JPH08309348A - Deodorizing apparatus of ion exchange pure water - Google Patents

Abstract

PURPOSE: To provide a deodorizing system removing an offensive smell substance in ion exchange pure water. CONSTITUTION: The upper part of one ion exchange column is packed with the regenerated mixed resin bed of a mixed bed type pure water making part and the lower part thereof is packed with a strongly acidic cation exchange resin polisher part regenerated to a hydrogen type and raw water is passed through the upper bed to make ion exchange pure water which is, in turn, passed through the lower bed to remove an offensive smell substance in pure water to obtain odorless pure water.

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a deodorizing system for ion-exchanged pure water for removing odorous substances contained in ion-exchanged pure water obtained by treating raw water with a mixed bed type pure water producing apparatus. Is.

[0002]

2. Description of the Related Art Conventionally, pure water is obtained by treating raw water such as tap water with a mixed bed type pure water producing apparatus configured to pass a mixture layer of a strongly acidic cation exchange resin and a strongly basic anion exchange resin. Is widely practiced in food manufacturing and other fields.

In these mixed bed type pure water producing apparatuses, since the odorous substance leaking from the strongly basic anion exchange resin is contained in the ion-exchanged pure water after the treatment, the product has an odor in the field of food production and the like. It was a big problem because of problems such as. In order to solve this problem, in the past, for example, “Activated Carbon Water Treatment Technology and Management”, Nikkan Kogyo Shimbun (1978), 130
As disclosed in the page, a method for deodorizing treated ion-exchanged pure water with activated carbon is performed.

[0004]

However, the conventional method using the above-mentioned activated carbon has the following drawbacks (1) to (3). (1) Contamination of treated water with salt and alkali: When ion-exchanged pure water is treated with activated carbon, impurities such as salt and alkali are eluted from the activated carbon into the treated water to contaminate the treated water.
It significantly increases the electrical conductivity of deionized deionized pure water and makes the pH more alkaline than neutral to significantly reduce the purity. Therefore, activated carbon cannot be used at all for deodorizing the high-purity pure water obtained by the mixed bed type pure water producing apparatus. (2) Contamination of treated water by microorganisms: Activated carbon has a porous structure and serves as a perfect residence for microorganisms, so many microorganisms propagate in activated carbon. Therefore, when ion-exchanged pure water is treated with activated carbon, these microorganisms are contaminated by contaminating the treated water, and the treated water becomes unsanitary and cannot be used for food production. (3) Necessity of complicated regeneration and sterilization of activated carbon:
In order to restore the odor removing ability of the activated carbon and to sterilize the microorganisms propagated in the activated carbon, it is necessary to bake the activated carbon or treat it with high-temperature steam. Must be done often.

The object of the present invention is to solve the above problems,
Let's provide a rational deodorization system for mixed-bed ion-exchange pure water that removes odorous substances in ion-exchange pure water by passing them through a hydrogen-type strongly acidic cation-exchange resin layer and polishing them to eliminate odors. It is what

[0006]

Means for Solving the Problems The deodorizing system for ion-exchanged pure water of the present invention is an ion produced by a mixed bed type pure water producing section having a mixed resin tower of a strongly acidic cation exchange resin and a strongly basic anion exchange resin. The odorous substance in the exchanged pure water is removed by passing it through a polishing section having a hydrogen-type strongly acidic cation exchange resin layer provided in the lower part of the mixed resin tower. In the above system, it is preferable to use, as the strongly acidic cation exchange resin of the polishing section, one having a sedimentation rate higher than that of the strongly acidic cation exchange resin of the mixed bed type pure water producing section. The mixed bed type ion exchange pure water deodorizing system of the present invention includes the following two methods. (1) System for forming a mixed bed layer by introducing gas from the interface between the regenerated strong acid cation exchange resin in the mixed bed type pure water production section and the regenerated strong acid cation exchange resin in the polishing section: In a system having a strongly acidic cation exchange resin layer below the mixed resin layer of the mixed bed type pure water production unit, in performing the regeneration of the system,
First, water is passed from the lower part of the strong acid cation exchange resin layer of the polishing part in an upward flow to perform backwashing, whereby the strong basic anion exchange resin layer, the strong acid cation exchange resin layer, and the polishing part from the upper part. The strong acid cation exchange resin layer is separated. Next, the strongly basic anion exchange resin is regenerated with a caustic aqueous solution, and the strongly acidic cation exchange resin is regenerated by passing the aqueous mineral acid solution upward from the bottom of the resin tower, and then the strongly acidic cation exchange resin in the polishing section is first used. Resin layer,
Then, it is continuously passed through the strong acid cation exchange resin layer of the mixed bed type pure water production section for regeneration, and then the strong acid cation exchange resin layer of the regenerated mixed bed pure water production section and the regenerated polishing section By introducing a gas such as air or nitrogen from the interface with the strongly acidic cation exchange resin layer and allowing it to diffuse upward, the mixed resin layer of the mixed bed type pure water production unit is provided above the interface and the polishing is performed at the bottom. This is a deodorization system for mixed-bed ion-exchanged pure water, which forms two layers of strong acid cation-exchange resin layer in some parts. (2) In the above system, the resin mixing gas is introduced from the lowermost part of the resin tower, and the polishing part is formed in the lower layer and the mixed bed type pure water producing part is formed in the upper part: In (1), the resin mixing gas Is introduced from the bottom of the regenerated strong acid cation exchange resin layer for polishing and is diffused upward to mix all the resin layers, then gas introduction is stopped to form a polishing layer on the lower side, and mixed with the upper portion. This is a mixed bed type ion exchange pure water deodorizing system for forming a bed type mixed resin layer.

