm (RO membrane permeate)
(2) Specific resistance of water to be treated: 0.066 to 0.1 MΩ · cm
(3) Processed water flow rate: 72 L / h (24 L / h per desalting chamber)
(4) Cathode-side small desalination chamber SV: 200 L / L · h ⁻¹
(5) Anode-side small desalination chamber SV: 200 L / L · h ⁻¹
(6) Conductivity of concentrated water: 10-15 μS / cm (RO membrane permeate)
(7) Concentrated water flow rate: 8 L / h
(8) Specific resistance of raw water of electrode water: Water whose specific resistance exceeds 5 MΩ · cm (9) Flow rate of electrode water: 10 L / h
(10) Operating current value: 1A
(11) Current density: 0.42 A / dm ²

(Example 2)
Filled ion exchanger in the cathode side small desalting chamber is 22.5% by volume of type I strong base (strongest base) anion exchange resin (Rohm & Haas), type II strong base anion exchange resin (Rohm EDI-, with the same specifications as EDI-A, except that the mixed-bed form was 27.5% by volume and made by strong acid cation exchange resin (Rohm and Haas) 50% by volume. B was obtained. The EDI-B thus obtained has a low basic anion exchanger ratio of 55% by volume in the anion exchanger filled in the cathode-side small desalting chamber. Using this EDI-B, continuous operation was performed under the same operation conditions as in Example 1. The operating voltage, the electrical resistance between the electrodes, and the specific resistance of deionized water were measured every 200 hours, and the results are shown in Table 1 and FIGS.

The EDI having a single desalination chamber structure used in Comparative Examples 1 and 2 will be described with reference to FIG.
FIG. 6 is a cross-sectional view of EDI 900. In the EDI 900, between a cathode chamber 920 and an anode chamber 960, three desalting chambers 950 and concentration chambers 930 provided on both sides of the desalting chamber 950 are arranged. The cathode chamber 920 includes a cathode 922, a frame body 921, and a partition film 924 arranged in this order from the cathode 922 side. In the anode chamber 960, a partition film 924, a frame body 961, and an anode 962 are sequentially arranged from the cathode 922 side. An electrode water inflow line 923 and an electrode water outflow line 925 are connected to the cathode chamber 920, and an electrode water inflow line 963 and an electrode water outflow line 965 are connected to the anode chamber 960.

  In the desalting chamber 950, a cation exchange membrane 942, a frame body 951, and an anion exchange membrane 946 are arranged in this order from the cathode 922 side, and an opening of the frame body 951 is filled with the ion exchanger. A treated water inflow line 955 and a deionized water outflow line 958 are connected to the desalting chamber 950. The concentration chamber 930 is formed by disposing a frame body 931 on both sides of the desalting chamber 950. A concentrated water inflow line 933 and a concentrated water outflow line 935 are connected to the concentration chamber 930.

(Comparative Example 1)
EDI similar to EDI900 was prepared by arranging three desalting chambers with the following specifications to obtain EDI-C. Using EDI-C, continuous operation was performed under the same operating conditions as in Example 1 except that the space velocity of the water to be treated in the desalting chamber was set to SV = 200 L / L · h ⁻¹ . During operation, the water to be treated was circulated in the desalting chamber in a downward flow to obtain deionized water. Concentrated water was circulated and drained to each concentrating chamber in a downward flow, and electrode water was circulated and drained to the cathode chamber and the anode chamber, respectively. After starting the operation, the operating voltage, the electrical resistance between the electrodes, and the specific resistance of deionized water were measured every 200 hours, and the results are shown in Table 1 and FIGS.

<EDI specifications>
(1) Cation exchange membrane: manufactured by Astom Co., Ltd. (2) Anion exchange membrane: manufactured by Astom Co., Ltd. (3) Partition membrane: Partition membrane of cathode chamber; Astom Co., Ltd., anion exchange membrane, partition membrane of anode chamber; Stock Cation exchange membrane manufactured by Astom Co., Ltd. (4) Desalination chamber: height 300mm, width 80mm, thickness 5mm
(5) Deionization chamber filled ion exchanger: Form I strong base (strongest base) anion exchange resin (Rohm and Haas) 50% by volume, strongly acidic cation exchange resin (Rohm and Haas) ) 50% by volume mixed bed form (6) Concentration chamber: height 300mm, width 80mm, thickness 4mm
(7) Packing ion exchanger in the concentration chamber: single-floor form of type I strong base (strongest base) anion exchange resin (Rohm and Haas) (8) Cathode chamber: height 300 mm, width 80 mm, thickness 4mm
(9) Filling ion exchanger in cathode chamber: single-floor form of type I strong base (strongest base) anion exchange resin (10) Anode chamber: height 300 mm, width 80 mm, thickness 4 mm
(11) Filling ion exchanger in the anode chamber: single bed form of strongly acidic cation exchange resin

(Comparative Example 2)
The packed ion exchanger in the desalting chamber is a mixed bed of 50% by volume of type II strongly basic anion exchange resin (Rohm and Haas) and 50% by volume of strongly acidic cation exchange resin (Rohm and Haas). EDI-D was obtained with the same specifications as EDI-C except that the form was adopted. Using EDI-D, continuous operation was performed under the same operation conditions as in Comparative Example 1. The operating voltage, the electrical resistance between the electrodes, and the specific resistance of deionized water were measured every 200 hours, and the results are shown in Table 1 and FIGS.

