KR20120091014A - Ion-exchange device, column therefor, and water treatment device - Google Patents

Abstract

[PROBLEMS] An ion exchange device capable of producing a high quality deionized water even after regeneration is reliably prevented from reverse regeneration of anion exchange resin and cation exchange resin in a tower, and a tower for the same.
[Resolution] During regeneration, the valve 12 is closed, the valves 7 and 10 are opened, and an acid solution such as HCl is supplied from the upper supply / discharge pipe 3, and from the third communication pipe 8 An alkaline solution such as NaOH is supplied. The acid solution flows in the order of the collecting and draining member 4, the inert resin 22, the cation exchange resin 21, the collecting and draining member 6, the communication pipe 5, and the valve 7. 21 is reproduced. The alkaline solution flows in the order of the collecting and draining member 9, the inert resin 32, the alkali exchange resin 31, the collecting and draining member 14, and the lower supply and drain piping 13, and the anion exchange resin 31 is regenerated. do.

Description

ION-EXCHANGE DEVICE, COLUMN THEREFOR, AND WATER TREATMENT DEVICE}

The present invention relates to a regenerated ion exchange device including an anion exchange resin and a cation exchange resin, and a column for the same. The present invention also relates to a water treatment apparatus including the ion exchanger.

BACKGROUND ART Ion exchange devices are widely used in pure water and ultrapure water production facilities in the electronics industry and the like. As one of these ion exchangers, a mixed phase ion exchanger is well known.

The hybrid phase ion exchange device includes an ion exchange column having a mixed ion exchange resin layer in which a strong acid cation exchange resin and a strong base anion exchange resin are mixed. Thus, cation and anion in raw water are simultaneously ion exchanged to produce pure water having high purity. In the regeneration of each of the ion exchange resins, the mixed ion exchange resin layers are backwashed in the same column, and a strong base anion exchange resin layer is formed on the upper layer by a specific gravity difference of each ion exchange resin, and a strongly acidic catty is formed on the lower layer. After the on-exchange resin layer is formed, each regenerator is passed through each of the ion-exchange resin layers to regenerate both ion-exchange resins individually. This regeneration operation may be performed in the same column, and each ion exchange resin may be separately extracted in a separate column, and regeneration may be performed separately in each column.

In the conventional mixed bed type ion exchange apparatus, the problem by separation incompleteness of the cation-anion exchange resin called "reverse regeneration" may arise.

That is, the cation exchange resin is used in H type, and the regeneration is performed by passing the acid solution. On the other hand, anion exchange resin is used by OH type, and the regeneration is performed by passing an alkali solution. As described above, prior to regeneration of the ion exchange resin of the mixed bed desalting tower, first, an upflow water flow is performed in the mixed bed, and the anion exchange resin and the cation exchange resin are separated by specific gravity, and then acid, for example, For example, an aqueous HCl solution is introduced from the bottom of the column to regenerate the cation exchange resin, and an alkali, for example, an NaOH aqueous solution is introduced from the top of the column to regenerate the anion exchange resin. Each regeneration waste liquid is discharged from the discharge pipe formed at the interface portion of the anion exchange resin phase and the cation exchange resin phase. Thereafter, N ₂ gas is introduced from the bottom of the tower, the anion exchange resin and the ion exchange resin are mixed to form a mixed phase, and water flow is resumed.

In such a regenerative mixed bed type ion exchange column, it is necessary to sufficiently separate the cation exchange resin and the anion exchange resin prior to the regeneration of each ion exchange resin by an acid or an alkali. If this separation is not completed, for example, when cation exchange resin is mixed in an anion exchange resin, the cation exchange resin is Na-type by regeneration (reverse regeneration) by alkali (mostly sodium hydroxide is used). When deionization is performed using this resin, sodium ions are released. In addition, when an anion exchange resin is mixed in the cation exchange resin, the anion exchange resin becomes SO ₄ type or Cl type by regeneration (reverse regeneration) by acid (mainly sulfuric acid or hydrochloric acid is used), and deionization During treatment, sulfate ions or chlorine ions are released.

