JP3090841B2 - Electric deionized water production equipment - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

The present invention is used in various industries such as semiconductor manufacturing industry, pharmaceutical industry, food industry, etc. using deionized water, in power plants (condensation treatment, makeup water treatment, etc.), in laboratories, etc. The present invention relates to an electric deionized water production device.

[0002]

2. Description of the Related Art As an apparatus for producing deionized water, a deionized water producing apparatus for deionizing water by passing water to be treated through an ion exchange resin has been known for a long time. Since the ion exchange resin is saturated with ions, the ion exchange resin must be regenerated with an acid and alkali aqueous solution. Has been put to practical use.

As shown in FIG. 9, a cation exchange membrane 41 and an anion exchange membrane 42 are bonded to both surfaces of a frame 40, respectively, and an ion exchange resin A plurality of deionization modules 44 filled with 43 (cation exchange resin and anion exchange resin) are juxtaposed via a rubber packing 45 provided around the frame 40, and a space between the deionization modules is provided. Is configured as a concentration chamber 46, and the plurality of deionization modules 4
An anode 47 and a cathode 48 are arranged on both sides of an alternately arranged body 4 and the concentration chamber 46. Note that, specifically, the deionization module 44 vertically or horizontally lays a plurality of ribs (not shown) in a space inside the frame 40 to partition the space inside the frame 40 into a plurality of small chambers, These chambers are filled with the ion exchange resin. Although not shown, a flow path forming material such as a synthetic resin net is accommodated in the concentration chamber 46. In this apparatus, a direct current is passed between the anode 47 and the cathode 48, and the water to be treated is caused to flow into the desalination chamber formed by the deionization module 44 through the water inflow line 49 to be treated. The electrode water flows into the concentration chamber 46 through the line 50, and the electrode water flows into the electrode chambers of both electrodes via the electrode water inflow lines 51 and 52, respectively.

[0004] The water to be treated that has flowed into the deionization chamber flows down the packed bed of the ion exchange resin 43, whereupon the impurity ions in the water to be treated are removed, and the deionized water is discharged through a deionized water outflow line 53. can get. When the concentrated water flowing into the concentration chamber 46 flows down in the concentration chamber 46, the ion exchange membrane 4
1 and 42, the impurity ions move through the electrode water outflow lines 54 and 55, receive the impurity ions, flow out of the concentrated water outflow line 57 as concentrated water in which the impurity ions are concentrated, and flow into the electrode chambers. leak.

[0005] Since the impurity ions in the water to be treated are electrically removed by the above operation, deionized water can be continuously obtained without regenerating the charged ion exchange resin with a chemical solution.

[0006]

However, in the above-mentioned conventional apparatus, it is difficult to set appropriate operating conditions, and the operating state is extremely unstable. That is, assuming now that the pressure in the desalting chamber 56 is P _d and the pressure in the concentration chamber 46 is P _c , it is preferable that P _d ≦ P _c from the structural point of view. The reason is that if P _d ≧ P _c , the problem of peeling of the ion exchange membranes 41 and 42 occurs. Ion exchange membranes 41, 42
Is bonded to the frame 40, but the pressure P in the desalting chamber 56 is
_{When d} is higher than the pressure _Pc in the concentration chamber 46, a force acts in a direction in which the adhesive is peeled off. In severe cases, the adhesive is peeled off or the adhesive part is left as it is, and the ion exchange membrane in the vicinity thereof is removed. The deionized water may leak, resulting in a problem that deionized water leaks or impairs the deionization performance. Such problems arise because of incomplete seals).

From the viewpoint of electric resistance, it is preferable that P _d ≦ P _c . The electric resistance of the desalting chamber 56 is determined by the resistance caused by the contact state between the ion exchange resins and the ion exchange resin, in addition to the electric resistance of the ion exchange membrane itself and the electric resistance of the ion exchange resin itself. The magnitude is also determined by the resistance element due to the contact state. In this case, when the ion exchange resin is more strongly pressed from the outside, and the ion exchange resin or the ion exchange membrane and the ion exchange resin are more strongly in contact with each other, the electric resistance is reduced. Becomes smaller. Conversely, if the pressing force at the time of the contact is weak, the electric resistance increases, and if the contact is released and the contact is separated, the electric resistance further increases. If the pressure P _d desalting chamber 56 wherein is higher than the pressure P _c in the concentrating compartment 46, ion exchange membrane 41 bulges outward, expanding the internal volume of that amount demineralizing compartment Therefore, if the contact between the ion-exchange resins or between the ion-exchange membrane and the ion-exchange resin is loose or severe, the contact is released and the ion-exchange resin is partially separated, and as a result, the electric resistance increases. . If the electric resistance increases, a high voltage is required to flow a constant current, which leads to an increase in the cost of the power supply unit.