  As shown in Table 1, in Example 1, the operating voltage 1000 hours after the start of operation was 12.65V, and the increase in the operating voltage 200 to 1000 hours after the start of operation was 2.48V. In Example 2, the operation voltage 1000 hours after the start of operation was 18.90 V, and the increase in the operation voltage 200 to 1000 hours after the start of operation was 5.40 V. In Comparative Example 2, the operating voltage 1000 hours after the start of operation was 11.72 V, and the voltage increase from 200 to 1000 hours after the start of operation was 2.39 V. On the other hand, in Comparative Example 1, the operating voltage 1000 hours after the start of operation exceeds 23 V, which is 1.8 times or more that of Example 1 or Comparative Example 2 and about 1.2 times that of Example 2. It was. In addition, in Comparative Example 1, the increase in operating voltage in 200 to 1000 hours after the start of operation is about 7.5 V, about 3 times that of Example 1 or Comparative Example 2, and about 1.4 times that of Example 2. there were. Therefore, when the low basic anion exchanger is included in the anion exchanger packed as a mixed bed form, it is lower than the case where only the type I strong base (strongest base) anion exchanger is included. It was found that operation with voltage can be performed stably.

FIG. 3 is a graph showing the relationship between EDI operating time and electrical resistance, with the operating time on the horizontal axis and the electrical resistance on the vertical axis. Legend (a) shows the results in Example 1, Legend (b) shows the results in Example 2, Legend (c) shows the results in Comparative Example 1, and Legend (d) shows the results in Comparative Example 2, respectively.
As shown in Table 1 and FIG. 3, in 200 to 1000 hours after the start of operation, the electrical resistance changed at 10.17 to 12.71Ω in Example 1, and at 13.50 to 18.90Ω in Example 2. In Comparative Example 2, the transition was from 9.33 to 11.74Ω. On the other hand, Comparative Example 1 had a high level of 15.71 to 23.23Ω. This result confirms that the operating voltages of Examples 1 and 2 and Comparative Example 2 are lower than those of Comparative Example 1.

FIG. 4 is a graph showing the relationship between the operation time of EDI and the specific resistance of deionized water, with the operation time on the horizontal axis and the specific resistance on the vertical axis. Legend (a) shows the results in Example 1, Legend (b) shows the results in Example 2, Legend (c) shows the results in Comparative Example 1, and Legend (d) shows the results in Comparative Example 2, respectively.
As shown in Table 1 and FIG. 4, in Example 1, the specific resistance of deionized water 1000 hours after the start of operation is 18.12 MΩ · cm, and the specific resistance of deionized water 200 to 1000 hours after the start of operation is 17.42-18.19 MΩ · cm. In Example 2, the specific resistance of deionized water 1000 hours after the start of operation is 17.20 MΩ · cm, and the specific resistance of deionized water 200 to 1000 hours after the start of operation is 17.20 to 18.00 MΩ · cm. Met. On the other hand, in Comparative Example 1, the specific resistance of deionized water 1000 hours after the start of operation is 2.20 MΩ · cm, and in Comparative Example 2, the specific resistance of deionized water 1000 hours after the start of operation is 2.03 MΩ · cm. cm. From these results, as shown in FIG. 4, a cathode-side small desalting chamber filled with an ion exchanger containing a type II strong basic anion exchange resin in a mixed bed form, and a type I strong base (strongest base) anion It was found that EDI-A, in which treated water is circulated in the order of the anode-side small desalination chamber filled with the exchange resin in a single bed form, can stably produce deionized water with extremely high water quality.

(Example 3)
Using EDI-A produced in Example 1, EDI-A was continuously operated in the same manner as in Example 1. The operating voltage, electric resistance, and specific resistance of deionized water 600 hours after the start of operation were measured, and the results are shown in Table 2.

Example 4
Processed water flow rate is 216 L / h (72 L / h per desalting chamber, cathode side small desalting chamber SV = 600 L / L · h ⁻¹ , anode side small desalting chamber SV = 600 L / L · h ⁻¹ ), EDI-A was continuously operated in the same manner as in Example 3 except that the flow rate of concentrated water was 24 L / h, the applied current was 3 A, and the current density was 1.25 A / dm ² . The operating voltage, electric resistance, and specific resistance of deionized water 600 hours after the start of operation were measured, and the results are shown in Table 2.