[0007]

[Function] The ion-exchanged pure water produced by the mixed bed type pure water production section having a mixed resin layer of a hydrogen-type strongly acidic cation exchange resin and a hydroxyl-type strongly basic anion exchange resin has a strong basic anion exchange. There are odorous substances based on amines generated from the resin. These odorous substances are mainly a small amount of eluate leaked from the strongly basic anion exchange resin and amines which are decomposition products of the quaternary ammonium group,
It produces an amine odor. The present invention provides a polishing section having a hydrogen-type strongly acidic cation exchange resin layer below the mixed resin layer, and removes these amine odor-producing substances from the ion exchange pure water to obtain the ion exchange pure water. It is odorless.

Further, the hydrogen-type strongly acidic cation exchange resin layer used as the polishing section always uses a new mineral acid for each regeneration when the strongly acidic cation exchange resin constituting the mixed resin layer is countercurrently regenerated with the mineral acid. As a result, the treatment is preferentially and sufficiently carried out, so that it can be sufficiently regenerated, sterilization and disinfection can be carried out, and microbial contamination of the treated water can be prevented.

[0009]

DESCRIPTION OF THE PREFERRED EMBODIMENTS FIG. 1 is a diagram for explaining in principle an example of a deodorizing system for ion-exchanged pure water according to the present invention. In FIG. 1, raw water such as tap water is passed through a regenerated mixed-bed mixed resin layer filled in the upper layer of only one tower to obtain ion-exchanged pure water, and then the same ion-exchange tower. The deodorized ion-exchanged pure water is obtained as treated water by passing water through the polisher portion having the hydrogen-type strongly acidic cation exchange resin filled in the lower layer.

2 to 18 are views for explaining an example of the mixed bed type ion exchange pure water deodorizing system of the present invention.
8 to 8 show a partial mixing method of a strongly acidic cation exchange resin and a strongly basic anion exchange resin, FIGS. 9 to 11 show a total mixing method thereof, and FIGS. 12 to 18 show a strong acid cation exchange resin having a large sedimentation rate. The total amount mixing method in the case of containing one is shown.

First, a partial mixing system of a strongly acidic cation exchange resin and a strongly basic anion exchange resin will be shown. FIG. 2 shows the packed state of the ion exchange resin in the ion exchange tower T. Reference numeral 1 is a strongly acidic cation exchange resin layer, and 2 is a mixed bed type strongly basic anion exchange resin layer. FIG. 3 shows a state during backwash separation which is carried out prior to regeneration of the ion exchange resin. 1'is a cation exchange resin slurry, 2'is a strongly basic anion exchange resin slurry, and W is an uppermost aqueous layer of the ion exchange column. Is. FIG.
Shows the sedimentation state of the ion exchange resin after backwash separation,
1 ″ represents a strongly acidic cation exchange resin layer, and 2 ″ represents a strongly basic anion exchange resin layer. FIG. 5 shows the regenerated state of the ion exchange resin. The strongly basic anion exchange resin layer 2 ′ ″ is a strong acid cation exchange resin layer 1 ′ washed with raw water by passing a caustic aqueous solution in a downward flow. In ″, an aqueous mineral acid solution is passed through in an upward flow and washed with pure water or treated odorless pure water to regenerate each. FIG. 6 shows a partial mixing of both ion exchange resins. A gas such as air or nitrogen is supplied from a partial mixing gas diffuser A provided at a position which should be the upper end of the polisher part 3 made of a hydrogen-type strongly acidic cation exchange resin. Is introduced and diffused upward, and then exhausted from above the ion exchange tower, and both ion exchange resins are mixed by stirring to mix resin slurry 4 in the mixed bed type pure water production section.
To form. FIG. 7 shows a layer fixing / washing operation of the mixed resin layer after mixing, in which raw water is immediately passed from the upper part of the ion exchange tower and discharged from the lowermost part of the ion exchange tower to fix the mixed resin layer and Wash all resin layers thoroughly,
At the bottom of the resin tower, a polisher section 3 made of a regenerated hydrogen-type strongly acidic cation exchange resin is provided, and a mixed bed type pure water producing section 5 having a regenerated mixed resin layer is formed on the polisher section 3. FIG. 8 shows a treatment process in which raw water is passed from the upper part of the ion exchange column to produce odorless pure water from the lowermost part of the ion exchange column. At this time, the strong acid cation exchange resin layer 1 may be divided into a net for the mixed bed type pure water production section and a polisher section in advance at the position of the partial mixing gas diffuser A.