[0008] Ion-exchange by but above P _d ≦ P _c in terms of the structure surface and electrical resistance as is preferred, when operating under the conditions of P _d ≦ P _c, the pressure differential concentrated water containing impurity ions at a high concentration There is a risk of entering the desalination chamber 56 through the membranes 41 and 42. This is because the ion exchange membrane does not have the ability to completely prevent liquid permeation. Further, since the salt concentration of the concentrated water in the concentration chamber 46 is higher than the salt concentration of the deionized water in the desalination chamber 56, a concentration gradient is generated between the two, and the deionized water having a low concentration is shifted from the concentrated water side having a high concentration. The ions tend to diffuse through the ion exchange membranes 41, 42 to the side, where the pressure P _c in the concentration chamber 46
There high when its tendency than the pressure P _d desalting chamber 56 becomes remarkable.

When the concentrated water mixes with the deionized water, the quality of the deionized water is deteriorated, and the performance of the apparatus is remarkably reduced. From such a viewpoint, the operating condition is P _d ≧ P
_c will be preferred. However, when P _d ≧ P _c , as described above, problems such as peeling and destruction of the ion exchange membrane and an increase in electric power cost due to an increase in electric resistance occur.

As described above, in the conventional apparatus, it is difficult to set appropriate operating conditions because there are two opposing operating conditions, the operating state is unstable, and even a slight change in the flow rate or pressure is caused. There is a problem that the properties of deionized water are affected.

Further, the operation of uniformly filling the deionization module 44 with the ion exchange resin 43 is extremely troublesome, difficult and inefficient. Further, in manufacturing an alternate array of the deionization modules 44 and the concentration chambers 46, a plurality of deionization modules 44 are stacked one upon another via a rubber packing 45, and these are fastened using fastening means. Therefore, when the number of the deionization modules 44 is large, the deionization modules cannot be uniformly tightened, which may cause incomplete sealing, and the number of deionization modules to be assembled is naturally limited. It was difficult to manufacture a large-sized device.

The present invention has been made in view of the above points,
It is an object of the present invention to provide an electric deionized water producing apparatus that can set appropriate operating conditions, stabilize the operating state, and can be easily manufactured and can be increased in size.

[0013]

According to the present invention, there is provided (1) a method of directly or indirectly joining a peripheral portion of a cation exchange membrane and an anion exchange membrane facing each other, and forming a concentrated water flow in an internal space formed by the joint. A plurality of enrichment chamber units, each having a passage and an inlet / outlet of concentrated water, are arranged in parallel at a predetermined interval between the anode and the cathode, and the space between the enrichment chamber units is filled with an ion exchanger. (2) a cation-exchange membrane and an anion-exchange membrane are overlapped, and the periphery of the opposing surface is joined to form a bag. The electric deionized water producing apparatus according to the above (1), wherein the flow path forming material is stored in the internal space of the bag body, and a concentrated water inlet / outlet is provided to constitute a concentrated room unit. Cation exchange membrane on one side of the hollow frame In addition to the above-mentioned (1), an anion exchange membrane is bonded to the other surface, a flow path forming material is accommodated in an internal space formed by the anion exchange membrane, and a concentrated water inlet / outlet is provided to constitute a concentrated chamber unit. And (4) the apparatus for producing deionized water according to the above (2) or (3), wherein the flow path forming material is an ion exchanger. (4) The electric deionized water production apparatus according to the above (4), which is an exchange fiber, (6) a frame integrally provided with a plurality of ribs having a hollow shape and a function of a flow path forming material. The electric deaeration device according to the above (1), wherein a cation exchange membrane is bonded to one surface of the body, and an anion exchange membrane is bonded to the other surface, and a concentrated water inlet / outlet is provided to constitute a concentration chamber unit. The gist is an ion water production system.