(Example 5)
Processed water flow rate is 288 L / h (96 L / h per desalination chamber, cathode side small desalination chamber SV = 800 L / L · h ⁻¹ , anode side small desalination chamber SV = 800 L / L · h ⁻¹ ), EDI-A was continuously operated in the same manner as in Example 3 except that the flow rate of concentrated water was 32 L / h, the applied current was 4 A, and the current density was 1.67 A / dm ² . The operating voltage, electric resistance, and specific resistance of deionized water 600 hours after the start of operation were measured, and the results are shown in Table 2.

FIG. 5 shows the relationship between the space velocity (SV) of treated water and the specific resistance of deionized water in the cathode side small desalination chamber and anode side small desalination chamber 600 hours after the start of operation, and the cathode side small desalting chamber. It is a graph showing the relationship between the space velocity (SV) of the to-be-processed water in a salt chamber and an anode side small desalination chamber, and the electrical resistance of EDI. Legend (e) shows the specific resistance of deionized water, and legend (f) shows the electrical resistance of EDI-A.
As shown in Table 2 and the results of Example 5 in FIG. 5, EDI-A passes 4 times the amount of treated water (SV = 800 L / L · h ^{−1 in the} small desalination chamber) of Example 3; Even with water, the deionized water maintained a good water quality of 11 MΩ · cm. Here, in Comparative Example 1 in which the amount of water to be treated in the demineralization chamber was operated at SV = 200 L / L · h ⁻¹ , the specific resistance of deionized water 600 hours after the start of operation was 1.98 MΩ · cm. Considering the fact (see Table 1), the EDI-A of the present invention is superior to the EDI of the desalination chamber type even if the SV of the water to be treated is increased, that is, the water flow rate is increased. It was found that deionized water with high specific resistance and good water quality can be obtained.

  In addition, since the electrical resistance of Example 5 was 18.2Ω and the electrical resistance after 600 hours of operation of Comparative Example 1 was 20.61Ω (see Table 1), EDI-A of the present invention was It was found that even if the flow rate of the water to be treated was increased, deionized water with good water quality could be obtained efficiently at a low voltage.

It is a fragmentary sectional view of the desalination chamber explaining the flow of the ion component in EDI of the present invention. It is sectional drawing of EDI which is an example of embodiment of this invention. It is a graph which shows the relationship between the operating time of EDI and the electrical resistance in Examples 1 and 2 and Comparative Examples 1 and 2. It is a graph which shows the relationship between the operation time of EDI and the specific resistance of deionized water in Examples 1 and 2 and Comparative Examples 1 and 2. It is a graph which shows the relationship between the water flow rate of to-be-processed water and the specific resistance of deionized water in Examples 3-5, and the relationship between the water flow rate of to-be-processed water and the electrical resistance of EDI. It is sectional drawing of EDI used for the comparative example.

Explanation of symbols

10,900 Electric deionized water production apparatus 22,922 Cathode 30,130,930 Concentration chamber 42,142,942 Cation exchange membrane 44,144 Intermediate ion exchange membrane 46,146,946 Anion exchange membrane 50,150,950 Desorption Salt chamber 52, 152 Cathode side small desalination chamber 54, 154 Anode side small desalination chamber 56 Untreated water outflow line 57 Untreated water inflow line 62, 962 Anode 151 Cation exchanger 153 Low basic anion exchanger 155 Anion exchange body

Claims (4)

An ion exchanger in a small desalting chamber partitioned by an anion exchange membrane on the anode side, a cation exchange membrane on the cathode side, and an intermediate ion exchange membrane provided between the anion exchange membrane and the cation exchange membrane And a concentrating chamber is provided on both sides of the desalting chamber via the anion exchange membrane or the cation exchange membrane, and the desalting chamber and the concentrating chamber include a cathode and an anode. In the electric deionized water production apparatus arranged between
The ion exchanger filled in the anode-side small desalting chamber partitioned by the anion exchange membrane and the intermediate ion exchange membrane includes an anion exchanger,
The ion exchanger filled in the cathode-side small desalting chamber partitioned by the cation exchange membrane and the intermediate ion exchange membrane is a weakly basic anion exchanger, a medium basic anion exchanger, or a type II strong basic anion exchange. It is a mixed bed form of an anion exchanger containing at least one selected from the group consisting of bodies and a cation exchanger,
An electrical deionized water production apparatus, characterized in that water supply means is provided for flowing water flowing through the cathode-side small desalting chamber to the anode-side small desalting chamber.   The total of the weakly basic anion exchanger, medium basic anion exchanger, and type II strongly basic anion exchanger contained in the anion exchanger filled in the cathode-side small desalting chamber is 50 volumes of the anion exchanger. The electrical deionized water production apparatus according to claim 1, wherein the percentage exceeds%.   The electric deionized water production apparatus according to claim 1 or 2, wherein the ion exchanger filled in the anode-side small demineralization chamber is a single-bed form of an anion exchanger.   The electric deionized water production apparatus according to any one of claims 1 to 3, wherein the intermediate ion exchange membrane is an anion exchange membrane.

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