Next, the total amount mixing method described above will be described. Fig. 9 shows the case of total mixing of both ion exchange resins. A gas diffuser A'for total mixing provided at the bottom of the ion exchange tower introduces gas such as air or nitrogen to the upper part to diffuse the gas upward. Then, the mixture is evacuated from above the ion exchange tower, and the whole amount of the ion exchange resin is stirred and mixed to form the mixed resin slurry 6. FIG. 10 shows a layer fixing / washing operation of the resin after mixing the whole amount. First, the gas introduction is stopped to stop the gas mixing operation, and the polisher section 7 made of a hydrogen-type strongly acidic cation exchange resin is provided at the bottom of the ion exchange tower. Immediately after the formation, raw water is passed from the upper part of the ion exchange tower and discharged from the lowermost part of the ion exchange tower, and the mixed bed type pure water producing section 8 having the regenerated mixed resin layer is fixed and washed. FIG. 11 shows a treatment process in which raw water is passed from the upper part of the ion exchange tower and odorless pure water is produced from the lowermost part of the ion exchange tower.

[0013] Next, in the above total mixing method, the total amount of the strong acidic cation exchange resin having a higher sedimentation rate than the strong acidic cation exchange resin of the mixed bed type pure water production section is used as the resin of the polisher section. The method will be described. Figure 12 shows the state of filling the ion exchange resin in the ion exchange tower,
Reference numeral 9 indicates a strong acidic cation exchange resin layer having a large sedimentation rate which serves as a polisher portion, 10 indicates a strong acid cation exchange resin layer of a mixed bed type pure water producing section, and 2 indicates a mixed bed type as described above. The strongly basic anion exchange resin layer of a pure water manufacturing part is shown. Figure
Reference numeral 13 shows a state during backwash separation which is carried out prior to regeneration of the ion exchange resin. 9'is a large sedimentation rate at the time of backwash expansion, slurry for a polisher part made of a strongly acidic cation exchange resin, 10 '.
Indicates the strongly acidic cation exchange resin slurry in the mixed bed type pure water production section at the time of backwash expansion, and 2'indicates the strongly basic anion exchange resin slurry at the time of backwash expansion as described above. Fig. 14 shows the sedimentation state of the ion exchange resin after backwash separation.
Indicates a large settling speed, a polisher part made of a strong acid cation exchange resin, 10 ″ indicates a strong acid cation exchange resin layer of a mixed bed type pure water producing section, and 2 ″ indicates a mixed bed type pure water producing section as described above. The strongly basic anion exchange resin layer of is shown. FIG. 15 shows a regenerating operation of the ion exchange resin layer. The strong basic anion exchange resin layer 2 ″ ′ is fed with a caustic alkaline aqueous solution in a downward flow as described above, and washed with raw water. Hydrochloric acid type is regenerated by discharging reclaimed wastewater from the bottom of the bed, and strong acid cation exchange resin layer 1 in the mixed bed type pure water production section 1
The large settling rate of 0 ″ ″ and the polisher part The strongly acidic cation exchange resin layer 9 ″ ″ is passed through an aqueous mineral acid solution from the lowermost part of the ion exchange column in an upward flow to obtain pure water or treated odorless pure water. By washing and discharging the drainage water from the upper part of the 10 "layer, they are all regenerated into hydrogen type. FIG. 16 shows the total mixing of all the ion exchange resins. A gas such as air or nitrogen is introduced from the total amount mixing gas diffuser A ′ provided at the bottom of the ion exchange column to diffuse the gas upward and to perform ion exchange. Evacuation is performed from above the tower, and all the ion exchange resins are mixed by stirring to form a mixed resin slurry 11. Fig. 17 shows the resin layer fixing / washing operation after mixing. First, the introduction of gas is stopped to stop the gas mixing operation, and the hydrogen type strong acid having a large sedimentation speed is quickly and efficiently at the bottom of the ion exchange column. Immediately after forming the polisher part 12 made of a cation exchange resin, raw water is passed from the upper part of the ion exchange column and discharged from the lower part of the ion exchange column, fixing and washing the regenerated mixed bed type pure water producing part 13. To do. The formation of the polisher portion can be performed more quickly and efficiently than the formation of the polisher portion having a normal sedimentation rate in FIG. Immediately thereafter, raw water is passed through the upper part of the ion exchange tower and discharged from the lowermost part of the ion exchange tower to fix and wash the regenerated mixed bed type pure water producing section 13. FIG. 18 shows a treatment process in which raw water is passed from the upper part of the ion exchange tower and odorless pure water is produced from the lowermost part of the ion exchange tower.