As an ion exchange device intended to prevent such reverse regeneration, Japanese Laid-Open Patent Publication No. Hei 10-137751 (Patent Document 1) divides a column into two chambers of upper and lower sides with a water-permeable partition plate, and a cation exchange resin in one chamber. Filled with anion exchange resin in the other chamber is described. In particular, in Figs. 5 and 11 of Patent Document 1, the inside of the tower is divided into two chambers with a water-permeable partition plate, a cation exchange resin is filled in the room, an anion exchange resin is filled in the room, and raw water is lost from the loss. It is described that the water is passed through the basement in order from the anion exchange resin to the cation exchange resin. This partition plate permits the flow of water, but prevents the flow of the ion exchange resin and prevents mixing of the anion exchange resin and the cation exchange resin. The tower body of this patent document 1 is a one tower system, and its device area is small.

In the column for ion exchange apparatus of patent document 1, when raw water is passed in order from cation exchange resin to anion exchange resin, Na derived from NaOH etc. for anion exchange resin regeneration from an anion exchange resin on a downstream side. Many metal ion components, such as this, elute, and there exists a possibility that process water quality may fall. When raw water is passed through an anion exchange resin to a cation exchange resin, metal components such as Na eluted from the anion exchange resin are captured by the cation exchange resin, and thus the treated water quality is improved.

By the way, in the ion exchange apparatus which passes raw water in order from anion exchange resin to cation exchange resin, when raw water contacts anion exchange resin, anion, such as a sulfate ion and a chlorine ion, by an anion exchange resin The component is substituted with OH ions and the pH becomes alkaline. And when hardness component is contained in raw water, the scale (for example, magnesium hydroxide, calcium carbonate, etc.) of these hardness components generate | occur | produce. In patent document 1, the reverse osmosis membrane apparatus is provided in front of the ion exchange apparatus, and the hardness component is removed (Paragraph 0066 of patent document 1).

Japanese Unexamined Patent Publication No. 10-137751

In the ion exchange apparatus of JP-A-10-137751, the partition plate separating the anion exchange resin layer and the cation exchange water layer is water-permeable, so that the acid solution for regenerating the cation exchange resin regenerates the partition plate during regeneration. Reverse regeneration occurs by passing through and contact with the anion exchange resin. In addition, reverse regeneration occurs when the alkaline solution for regenerating anion exchange resin passes through the partition plate and contacts the cation exchange resin. Paragraph 0023, 0027, 0028 of Patent Document 1 describes that water is passed through as pure water so that one regeneration agent does not flow into the other ion exchange resin layer during regeneration, but it is insufficient to completely prevent mixing of the regeneration agent. Reverse playback occurs.

SUMMARY OF THE INVENTION An object of the present invention is to provide an ion exchange apparatus capable of producing high quality deionized water even after the regeneration of the anion exchange resin and the cation exchange resin in the inside of the tower without fail, and to provide a tower for the same. It is done.

The present invention also prevents scale precipitation into the anion exchange resin in the tower and prevents reverse regeneration of the anion exchange resin and the cation exchange resin, thereby ensuring stable water production. It is an object to provide a device.

In the tower for ion exchange devices in which the ion exchange device is filled with an ion exchange resin, the tower body for the ion exchange device according to the first aspect is formed by partitioning the loss and the basement by a water-repellent partition plate in the column, and is taken out of the tower body. The loss and the basement are communicated by the surrounding communication means.

The ion exchange apparatus of a 2nd aspect is equipped with the ion exchange apparatus tower | column of a 1st aspect, the cation exchange resin accommodated in one of the loss | disassembly and basement of the tower body, and the anion exchange resin accommodated in the other.

The ion exchange device of the third aspect includes, in the second aspect, an upper supply pipe for supplying or discharging a liquid to an upper portion of the loss, and a lower supply pipe for supplying or discharging a liquid to a lower portion of the base. The communication means communicates with the first communication pipe for supplying liquid to the lower part of the loss, the second communication pipe for supplying liquid to the upper part of the base, and the first communication pipe and the second communication pipe. And a third communication pipe, an opening and closing means of the third communication pipe, and a supply and discharge means of the regeneration liquid formed in the first communication pipe and the second communication pipe, respectively.