The apparatus of the present invention will be described below with reference to the drawings. FIG. 1 shows an embodiment of the apparatus of the present invention. 1
Is a casing, a base 2 is provided at a lower portion of the casing 1, an anode 3 and a cathode 4 are provided on the base 2 so as to face each other, and a plurality of enrichment chamber units 5 and A desalination unit 6 is provided.

The concentrating chamber unit 5 directly or indirectly joins the peripheral portions of the pair of anion exchange membranes 7 and the cation exchange membranes 8 facing each other to form a concentrated water flow path therein and form concentrated water. Although an entrance is provided, there are various modes. 3 to 5 show an example in which the periphery of the opposing surfaces of the ion exchange membranes is indirectly joined.

That is, as shown in FIG. 3 as an exploded perspective view, an anion exchange membrane 7 is joined to one surface of a hollow frame 9 and a cation exchange membrane is attached to the other surface of the frame 9. 8 are joined. Since the joint portion is a contact surface with the frame 9, the peripheral portions of the opposing surfaces of the ion exchange membranes 7 and 8 are indirectly joined via the frame 9. Adhesion with an adhesive is usually employed as the joining means, but other known joining methods, such as adhesion with a double-sided tape, may be used.

Thus, the ion exchange membranes 7 and 8 are joined to the frame 9 to form a space therein, thereby forming the concentration chamber 10. The concentrating chamber 10 serves as a flow path through which the concentrated water flows, and a flow path forming material is stored in the concentrating chamber 10 for forming and maintaining the flow path. Since the ion exchange membranes 7 and 8 are made of a flexible material, there is a possibility that the ion exchange membranes 7 and 8 are easily deformed by the pressing force from the desalting unit 6, and in this case, the anion exchange membrane 7 and the cation exchange membrane 8 come into contact with each other. Thus, there arises a problem that the concentrated water flow path to be formed in the internal space is closed. Then, the above-mentioned flow path forming material is stored to secure the concentrated water flow path. The thickness of the concentrated water channel is 1 to 10 mm, preferably 2 to 4 mm. It is preferable to use an ion exchanger as the flow path forming material. The use of the ion exchanger has the advantage that the electric resistance in the concentration chamber can be reduced and the power cost can be reduced. Although ion exchange fibers are preferably used as the ion exchanger, granular ion exchange resins and the like can also be used. As the ion exchange fiber, a felt-like fiber is preferable.

FIG. 3 shows an example using felt-like ion exchange fibers (for example, cation exchange fibers) 11, and FIG. 4 is a longitudinal sectional view of FIG. As shown in these figures, the ion exchange fibers 11 are stored in a completely filled state so as to fill the entire space of the concentration chamber 10. In this way, there is an advantage that no space is created between the ion exchange fiber 11 and the concentration chamber 10 and the electric resistance can be reduced.

When the felt-like ion exchange fibers 11 are used, the concentrated water flows through the voids in the fibers.
Therefore, the void forms a concentrated water flow path.

As the flow path forming material, in addition to the above-mentioned ion exchanger, although not particularly shown, a net made of plastic or the like, cloth, or the like can also be used.

In the present invention, there are two modes for accommodating the flow path forming material in the concentration chamber 10, namely, insertion and fixing. That is, the flow path forming material may be inserted (filled) into the concentration chamber 10 so as to fill the space, or may be simply inserted, and the flow path forming material may be fixed to the frame 9 by using some fixing means, for example. You may.

The present invention is not limited to the case where a separate flow path forming material is provided. For example, the frame and the flow path forming material may be integrated. That is, as shown in FIG.
Are integrally provided, the rib 12 functions as a flow path forming material. Reference numeral 13 denotes a water passage hole provided in the rib 12.

Reference numeral 14 denotes a concentrated water inlet provided at the lower end of the frame 9, and reference numeral 15 denotes a concentrated water outlet provided at the upper end of the frame. These ports communicate with the inside of the concentration chamber.