The technical requirements of each structure used in the present invention will be described in detail below.

(1) Ion-exchanged pure water: High-purity pure water obtained by passing raw water through a mixed-bed type pure water production section in which a hydrogen type strongly acidic cation exchange resin and a hydroxyl group type strongly basic anion exchange resin are mixed. Refers to water.

The ion-exchanged pure water in the mixed bed type pure water production section is of high purity with an electric conductivity of about 1 μS / cm or less (25 ° C.) and a pH of about 7, but it is strongly basic. Amine compounds such as trimethylamine and dimethylethanolamine generated by decomposition of anion-exchange resin and decomposition of quaternary ammonium groups are included, but most of them are adsorbed and removed by the adjacent hydrogen-type strongly acidic cation-exchange resin. . However, the eluate and amine odor substance generated from the strongly basic anion exchange resin existing in the lower part of the mixed bed column have few opportunities and time for contact with the adjacent strongly acidic cation exchange resin, so that a considerable amount of amine odor is generated. The result is that it remains in the treated water.

(2) Strong acidic cation exchange resin and strong basic anion exchange resin used in the mixed bed type pure water production section: Strong acidic cation exchange resin and strong used in the mixed bed type pure water production section As the basic anion exchange resin, all the usual ion exchange resins for mixed beds are used.

(3) Strong Acid Cation Exchange Resin for Polishing: As the strong acid cation exchange resin for polishing, all the strong acid cation exchange resins used in a general mixed bed type pure water production unit which are generally used are used. When the total amount of ion-exchange resin is mixed, the sedimentation rate of hydrogen-type strongly acidic cation-exchange resin particles in the polisher is higher than the sedimentation rate of hydrogen-type strongly acidic cation-exchange resin particles used in the mixed bed pure water production section. It is preferable to use the other ones because the layer fixation after mixing can be performed quickly and efficiently. To select ion-exchange resin particles with a high sedimentation rate, use spherical resin particles, and either the resin particle size is large or the resin matrix structure is a copolymer of styrene and divinylbenzene (DVB). In this case, it is necessary to select one with a high degree of crosslinking (DVB%). Alternatively, those having both of these properties have a higher sedimentation rate. Table 1 shows an example of selection of a strongly acidic cation exchange resin having a high sedimentation rate.

[0019]

[Table 1]

Table 1 shows the properties of an example of the strongly acidic cation exchange resin used in the mixed bed type pure water producing section.
Shows an example of a resin in which the DVB of the resin matrix was increased from 8% to 10% and the true density was increased from about 1.26 to about 1.32 to increase the sedimentation rate. This is an example of a resin having a large particle size to further increase the sedimentation rate.

The hydrogen type strong acid cation exchange resin in the polisher part having a high sedimentation rate is used in combination with the strong acid cation exchange resin in the mixed bed type pure water production part to be used in the case of the partial mixing system of FIGS. It is also possible to do so.

Sterilization and disinfection of microorganisms by regenerating or regenerating ion exchange resin: Strongly basic anion exchange resin is a caustic alkaline aqueous solution at room temperature to 60 ° C., and strongly acidic cation exchange resin is a mineral acid aqueous solution at ordinary temperature. When the adsorbed amine odor substance cannot be desorbed sufficiently from the strongly acidic cation exchange resin in the mixed bed type pure water production section or the polisher section, it is regenerated by the regeneration cycle treatment, and a hot caustic alkali aqueous solution at 30 to 60 ° C Since regenerative treatment is performed by washing with water or hot water, strong base anion exchange resin and strong acid cation exchange resin are sterilized and disinfected during such regeneration treatment and regeneration treatment.
It is possible to prevent the deodorized water of ion-exchanged pure water from being contaminated with microorganisms.

Hereinafter, the present invention will be described in more detail with reference to actual examples. Example 1 An ion exchange column was filled with a strongly acidic cation exchange resin and a type I strongly basic anion exchange resin for a mixed bed type pure water production section and a polisher section, and backwashing separation, sedimentation and regeneration were performed to perform partial mixing and The layer is fixed and washed to prepare a system that has the mixed resin layer of the mixed bed type pure water production section as the upper layer and the polisher part of the hydrogen-type strongly acidic cation exchange resin as the lower layer, and deodorizes the ion-exchanged pure water. The results were as follows. The raw water used was tap water, and in the washing of the mixed resin layer and subsequent production of deodorized ion-exchanged pure water, the tap water was treated with activated carbon to make it odorless and used as odorless raw water.