The ion exchange device of the fourth aspect is, in the third aspect, a water collecting member for passing water through the upper portion of the upper chamber, the lower portion of the upper chamber, the upper portion of the chamber and the lower portion of the chamber, but preventing the passage of the ion exchange resin. It is arrange | positioned, The terminal of the said upper supply-discharge piping, the 1st communication piping, the 2nd communication piping, and the lower supply-discharge piping is respectively connected to the collection and drainage member, It is characterized by the above-mentioned.

In the ion exchange apparatus of the fifth aspect, in the fourth aspect, granular inert resin is filled in the upper portion of the upper chamber and the upper chamber of the chamber, respectively, and the drainage member of the upper chamber and the lower chamber of the chamber are respectively It is characterized by being embedded in inert resin.

The water treatment apparatus of a sixth aspect has the ion exchange apparatus of any one of the second to fifth aspects and the hardness component removing means formed at the front end of the ion exchange apparatus.

In the water treatment apparatus of the seventh aspect, in the sixth aspect, the ion exchange apparatus is configured so that the water to be treated first comes into contact with the anion exchange resin and then with the cation exchange resin.

In the tower body and the ion exchange device of the present invention, the upper and lower chambers are partitioned by a water-repellent partition plate, a cation exchange resin is accommodated in one chamber, and an anion exchange resin is accommodated in the other chamber. The water to be treated (raw water) is supplied to one chamber, flows into the other chamber via a communication means, and is taken out of the other chamber.

In this ion exchange apparatus, an acid or alkali is separately supplied to each chamber at the time of regeneration of ion exchange resin. Therefore, the cation exchange resin and the anion exchange resin are not mixed at all, and the partition plate which partitions both chambers is of a water order, and the acid or alkali supplied to one of the chambers passes through the partition plate to the other chamber. It does not flow in at all, and reverse regeneration is prevented.

The tower body of the present invention is divided into two chambers with a partition plate inside, and has a smaller installation space than the anion exchange tower and the cation exchange tower, and the length of the pipe is also reduced, and ion exchange is performed. The height of the ion exchange apparatus can be made low by separating between the ion exchange resin chambers which fill resin with a partition plate. In addition, it can be produced inexpensively.

In the ion exchange apparatus of a 3rd aspect, an acid or an alkali can pass easily through a 1st communication pipe and a 2nd communication pipe, respectively, and can regenerate efficiently. At this time, by closing the third communication pipe, mixing of acid and alkali is completely prevented. And the ion exchange resin of a loss | disappearance and a basement can be reproduce | regenerated simultaneously, and a regeneration time can be shortened significantly.

According to the ion exchange apparatus of a 4th aspect, local retention of water does not generate | occur | produce in a loss | disappearance and a basement, and can produce | generate treated water (deionized water) and regenerates ion exchange resin efficiently.

In the ion exchange apparatus of the fifth aspect, the inert resin is filled in the upper parts of the loss and the basement, and the flow of the ion exchange resin is suppressed. When the ion exchange resin is flowed, there is a possibility that the water quality decreases because the liquid does not contact the ion exchange resin evenly at the time of harvesting or regeneration, but according to this claim 5, such a water quality decrease is prevented, You can get it. In addition, the direction of water passing between the water to be treated and the regenerant at the time of collection and regeneration is not particularly limited, but it is preferable that the water to be taken upstream and the regeneration to downflow can be obtained because high-quality treated water can be obtained. This is considered to be because the ion-exchange resin sufficiently regenerated by the filling of the inert resin is fixed to the upper portion of each ion-exchange resin, and the ion-exchange resin is located on the outlet side of the water to be treated during water collection.

In the water treatment apparatus of the present invention, raw water is first passed through the water treatment apparatus after the hardness component is removed by the hardness component removal means, so that scale precipitation in the ion exchange apparatus is prevented.

In particular, in this ion exchange apparatus, when water is passed in order from anion exchange resin to cation exchange resin, generation of scale components in the anion exchange resin of the ion exchange apparatus is prevented. In addition, in the ion exchange device, since the water to be treated first contacts the anion exchange resin, metal components such as Na, which have flowed out of the anion exchange resin, are captured by the cation exchange resin.

In addition, when the water to be treated first comes into contact with the anion exchange resin in the ion exchange device, the pH of the water to be treated increases, and the water to be treated with the high pH is brought into contact with the cation exchange resin, thereby causing ions in the cation exchange resin. Exchange capacity is greatly increased.