FIGS. 6 and 7 show another embodiment of the concentration chamber unit according to the present invention, that is, an example in which the peripheral portions of opposing surfaces of ion exchange membranes are directly joined. In this embodiment, the anion exchange membrane 7 and the cation exchange membrane 8 are overlapped, and the peripheral portions of the opposing surfaces are joined to form a bag. In FIG. 6, a hatched portion H indicates a joined portion. Also in this case, as a joining means, an adhesive with an adhesive, an adhesive with a double-sided tape, and other known joining methods are employed.
The inner space of the bag is configured as a concentration chamber 10, the concentration chamber 10 serves as a concentrated water flow path, and a felt-like ion exchange fiber 11 as a flow path forming material is housed in the concentration chamber 10. As flow path forming materials other than ion exchange fibers,
The same one as described above with reference to FIGS. 3 and 4 is used. Also, the manner of storing the flow path forming material is the same as described above.
It may be inserted or fixed. FIG. 7 is a longitudinal sectional view of FIG.
As described above, in this embodiment, the ion exchange fibers 11 are densely packed and stored in the concentration chamber 10 in the same manner as described above. At the upper and lower ends of the bag, a concentrated water inlet 14 and a concentrated water outlet 15 are provided to communicate with the inside of the concentration chamber 10, respectively.

A plurality of the concentrating chamber units 5 configured as described above are arranged on the base 2 at predetermined intervals. FIG. 2 is a sectional view taken along the line AA of FIG. 1. Support frames 16, 16 are provided in the casing 1 so as to face each other for mounting and fixing the enrichment chamber unit 5. Each of the support frames 16 has a plurality of concave grooves 17 along the longitudinal direction, and L-shaped grooves 18 are formed at both ends in the longitudinal direction. The enrichment chamber unit 5 is inserted between the support frames 16 and 16 from above to below so that both end portions are fitted into the concave grooves 17 and 17 of the support frame. It is held and fixed on the base 2.

On the other hand, the base 2 comprises a mesh portion 19 having a fine mesh and legs 20 for supporting and fixing the mesh portion 19. The mesh portion 19 has a projecting shape projecting upward at predetermined intervals. A part 21 is provided. The protruding portions 21 are provided along the width direction of the enrichment chamber unit 5, and are formed simultaneously between the front and rear protruding portions 21 when the enrichment chamber unit 5 is inserted between the support frames 16 as described above. Unit 5
Is fitted at the lower end. Net 19
Has a mesh mesh to the extent that the ion exchanger does not pass therethrough, so that when the space between the concentrating chamber units 5 and 5 is filled with the ion exchange resin, the resin does not pass through the net 19.

The base 2 is not limited to the above structure.
In short, any material having a fine pore structure that allows deionized water to pass therethrough but does not allow the ion exchanger to pass through may be used. For example, a urethane sponge may be used.

The anode 3 and the cathode 4 are each an electrode support 2
An anode plate 24 and a cathode plate 25 are respectively attached to the concave portions 2 and 23, and a partition film is usually bonded to the front surfaces of the electrode supports 22 and 23, respectively.

As the partition membrane, a cation exchange membrane, an anion exchange membrane, or a mere diaphragm having no ion exchange property is used. In this embodiment, the ion exchange membrane of the concentration chamber unit 5 also serves as the partition membrane. Used. That is,
The enrichment chamber units 5 and 5 are adhered to the front surfaces of the electrode supports 22 and 23 in both electrode portions, respectively, and the cation exchange membrane 8 of the enrichment room unit is mounted on the front surface of the electrode support 22 of the anode 3.
In addition, the anion exchange membranes 7 of the unit are bonded to the front surface of the electrode support 23 of the cathode 4, respectively, and the anode chambers 26, A cathode chamber 27 is formed.

Since chlorine gas may be generated by electrolysis in the anode chamber 26, the cation exchange membrane adhered to the front surface of the electrode support 22 of the anode 3 is made of fluorine having excellent oxidation resistance. It is preferable to use a resin-based cation exchange membrane (for example, Nafion (trade name)).

The anode 3 and the cathode 4 configured as described above are placed on the base 2 at both ends in the casing 1. At this time, the enrichment chamber units 5 and 5 adhered to the front surfaces of the electrode supports 22 and 23 respectively have both side ends fitted into the L-shaped grooves 18 and 18 of the support frame and fixed in position.