(1) Filling with ion exchange resin: inner diameter 50 mm,
Using a 2,000 mm high ion exchange column, add raw water to a water depth of approximately 1 m, and add Ionac C-249 manufactured by Sybron Chemical Co. of the United States as a strongly acidic cation exchange resin to the lower layer to obtain 1.00 L (layer height). Purolite manufactured by Purolite of the United States as a type I strong basic anion exchange resin.
A-400E is charged to fill the upper layer with 1.00 L (layer height 51.0 cm), and the total ion exchange resin filling amount is 2.00 L (total layer height 102.
0 cm). The resin filling amount is measured by a standard method.
Backwashing and natural sedimentation were repeated.

(2) Separation by backwash and sedimentation: Raw water was introduced from the bottom of the ion exchange column, and backwashed for 20 minutes so that the total expansion rate of the resin layer was about 60%, to remove both ion exchange resin slurries. After separation, backwashing was stopped and both resin layers were allowed to settle spontaneously, and a Purolite A-400E layer was separated as an upper layer and an Ionac C-249 layer was separated as a lower layer.

(3) Regeneration: Regeneration was carried out according to the usual regeneration method of the mixed bed type pure water producing section. Upper Purolite A-400E
Is a downward flow of 5% NaOH at 50 ℃ as a regenerant at SV 3 / h 1.
After replenishing for 5 hours, raw water at 50 ° C was passed for 20 minutes at SV 3 / h to replace the regenerating solution, and the raw water at 50 ° C was washed for 90 minutes at SV 20 / h for regeneration. Ionac C-249 in the lower layer was treated with 5% HCl at room temperature for 1 hour at SV 3 / h as a regenerant in an upward flow, and then treated with odorless pure water at room temperature for 20 minutes at SV 3 / h. The regenerated liquid was replaced with water to replace the regenerated liquid, followed by washing with SV20 / h for 60 minutes to regenerate. The regenerated waste water of both ion exchange resins was discharged to the outside of the ion exchange tower via a collector provided on the boundary surface of both ion exchange resin layers by a conventional method.

(4) Partial mixing: The water level on both ion exchange resin layers was set to about 30 cm, and the water level on the lower side of the lower Ionac C-249 layer was adjusted to about 30 cm.
Compressed air was introduced into the gas dissipator for partial mixing installed at the top of 27 cm, and the air was diffused upward for about 3 minutes and exhausted from the top of the ion-exchange tower. Mix the top layer of Ionac C-249 with the entire top layer of Purolite A-400E. On this occasion,
The layer of Ionac C-249 below the gas diffuser becomes the polisher part of the hydrogen-type strongly acidic cation exchange resin without mixing.

(5) Layer fixing / washing: The above mixing operation was stopped, and odorless raw water was immediately drained from the bottom of the ion exchange tower while passing 40 L / h of water from the top of the ion exchange tower. Fix the mixed resin layer of the production department, and then pass the odorless raw water at the same flow rate to wash the mixed resin layer of the mixed bed type production department and the lower layer of the posi- rier unit, and discharge electricity from the bottom of the ion exchange tower. The conductivity was adjusted to less than 0.5 μS / cm (25 ° C). It took about 30 minutes.

(6) Production of odorless ion exchange pure water: Odorless raw water was passed through the ion exchange tower at 40 L / h (SV 27 / h for mixed bed layer, SV 80 / h for polisher layer). Deodorized ion-exchanged pure water was collected as treated water from the bottom of the ion-exchange tower. Table 2 below shows the treatment results of ion-exchanged pure water and deodorized ion-exchanged pure water that has passed through the polisher layer.

[0030]

[Table 2]

From the results shown in Table 2, the mixed-bed ion-exchanged pure water produced by using the type I strongly basic anion exchange resin had a fishy amine odor, but the hydrogen type strongly acidic cation exchange was used. By the treatment with the resin polisher, all such amine odors are removed to make it odorless, and the electric conductivity (conductivity) is 0.17 to 0.18 μS / cm (25 ° C) of ion-exchanged pure water.
It was found that the odorless pure water of good quality can be easily and stably obtained by using only one ion-exchange tower.

Example 2 An example in which a type II type instead of type I type is used as the strongly basic anion exchange resin used in the mixed bed type pure water producing section in Example 1. The other ion exchange resins and the operating procedure are the same as in Example 1.