That is, the following equilibrium reaction which advances in a cation exchange resin layer is accelerated | stimulated by entering into a cation exchange resin layer by coming into contact with an anion exchange resin to process water, and having a low H ⁺ ion concentration. In addition, [H ⁺ ]-R represents a cation exchange resin.

[H ⁺ ] -R + [Na ⁺ ] ⇔ [Na ⁺ ] -R + [H ⁺ ]

As a result, it is possible to stably produce ion exchange treated water having good water quality over a long period of time.

In the water treatment device of the present invention, after removing the hardness component in advance, the water is passed through an anion exchange resin and a cation exchange resin in order in the ion exchange device, thereby improving the treated water quality and the substantial ion exchange capacity of the cation exchange resin. The improvement of is obtained. By adjusting the resin volume ratio to the exchange capacity ratio, both the cation exchange resin and the anion exchange resin can be used in the form of using the exchange capacity at the time of regeneration, thereby improving economic efficiency. When the removal of weak base components such as boron and silica is necessary, the economical efficiency can be further improved by changing the volume ratio of the cation exchange resin and the anion exchange resin in accordance with the actual exchange capacity of those elements.

1A is a schematic cross-sectional view showing a state at the time of drainage of the ion exchange apparatus according to the embodiment.
1B is a schematic cross-sectional view showing a state during regeneration of the ion exchange apparatus according to the embodiment.
2 is a flowchart showing a water treatment apparatus according to the embodiment.
3 is a graph showing the results of Examples and Comparative Examples.

EMBODIMENT OF THE INVENTION Hereinafter, embodiment is described with reference to drawings.

First, with reference to FIG. 1A, 1B, embodiment of the tower body for ion exchange apparatus of this invention, and an ion exchange apparatus is described.

The top body 1 is comprised by the cylindrical part 1a which made the cylinder axial direction the perpendicular direction, the hard plate part 1b of the top part, and the hard plate part 1c of the bottom part. The hard plate part 1b is convexly curved upward, and the hard plate part 1c is convexly curved downward.

The tower body 1 is divided into two chambers, the upper chamber 20 and the basement chamber 30, by the water-repellent partition plate 2. In this embodiment, the partition plate 2 is made of a metal or synthetic resin that does not allow water to pass through at all, and is convexly curved downward like the hard plate portion 1c. The peripheral edge part of the partition plate 2 is watertightly engaged with the inner peripheral surface of the cylindrical part 1a by welding etc.

The first collecting and draining member 4 is disposed above the upper chamber 20, and the upper supply and draining pipe 3 is connected to the first collecting and draining member 4. The second collecting and draining member 6 is provided in the lower part of the upper chamber 20, and the first communication pipe 5 is connected to the collecting and collecting member 6. The third collecting and draining member 9 is provided in the upper part of the chamber 30, and the second communication pipe 8 is connected to the collecting and collecting member 9. The communication pipes 5 and 8 are connected by the third communication pipe 11, and the valve 12 is provided in the communication pipe 11.

At the end portions of the communication pipes 5 and 8, valves 7 and 10 as supply / discharge means of the regeneration liquid are respectively formed. In the lower part of the basement 30, the 4th water collecting and draining member 14 is provided, and the lower water supply and draining pipe 13 is provided in this water collecting and draining member 14. As shown in FIG.

Most of the cation exchange resin 21 is filled in the chamber 20, and granular inert resin 22 is filled in the upper side of the cation exchange resin 21. The first collecting and draining member 4 is embedded in this inert resin 22.

Most of the inside of the chamber 30 is filled with anion exchange resin 31, and granular inert resin 32 is filled above the anion exchange resin 31. The third collecting and draining member 9 is embedded in this inert resin 32.

As inert resin, polyacrylonitrile-type resin etc. which have a specific gravity smaller than ion exchange resin are used. The particle diameter of the inert resin is preferably about the same as that of the ion exchange resin.