The desalting section 6 is formed by filling each space between the concentrating chamber units 5 and 5 with an ion exchanger. In addition,
Instead of using the ion exchange membrane of the concentration chamber unit 5 as a partition membrane as in the present embodiment, when a dedicated partition membrane is provided on the front surface of the electrode support, the space between the anode and the concentration chamber unit and the cathode An ion exchanger can also be filled in the space between the air conditioner and the enrichment unit to form a desalination unit. However, in this case, it is necessary to adhere an anion exchange membrane to the front surface of the anode electrode support and a cation exchange membrane to the front surface of the cathode electrode support, which is different from this embodiment. Usually, an ion exchange resin is used as the ion exchanger, but an ion exchange fiber may be used. 1 and 2 show:
An example in which the ion exchange resin 28 is used as an ion exchanger is shown. In this case, a cation-exchange resin and an anion-exchange resin are used. When filling the space, a mixed cation-exchange resin of a cation-exchange resin and an anion-exchange resin may be used. And an anion exchange resin may be alternately packed in layers.
The thickness t (FIG. 1) of the desalting section 6 is 2 to 30 mm, preferably 4 to 10 mm.

The treated water inflow pipe 29 is provided on the upper surface of the casing 1.
In addition, a deionized water outflow pipe 30 is provided on the lower surface, and a concentrated water inflow pipe 31 and electrode water inflow pipes 32, 33 are respectively provided in the lower part of the casing, and these inflow pipes 31, 32, 33 are respectively provided. Through the net 19 of the table, the inflow pipe 31 is connected to the concentrated water inlet 14 of the enrichment chamber unit, and the inflow pipes 32, 33 are respectively connected to the anode chamber 26,
It is connected to each lower part of the cathode chamber 27. A concentrated water outlet pipe 34 is connected to the concentrated water outlet 15 of the concentration chamber unit, and electrode water outlet pipes 35 and 36 are connected to upper portions of the anode chamber 26 and the cathode chamber 27, respectively. ,
The outlet pipes 32, 33 and the outlet pipes 34, 35, 36 extend outward from the casing, respectively. The casing in the apparatus of the present invention is not limited to the rectangular box-shaped container as described above, and the present invention can be similarly applied to a cylindrical container.

Although the apparatus of the present invention is configured as described above, the apparatus J of the present invention can be used in combination with a decarboxylation apparatus D and a reverse osmosis membrane apparatus K as shown in FIG. First, the water to be treated A is decarbonated by passing it through a decarbonation device D, and then the treated water is passed through a reverse osmosis membrane device K, so that Ca which causes scale deposition in the electric deionized water production device is produced. It is preferable because hardness components such as ions and Mg ions can be removed.

[0035]

Next, the operation of the present invention will be described with reference to FIG.
By passing a direct current between the anode 3 and the cathode 4, the water to be treated flows into the treated water inflow pipe 29 and the concentrated water inflow pipe 31.
More concentrated water flows in, and electrode water flows in from electrode water inflow pipes 32 and 33.

The water to be treated flowing from the treated water inflow pipe 29 flows down in each of the desalting sections 6 in a downward flow, and when passing through the packed bed of the ion exchange resin 28, impurity ions are removed. Water is obtained, and this deionized water is guided to the lower part of the casing through the mesh portion 19 of the base, and the deionized water outflow pipe 30 is formed.
More outflow.

On the other hand, the concentrated water flowing from the concentrated water inflow pipe 31 flows upward through each of the concentration chambers 10 and rises. The impurity ions in the desalting section 6 are electrically attracted to the ion exchange membrane 7,
It moves to the concentration chamber 10 through 8. The concentrated water flowing through the concentration chamber 10 receives the moving impurity ions and flows out of the concentrated water outflow pipe 34 as concentrated water in which the impurity ions are concentrated. The electrode water flowing from the electrode water inflow pipes 32, 33 flows out of the electrode water outflow pipes 35, 36.