(1) Packing with ion exchange resin: An ion exchange column similar to that used in Example 1 was used, and as the type II strong basic anion exchange resin, Ionac AS manufactured by Sybron Chemical Co. of the United States was used.
B-2HP was used, and as the strongly acidic cation exchange resin, the same Ionac C-249 as in Example 1 was used. The filling quantity and filling method of each ion-exchange resin are the same as in Example 1.

(2) Backwash separation and sedimentation: Both ion exchange resins were backwashed and separated in the same manner as in Example 1, and Ionac AS was added to the upper layer.
The B 2 HP layer and the lower layer, the Ionac C-249 layer, were separately packed.

(3) Regeneration: The method and apparatus for regenerating both ion exchange resins are the same as in Example 1, but Io
The regenerated liquid of nac ASB-2HP was 5% NaOH at 35 ℃, and SV 3 / h
The difference is that the raw water at 35 ° C was passed for 20 minutes at SV 3 / h for 20 minutes to replace the regenerating solution, and the raw water at 35 ° C was washed for 90 minutes at SV20 / h for regeneration.

(4) Partial mixing: The same procedure as in Example 1 was used, but Ionac ASB was used instead of Purolite A-400E in the upper layer.
-2HP is the only difference.

(5) Layer fixing / washing: The same procedure as in Example 1 was carried out.

(6) Production of odorless ion-exchanged pure water: The same procedure as in Example 1 was carried out. Table 3 below shows the treatment results of ion-exchanged pure water and deodorized ion-exchanged pure water that has passed through the polisher section.

[0039]

[Table 3]

From the results shown in Table 3, the mixed-bed type ion-exchanged pure water produced by using the type II strong basic anion exchange resin had an aromatic amine odor, but the hydrogen type strong acidic cation exchange resin was used. The treatment with the polisher removes all such amine odors and makes them odorless, and the electrical conductivity (conductivity) is 0.22 to 0.23 μS / cm (25 ° C) of ion-exchanged pure water of 0.
It was found that the odorless pure water of good quality can be easily and stably obtained by using only one ion-exchange tower.

Example 3 An example in which the partial mixing system of the mixed bed type ion exchange resin portion is the total amount mixing system of all the ion exchange resins in Example 2 will be described. The procedure is exactly the same as in Example 2 except for the operation of performing the total amount mixing method and the operation of fixing and washing the layer after mixing.

(1) Total amount mixing: The water level on the total ion exchange resin layer is set to 60 cm, and compressed air is introduced into the total amount mixing gas dissipator provided at the lowest part of the total ion exchange resin layer to move the air upward. All the ion-exchange resins are mixed in a slurry state by being diffused for about 3 minutes and exhausted from the upper part of the ion-exchange tower.

(2) Layer fixing / washing: Stop the introduction of gas,
The resin mixing operation was stopped, and the hydrogen-type strongly acidic cation exchange resin polisher part was
Forming 25-27 cm, while immediately draining from the bottom of the ion exchange tower, odorless raw water is passed at 40 L / h from the top of the ion exchange tower, fixing the mixed resin layer of the mixed bed pure water production section, Then, the odorless raw water is passed at the same flow rate to wash the mixed resin layer of the mixed bed type pure water production section and the lower layer of the posi- ryer section. ) Less than. It took about 30 minutes.

(3) Production of odorless ion-exchanged pure water: The same procedure as in Example 2 was carried out. Table 4 below shows the treatment results of ion-exchanged pure water and deodorized ion-exchanged pure water that has passed through the polisher portion.

[0045]

[Table 4]

From the results shown in Table 4, the formation of the polisher part and the mixed resin layer of the mixed bed type deionized water producing part were carried out by the total mixing method. As a result, the mixed bed type using the type II strong basic anion exchange resin was used. Ion-exchanged pure water had an aromatic amine odor, but by the treatment with the hydrogen type strongly acidic cation exchange resin polisher, all such amine odor was removed to make it odorless, and the electric conductivity (conductivity) Is 0 for ion-exchanged pure water.
49-0.50 μS / cm (25 ° C) drops to 0.44 μS / cm (25 ° C) and stabilizes, and high-quality odorless pure water can be easily and stably obtained by using only one ion exchange tower. I found out that

Example 4 In Example 3, a hydrogen-type strongly acidic cation exchange resin having a large sedimentation rate was selected and used as the hydrogenation type strongly acidic cation exchange resin of the polisher part, and the strongly acidic cation exchange resin of the mixed bed type pure water producing part was used. An example in which the normal resin used in Example 3 is used and the mixed resin layer is formed by the total amount mixing method will be described. Other operating procedures are the same as in Example 3.