As the collecting and draining members 4, 6, 9, and 14, a collecting plate used in a conventional ion exchange device, a strainer in which a plurality of slits are formed in a radially extending pipe, and the like can be used. For example, when the size (particle diameter) of the ion exchange resin is about 0.4 mm, it is preferable to use a strainer having a width of the slit of about 0.2 mm. The collecting and draining members 4 and 14 each have a shape along the hard plate portion 1b and the hard plate portion 1c, and have a small dead space along the hard plate portion 1b and the hard plate portion 1c. Moreover, the water collecting and draining members 6 and 9 have the shape along the partition plate 2, and the dead space along the partition plate 2 is small.

The flow at the time of production (water collection) of deionized water using this ion exchange apparatus is shown to FIG. 1A. In this case, the valve 12 is opened, the valves 7 and 10 are closed, and raw water (treated water) is supplied from the lower supply / discharge pipe 13. The raw water is collected in the water collecting member 14, the anion exchange resin 31, the inert resin 32, the collecting water member 9, the communication pipe (8, 11, 5), the collecting water member (6), cation It flows in order of the exchange resin 21, the inert resin 22, the collection / drainage member 4, and the upper supply / discharge piping 3, and is taken out as process water (deionized water).

At the time of regeneration of the anion exchange resin 31 and the cation exchange resin 21, the valve 12 is closed, the valves 7 and 10 are opened as shown in FIG. 1B, and HCl, An acid solution such as H ₂ SO ₄ is supplied and an alkaline solution such as NaOH is supplied from the second communication pipe 8. The acid solution flows in the order of the collecting and draining member 4, the inert resin 22, the cation exchange resin 21, the collecting and draining member 6, the communication pipe 5, and the valve 7. ), And the cation exchange resin 21 is thereby regenerated. The alkaline solution flows in the order of the collecting and draining member 9, the inert resin 32, the anion exchange resin 31, the collecting and draining member 14, and the lower supply and drain piping 13, and flows out as regeneration wastewater (alkali). This causes the anion exchange resin 31 to be regenerated.

After completion of the regeneration, instead of the HCl solution and the NaOH solution of FIG. 1B, each of the pure waters is passed through, the respective paths and the resin are rinsed, and the washing water is discharged while separately washing the loss and the compartment with the pure water as needed. Thereafter, pure water is circulated between the loss 20 and the chamber 30 for a predetermined time, and then the flow returns to the water collection process. In this regeneration, the cation exchange resin 21 and the anion exchange resin 31 do not mix with each other at all. In addition, there is no case where the regeneration acid solution flows into the basement 30 or the alkaline solution is mixed in the loss chamber 20, so reverse regeneration is completely prevented. Moreover, the cation exchange resin 21 and the anion exchange resin 31 can be reproduced in parallel at the same time, and the regeneration time is remarkably short.

This ion exchange device divides the inside of one tower body into two upper and lower chambers by one partition plate 2, and has a low height of the tower body and a small installation space. Moreover, the piping 5, 11, 8 which communicates the upper chamber 20 and the lower chamber 30 may be short.

In this ion exchange device, the collecting and draining members 4, 6, 9 and 14 are formed along the hard plate portion 1b, the partition plate 2 and the hard plate portion 1c, so that local retention of water is prevented.

In this ion exchange apparatus, inert resins 22 and 32 are filled in the upper part of the chamber 20 and the basement 30, and the flow of the cation exchange resin 21 and the anion exchange resin 31 is prevented. The liquid is uniformly brought into contact with the cation exchange resin 21 and the anion exchange resin 31 at the time of collection and regeneration, so that high quality deionized water is obtained and sufficient regeneration is achieved.

In the said embodiment, although the cation exchange resin is accommodated in the upper chamber 20 and the anion exchange resin is accommodated in the chamber 30, you may reverse. In the said embodiment, although the upper chamber 20 and the basement 30 communicate with each other via the piping 5, 11, 8, it is not limited to this, as long as it pulls out and surrounds the exterior of the tower body 1. In addition, although three valves 7, 10, and 12 are used in this embodiment, you may make it flow path switch using two three-way valves.

Next, with reference to FIG. 2, embodiment of the water treatment apparatus of this invention is described.

2 is a flowchart of a water treatment apparatus according to the embodiment. The raw water is passed through the ion exchange device 42 after the hardness component is removed by the hardness component removing means 41. This ion exchange apparatus 42 has the structure shown to FIG. 1A, 1B, The inside of the tower body 1 is divided into two chambers by the partition plate 2, and the anion exchange resin 31 is filled in the room, The cation exchange resin 21 is filled in the loss. The raw water from which the hardness component is removed is first contacted with the anion exchange resin 31 to remove anion, and then contacted with the cation exchange resin 21 to remove the cation, thereby becoming treated water.