As shown in FIG. 8, a part of the water A to be treated (the permeated water when first passed through the decarbonation device D and the reverse osmosis membrane device K) supplied to the apparatus of the present invention is converted into concentrated water B And the concentrated water B flowing out of the concentration chamber
Can be used as electrode water C. As described above, when the concentrated water is used as the electrode water, the current efficiency is improved due to the large amount of ions, and the power cost can be reduced. Further, the remaining part of the concentrated water B may be refluxed to the supply part of the water A to be treated between the decarboxylation device D and the reverse osmosis membrane device K for circulation and use. It can contribute to improvement of recovery rate. The flow direction of the concentrated water to the concentration chamber may be a downward flow.

In operating the apparatus of the present invention, the desalination section 6
In relation to the pressure _Pd of the concentration chamber 10 and the pressure _Pc of the concentration chamber 10,
It is possible to operate under the condition of P _d ≧ P _c . That is,
When P _d ≧ P _c , the ion exchange membranes 7 and 8 of the enrichment chamber unit 5 receive a force in the direction of pushing inward and do not receive a force in the outward direction, that is, a force in the direction of peeling. There is no problem that the exchange membranes 7 and 8 are peeled or torn.

When P _d ≧ P _c , a force is exerted in the direction in which the desalting section 6 expands. Even if the desalting section 6 expands, there is no problem for the following reasons. That is, a plurality of ribs are vertically or horizontally provided in the space inside the frame 40 to prevent the ion exchange membrane from bending outward and expanding like the deionization module of the conventional device. The space portion is divided into a plurality of small chambers, and unlike the case where the hermetically sealed small chamber is filled with an ion exchange resin, the desalting section 6 of the present invention does not store extra things such as ribs inside. Therefore, the deionization chamber is open compared to the conventional deionization chamber, and the degree of freedom of movement of the ion exchange resin in the desalination section 6 is larger than that of the ion exchange resin in the deionization module. Therefore, even if the phenomenon of contact separation between the ion-exchange resins or between the ion-exchange membranes 7 and 8 and the ion-exchange resin 28 occurs temporarily due to the spread of the desalination section 6, the flow of the water to be treated easily and easily. It quickly returns to the contact state, and there is no risk of causing an increase in electric resistance.

If P _d ≧ P _c , there is no possibility that the concentrated water enters the desalting section 6 through the ion exchange membranes 7 and 8 in view of the pressure gradient. Regarding the tendency of ions in concentrated water to diffuse toward deionized water due to concentration gradient,
When P _d ≦ P _c , the tendency is increased from the surface of the pressure gradient. On the other hand, when P _d ≧ P _c , a physical action in the direction of suppressing the tendency (action by the above-described pressure gradient) occurs. Set.

Thus, in the device of the present invention, P _d ≧
It is possible to operate under the condition of _Pc , whereby uniform and appropriate operating conditions can be set, and there is an effect that a stable operating state can be maintained.

In the above description, an example in which the water to be treated flows in a downward flow has been described. However, it is a matter of course that the apparatus may be configured to flow the water to be treated in an upward flow.

[0044]

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS
The treated water quality was measured. The configuration and operating conditions of the device are as follows. Cation exchange membrane: CMH manufactured by Tokuyama Soda Anion exchange membrane: AMH manufactured by Tokuyama Soda Anode, cathode: Platinum electrode (10cm × 20c)
m) Number of concentrating chamber units: 2 Concentrated water channel material: 2 mm thick, cation exchange fiber (manufactured by Nichibi) Number of desalting parts: 3 (however, the same anion exchange membrane as above on the front surface of the anode electrode support) In addition, the same cation exchange membrane as above is bonded to the front surface of the electrode support of the cathode as a dedicated partition membrane, and the space between the positive and negative electrodes and the enrichment unit is filled with ion exchange resin. The number of desalted portions was set to 3 by forming a desalted portion by means of a filter.) Desalted portion thickness: 1 cm Ion exchange resin: Amberlite IR-120B
(Trade name) and Amberlite IRA-402 (trade name)
DC power supply: Takasago GPO110-3 Treated water: Permeated water de-ionized by reverse osmosis membrane SU-720 (manufactured by Toray) after treatment of tap water with activated carbon Water quality of permeated water: Electric conductivity 5-7 μS / cm,
pH 6.3 to 6.4, water temperature 16 to 18 ° C Operating pressure: 1.5 kgf /
cm ^2, 1.3kgf / cm ² with deionized water outlet, 1.0 kgf / cm ² with downward circulation water concentrated water inlet, 0 with concentrated water outlet.
9 kgf / cm ² , upward flowing water The quality of the treated water one day after the start of operation was measured. Table 1 shows the conditions for 1) the flow rate of the water to be treated, 2) the total flow rate of the concentrated water and the electrode water, 3) the current, and 4) the voltage.
The measurement was carried out with various changes as shown in FIG. Table 1 shows the results.