(1) Ion exchange resin used and packing: The same type II strong basic anion exchange resin as in Example 3 was used for the mixed bed type pure water production section using the same ion exchange column as in Example 3. Ionac ASB-2HP 1.00L and strong acid cation exchange resin Io
Using nac C-249 0.50L, strong acid cation exchange resin for polisher has high sedimentation rate.
It was filled using 0.50 L of the sieve fraction of ct CS-399C. Ionac
C-249 settling velocities are based on particle sizes of 16-40 ASTM
The mesh (particles -1.18 + 0.428), the degree of cross-linking is DVB 8%, and the true density is about 1.26, while the strongly acidic cation-exchange resin in the polisher with a high sedimentation rate is For the Ionac Impact CS-399C sieve product shown, the settling rate values are 16-18 ASTM mesh (particle size -1.18).
mm + 1.00 mm), the degree of cross-linking is DVB 10%, and the true density is approx.
It is as large as 1.32, and both the particle size and the true density, which are factors that increase the sedimentation velocity, are large. The filling method of each ion exchange resin is the same as that of the second embodiment.

(2) Backwash separation and sedimentation: In the same manner as in Example 3, three types of ion exchange resins were backwashed simultaneously for 20 minutes so that the total resin layer expansion coefficient was about 60%, and The ion exchange resin was separated as a slurry. After that, backwashing was stopped and each resin layer was allowed to spontaneously settle, and the upper layer was the Ionac ASB-2HP layer, the middle layer was the Ionac C-249 layer, and the lower layer was the Ionac Impact C layer.
The S-399C sieve fraction layer was separately packed.

(3) Regeneration: The same as in Example 3.

(4) Total amount mixing: The same as in Example 3.

(5) Layer fixing / washing: The same procedure as in Example 3 was carried out, but the sedimentation and fixing of the polisher portion were carried out more quickly than in the case of Example 3, so that mixing in the mixed bed type pure water producing section was carried out. There was little re-separation of the resin layer, and the layer was fixed while maintaining a good mixed state.

(6) Production of odorless ion-exchanged pure water: Odorless ion-exchanged pure water was obtained in the same manner as in Example 3.
Table 5 below shows the treatment results of ion-exchanged pure water and deodorized ion-exchanged pure water that has passed through the polisher portion.

[0054]

[Table 5]

From the results of Table 5, as a result of the deodorization system treatment of the mixed bed type ion exchange pure water by the total mixing method using the hydrogen type strongly acidic cation exchange resin having a high sedimentation rate as the polisher part, the strong type II was obtained. The mixed-bed type ion-exchanged pure water using the basic anion exchange resin had an aromatic amine odor, but the treatment with the polisher part removed all the amine odors and made them odorless, and the electric conductivity ( Conductivity) is 0.45μS / cm (25 ℃) of ion-exchanged pure water is 0.
It is stable at 41 μS / cm (25 ° C.) and the treated water of better quality than in the case of Example 3 which does not use the polisher part having a high sedimentation rate can be easily obtained by using only one ion exchange column. I understood.

[0056]

As is apparent from the above description, according to the system of the present invention, a mixed bed type pure water having a mixed resin layer of a hydrogen type strongly acidic cation exchange resin and a hydroxyl group type strongly basic anion exchange resin. Since a hydrogen-type strongly acidic cation exchange resin layer for polishing is provided in the lower part of the production unit, a substance that generates an amine odor contained in ion-exchanged pure water produced by a mixed bed type pure water production apparatus having the mixed resin layer. Can be removed to make the ion-exchanged pure water odorless.

In addition, the hydrogen-type strongly acidic cation exchange resin layer used for polishing is always regenerated by a new mineral acid at each regeneration when the strongly acidic cation exchange resin constituting the mixed resin layer is countercurrently regenerated with the mineral acid. Since the processing is performed preferentially and sufficiently, the reproduction is sufficiently performed,
Sterilization and disinfection can be performed, and microbial contamination of treated water can be prevented.

[Brief description of drawings]

FIG. 1 is a diagram illustrating the principle of a deodorizing system for ion-exchanged pure water according to the present invention.

FIG. 2 is a diagram showing a state of resin filling in the partial mixing system of the present invention.

FIG. 3 is a diagram showing a state of backwash separation in the partial mixing system of the present invention.

FIG. 4 is a diagram showing a state of sedimentation in the partial mixing system of the present invention.

FIG. 5 is a diagram showing a state of reproduction in the partial mixing system of the present invention.

FIG. 6 is a diagram showing a state of partial mixing in the partial mixing system of the present invention.

FIG. 7 is a diagram showing a state of layer fixing / washing in the partial mixing system of the present invention.

FIG. 8 is a diagram showing a processing state in the partial mixing system of the present invention.

FIG. 9 is a diagram showing a state of total volume mixing in the total volume mixing method of the present invention.