Moreover, a reverse osmosis apparatus (RO apparatus), an ion exchange apparatus, etc. are mentioned as a hardness component removal means. Only one stage may be used for these hardness component removal means, and two or more stages may be connected in series, and two or more types of hardness component removal means may be connected in series. Illustrating the configuration of the water treatment apparatus of the present invention including the hardness component removing means, the following (a)? same as (j).

(a) RO-ion exchange device according to the present invention

(b) RO-RO-ion exchange apparatus according to the present invention

(c) RO-degassing apparatus-Ion exchange apparatus which concerns on this invention

(d) Degassing apparatus-RO-ion exchange apparatus which concerns on this invention

(e) Degassing apparatus-RO-RO-Ion exchange apparatus which concerns on this invention

(f) RO-degassing apparatus-RO-ion exchange apparatus which concerns on this invention

(g) RO-RO-deaerator-ion exchange device according to the present invention

(h) Ion Exchange Device—Ion Exchange Device According to the Present Invention

(i) Ion exchange apparatus-degassing apparatus-ion exchange apparatus which concerns on this invention

(j) Ion exchange apparatus-degassing apparatus-ion exchange apparatus-ion exchange apparatus which concerns on this invention

In the ion exchange device 42 of this water treatment device, the water to be treated is passed through anion exchange resin 31 to cation exchange resin 21 in order, that is, as shown in FIG. 1A, the valve 12 is opened. Opening, closing the valves 7 and 10, and collecting the raw water from the lower supply and drain pipe 13, the collecting and draining member 14, the anion exchange resin 31, the inert resin 32, and the collecting and draining member 9. , The communication piping 8, 12, 5, the drainage member 6, the cation exchange resin 21, the inert resin 22, the drainage member 4, and the upper supply and drainage pipe 3 in order. Even if metal ions such as Na are eluted from the anion exchange resin 31, these metal ions are captured by the cation exchange resin 21 and are not leaked in the treated water. Further, the cation exchange capacity of the cation exchange resin 21 is obtained by first contacting the anion exchange resin 31 with the treated water having a high pH (lower H ⁺ ion concentration) with the cation exchange resin 21. This greatly increases. For this reason, the treated water with favorable water quality is obtained. In addition, since raw water is treated by the hardness component removing means 41 to remove the hardness component and then passed through to the ion exchange device 42, the scale component is also prevented from adhering to the anion exchange resin 31. Can reliably flow through.

<Necessary resin volume ratio>

As shown in Table 1 below, ion exchange resins typically differ in total exchange capacity in cation exchange resins and anion exchange resins. In general, if the cation exchange resin has a large total exchange capacity, and the ions in the water supply are cation and anion equivalents, it is preferable to make the amount of the anion exchange resin large in volume compared to the cation exchange resin. For example, the volume of the anion exchange resin is 1.5? Of the volume of the cation exchange resin. 5 times is preferable. In addition, when it is necessary to improve the removability of weak bases such as boron and silica, as shown in the following example, the volume resin ratio is not only adjusted to the total exchange capacity, but also at a volume resin ratio that matches the actual exchange capacity of these weak bases. It is desirable to.

Example

Hereinafter, an Example, a reference example, and a comparative example are demonstrated.

Example 1, Comparative Example 1

In Example 1, the ion exchange apparatus shown in FIGS. 1A and 1B was used. The specifications are as follows.

Top diameter: 450 mm

Top height: 3000 mm

Loss volume: 190 ℓ

Volume: 260 ℓ

Filling amount of cation exchange resin 21: 150 L

Filling amount of anion exchange resin (31): 200 L

Filling amount of inert resin 22: 30 L

Filling amount of inert resin 32: 30 l

In Comparative Example 1, a commercially available mixed phase ion exchange device was used. The specifications are as follows.

Top diameter: 450 mm

Top height: 4000 mm

Volume: 640 ℓ

Filling amount of cation exchange resin: 150 ℓ

Filling amount of anion exchange resin: 200 ℓ

In Example 1 and Comparative Example 1, the following were used as the anion exchange resin and the cation exchange resin.