[0045]

[Table 1]

As is clear from the above results, good treated water quality was obtained. From this, it was found that the apparatus of the present invention has a sufficiently practical deionizing ability. Also, no leakage of the solution to the outside was observed due to the container structure.

[0047]

As described above, according to the present invention, appropriate operation conditions can be set, the operation state can be stabilized, and the deionization performance is always stable even when there are flow rate and pressure fluctuation factors. In addition to the high reliability, there is an effect that the electric resistance can be reduced and the power cost can be reduced.

Since the ion exchanger is filled between the concentrating chamber units, the troublesome work of uniformly filling the ion exchange resin in the deionization module as in the conventional apparatus is not required, and the production is easy. is there. Further, in the manufacture thereof, there is no need to stack and fix the deionization module and the concentration chamber as in the conventional apparatus, and as a result, there is no restriction or difficulty in manufacturing a large-sized apparatus, and the apparatus can be easily manufactured. This has the effect of realizing an increase in size.

[Brief description of the drawings]

FIG. 1 is a longitudinal sectional view of the device of the present invention.

FIG. 2 is a sectional view taken along line AA of FIG.

FIG. 3 is an exploded perspective view of a concentration chamber unit.

FIG. 4 is a longitudinal sectional view of the concentration unit of FIG. 3;

FIG. 5 is a longitudinal sectional view of another embodiment of the concentration chamber unit.

FIG. 6 is an exploded perspective view of another embodiment of the concentration chamber unit.

FIG. 7 is a longitudinal sectional view of the concentration unit of FIG. 6;

FIG. 8 is a block diagram of a deionization system using the apparatus of the present invention.

FIG. 9 is a schematic longitudinal sectional view of a conventional device.

[Explanation of symbols]

 3 Anode 4 Cathode 5 Concentration room unit 6 Desalination section 7 Anion exchange membrane 8 Cation exchange membrane 14 Concentrated water inlet 15 Concentrated water outlet 28 Ion exchange resin

Claims (6)

(57) [Claims] 1. A peripheral portion of a cation exchange membrane and an anion exchange membrane, which are directly or indirectly joined to each other, to form a concentrated water flow path in an internal space formed thereby and to provide an inlet / outlet of the concentrated water. A plurality of concentrating chamber units are arranged in parallel at a predetermined interval between the anode and the cathode, and a desalting section is formed by filling an ion exchanger in a space between the concentrating chamber units. Electric deionized water production equipment. 2. A cation-exchange membrane and an anion-exchange membrane are superimposed on each other, and their peripheral portions are joined to form a bag.
2. The electric deionized water producing apparatus according to claim 1, wherein a flow path forming material is accommodated in the internal space of the bag body, and a concentrated water inlet / outlet is provided to constitute a concentrated chamber unit. 3. A cation exchange membrane is joined to one surface of a frame having a hollowed-out shape, and an anion exchange membrane is joined to the other surface. 2. The electric deionized water producing apparatus according to claim 1, wherein the forming material is housed, and a concentrated water inlet / outlet is provided to constitute a concentrated chamber unit. 4. The electric deionized water producing apparatus according to claim 2, wherein the flow path forming material is an ion exchanger. 5. The electric deionized water producing apparatus according to claim 4, wherein the ion exchanger is an ion exchange fiber. 6. A cation exchange membrane is joined to one surface of a frame body integrally provided with a plurality of ribs having a hollowed-out shape and functioning as a flow path forming material, and the other side. 2. The electric deionized water producing apparatus according to claim 1, wherein an anion exchange membrane is joined to the surface of the above, and a concentrated water inlet / outlet is provided to constitute a concentrated room unit.