Anion exchange resin: Strong basic anion exchange resin `` Dow 550A ''

Cation Exchange Resin: Strong Acid Cation Exchange Resin `` Dow 650C ''

RO treated water (conductivity: 5 μS / cm, metal Na: 1 ppm, chloride ion: 1 ppm, SiO ₂ : 1 ppm) was passed through each ion exchanger for a predetermined time, and then the following acid solution and alkaline solution were used. At the same time, regeneration was carried out to check the quality of the treated water thereafter.

(1) operating conditions

    RO treated water flow rate: 15 ㎥ / h

(2) playback conditions

    Acid solution

       HCl concentration: 5 wt%

       Water flow rate: 0.75 ㎥ / h, 30 minutes

    Alkaline solution

       NaOH concentration: 5 wt%

       Water flow rate: 1 ㎥ / h, heated 40 ℃, 40 minutes

<Play time comparison>

The regeneration time (min) of the ion exchange apparatus of Example 1 was 40 (drug passing time) + 40 (drug extrusion time by pure water) + 5 (drain while washing with pure water) + 15 (circular washing of pure water) = 100 min It was.

On the other hand, the regeneration time of the conventional mixed bed type ion exchanger of Comparative Example 1 was 10 (resin separation time) + 30 (cation exchange resin: chemical liquid passing time) + 30 (cation exchange resin: chemical extrusion time) + 40 (no On-exchange resin: chemical passing time) + 40 (no-ion exchange resin: chemical extrusion time) + 5 (water draining with pure water) + 15 (resin mixing time) + 30 (circulation washing) = 200 min.

In the ion exchange apparatus regenerated in this Example 1 and the comparative example 1, Table 2 shows the time-dependent change of the specific-resistance value of the treated water at the time of passing through said RO treated water on the same conditions, and starting a collection process. In addition, Table 3 shows the quality of the treated water at the time point 1 hour after the start of regeneration after regeneration.

As is apparent from Tables 2 and 3, according to the present invention, it is possible to shorten the water quality rise time due to reverse regeneration (Table 2) and high purity (Table 3), as compared with the conventional mixed bed ion exchange column. Since the on-exchange resin and the cation exchange resin can be regenerated at the same time, the regeneration time can also be reduced by half, and the apparatus cost and the installation area are equal or less.

[Example 2]

The simulated raw water described later was passed through the RO device as the hardness component removing means, and then passed through the ion exchange device shown in FIGS. 1A and 1B. The main conditions of this ion exchange apparatus are as follows.

(1) ion exchange resin

    Cation Exchange Resin: Dow 650C, Filling 300ml

    Anion Exchange Resin: Dow 550A, 600ml Filling

(2) Water flow rate: 1 L / min

(3) playback conditions

The regeneration solution is as follows.

    HCl aqueous solution: 5 wt% HCl concentration, water flow rate: 1 L / h, 30 minutes

    NaOH aqueous solution: NaOH concentration of 5% by weight, water flow rate: 2 L / h, warming 40 ° C., 30 minutes

The regeneration solution was passed through as follows.

    30 minutes (drug passing time) → 30 minutes ultra-pure water (drug extrusion time) → 15 minutes raw water flow (driving time)

(4) RO device

The main conditions of the RO device are as follows.

    RO membrane: ES-20-D (Nitto Corporation)

    RO operating condition: 75% recovery rate

    RO treated water Mg concentration: 1 mg / l

    Na concentration: 1 mg / l

(5) Manufacturing method of simulated raw water

The simulated raw water was prepared by dissolving 60 mg / L-asCa and 50 mg / L-asNa of MgCl ₂ in ultrapure water, respectively, and degassing by membrane degassing. The degassing film used was Liqui-Cel DX-50 (Selgard).

(6) results

As a result, as shown in Table 4, the Na concentration in the treated water after 1 Hr of water after regeneration was 1 ppt (ng / L) or less. The Na concentration of the treated water for 360 hours from the start of water passage is shown in FIG. 3.

Comparative Example 2

Simulated raw water was treated in the same manner as in Example 2 except that the simulated raw water was passed directly to the ion exchanger without passing through the RO device.

In this case, the scale of magnesium hydroxide generate | occur | produced in the anion exchange resin layer immediately after water flow start, and it became difficult to continue water flow.

[Referential Example 1]

In Example 2, the simulated raw water was passed through the RO apparatus, first through the cation exchange resin, and then through the anion exchange resin. That is, the water flow order of anion exchange resin and cation exchange resin was reversed to Example 2. Other than this was carried out similarly to Example 2, and passed through. As a result, as shown in Table 4, it was observed that the Na concentration in the treated water after 1 Hr at the time of water passage after regeneration was 3 ppt, which was several times or more the concentration of Example 2. The Na concentration of the treated water for 360 hours from the start of water passage is shown in FIG. 3.

Comparative Example 3

Same as Example 2 except that the anion exchange resin and the cation exchange resin used in Example 2 were used in the same amount as in Example 2, and the mixture was mixed to form a mixed phase and the water flow during regeneration was as follows. Water flow was performed on conditions. As a result, as shown in Table 4, the Na concentration in the treated water after 1 Hr of water after regeneration was 52 ppt. The Na concentration of the treated water for 360 hours from the start of water passage is shown in FIG. 3.

<Water flow at the time of reproduction in the comparative example 3>

Pass 20 minutes ultrapure water upstream at 0.3 ℓ / min (resin separation time) → (30 minutes (chemical (HCl) liquid) → 30 minutes ultra pure water (chemical extrusion)) → (30 minutes (chemical (HCl) liquid)) → 30 minutes ultra pure water (chemical extrusion) → 15 minutes ultra pure water (resin mixing) → 30 minutes (operation switching time)

[Review]

As shown in Table 4 and FIG. 3, the present invention can stably produce high-quality treated water.

While the invention has been described in detail using specific embodiments, it will be apparent to those skilled in the art that various changes may be made without departing from the spirit and scope of the invention.

In addition, this application is based on the Japanese patent application (patent application 2009-227453) filed on September 30, 2009 and the Japanese patent application (patent application 2010-059390) filed on March 16, 2010, The whole is incorporated by reference.

1: Top body
1b, 1c: hard board
2: partition plate
3: upper supply and demand piping
4, 6, 9, 14: no water drainage
5, 8, 11: communication piping
13: lower supply pipe
20: loss
30: you
41: hardness component removal means
42: ion exchange device

Claims (7)

In the tower body for the ion exchange apparatus filled with the ion exchange resin therein,
In the tower body, the loss and the basement are partitioned by a water-repellent partition plate,
The tower body for ion exchange apparatus characterized by the loss | disconnection and a basement communicate with the communication means enclosed outside the tower body and enclosed. The tower body for ion exchange apparatus of Claim 1,
Loss of the tower body and the cation exchange resin housed in one of the basements,
An ion exchange device comprising an anion exchange resin housed in the other. The method of claim 2,
An upper supply and drain pipe for supplying or discharging a liquid to an upper portion of the loss,
The lower supply-discharge piping for supplying or discharging a liquid in the lower part of the basement is provided, The said communication means,
A first communication pipe for supplying liquid to the lower part of the loss,
A second communication pipe for supplying liquid to the upper part of the basement,
A third communication pipe communicating the first communication pipe and the second communication pipe,
Opening and closing means of the third communication pipe,
And an air supply / discharge means for regeneration liquid formed in each of the first communication pipe and the second communication pipe. The method of claim 3, wherein
At the upper part of the loss, the lower part of the loss, the upper part of the cellar and the lower part of the cellar, a collecting and draining member for passing water but preventing passage of the ion exchange resin is disposed,
An end of each of the upper supply pipe, the first communication pipe, the second communication pipe, and the lower supply pipe is connected to the collector member. The method of claim 4, wherein
A granular inert resin is filled in the upper part of the upper chamber and the upper chamber of the chamber, respectively, and the collecting and draining member of the upper chamber and the lower chamber of the chamber are embedded in the inert resin, respectively. The water treatment apparatus which has the ion exchange apparatus in any one of Claims 2-5, and the hardness component removal means formed in the front end of this ion exchange apparatus. The method according to claim 6,
And said ion exchange device is configured such that the water to be treated first comes into contact with the anion exchange resin and then with the cation exchange resin.

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