FIG. 10 is a diagram showing a state of layer fixing and washing in the total volume mixing method of the present invention.

FIG. 11 is a diagram showing a processing state in the total amount mixing method of the present invention.

FIG. 12 is a diagram showing a state of resin filling in a total sedimentation rate mixing method with a large sedimentation rate hydrogen type strongly acidic cation exchange resin of the present invention.

FIG. 13 is a diagram showing a state of backwash separation in a total sedimentation rate system containing a large sedimentation rate hydrogen type strongly acidic cation exchange resin of the present invention.

FIG. 14 is a diagram showing a state of sedimentation in a total sedimentation rate mixing method for a large sedimentation rate hydrogen type strongly acidic cation exchange resin of the present invention.

FIG. 15 is a diagram showing a state of regeneration in a total sedimentation rate system containing a large sedimentation rate hydrogen type strongly acidic cation exchange resin of the present invention.

FIG. 16 is a diagram showing the state of total volume mixing in the total volume mixing system containing a large sedimentation rate hydrogen type strongly acidic cation exchange resin of the present invention.

FIG. 17 is a diagram showing a state of layer fixation / washing in the large sedimentation rate hydrogen type strongly acidic cation exchange resin-containing total amount mixing method of the present invention.

FIG. 18 is a diagram showing the state of treatment in the large sedimentation rate hydrogen type strongly acidic cation exchange resin-containing total amount mixing method of the present invention.

[Explanation of symbols]

T Ion exchange tower, I Strongly acidic cation exchange resin layer for resin filling, 2 Strongly basic anion exchange resin layer for mixed bed type for resin filling, 1'Backwash expansion strong acidic cation exchange resin slurry, 2'Backwash expansion When strongly basic anion exchange resin slurry, W water layer, 1 ″ strongly acidic cation exchange resin layer after sedimentation, 2 ″ strongly basic anion exchange resin layer after sedimentation,
1 ″ ″ Strongly acidic cation exchange resin layer after regeneration, 2 ″ ″
Strongly basic anion exchange resin layer after regeneration, gas diffuser for A partial mixing, 3 hydrogen type strongly acidic cation exchange resin polisher part, 4 mixed resin slurry for mixed bed layer during partial mixing,
5 Regenerated mixed bed type pure water production section, A'gas mixture for total volume mixing, 6 All resin layer in total volume mixing, 7 Hydrogen type strong acid cation exchange resin polisher section, 8 Regenerated mixed bed type pure water production section , 9 Large sedimentation rate at resin filling Strong acidic cation exchange resin polisher part, 10 Strong acidic cation exchange resin layer for mixed bed at resin filling, 9'Large sedimentation rate at backwash expansion Great acidic cation exchange resin polisher slurry, 10 ' Strong acid cation exchange resin slurry for mixed bed type during backwash expansion, 9 ″ Large sedimentation rate after sedimentation Strong acidic cation exchange resin polisher part, 10 ″
Strong acid cation exchange resin layer for mixed bed type after settling, 9 ′ ″
Large sedimentation rate after regeneration Strong acidic cation exchange resin polisher part, 10 ″ ″ Regenerated strong acid cation exchange resin layer for mixed bed, 11 Total resin slurry during total mixing, 12 Large sedimentation rate Hydrogen type strong acidic cation Exchange resin polisher, 13 regenerated mixed bed pure water production

Claims (4)

[Claims] 1. A mixed bed type pure water production section having a mixed resin layer of a hydrogen type strongly acidic cation exchange resin and a hydroxyl group type strongly basic anion exchange resin, and a lower portion of the mixed resin layer of the mixed bed type pure water production section. It is possible to remove odorous substances contained in the ion-exchanged pure water generated from the mixed bed type pure water production unit by treating the polishing unit having a hydrogen-type strongly acidic cation exchange resin layer with water. Characteristic ion exchange pure water deodorization system. 2. A system having the hydrogen type strong acid cation exchange resin layer of the polishing section below the mixed resin layer of the mixed bed type pure water producing section, wherein the hydrogen type strong acid cation exchange resin layer of the polishing section is first prepared. The mixed resin layer is separated into a strong basic anion-exchange resin layer as an upper layer and a strong acidic cation-exchange resin layer as a lower layer by backwashing with water flowing upward from the lower part. The caustic is passed through the exchange resin layer in a downward flow to regenerate it, while the strong acid cation exchange resin layer is passed through with a mineral acid in an upward flow from below the strong acid cation exchange resin layer in the polishing section, Then, by passing through the strongly acidic cation exchange resin layer of the mixed bed type pure water production section to regenerate both strongly acidic cation exchange resin layers and washing each resin layer with water, the mixed bed type pure water production section Strongly acidic cation exchange resin Deodorization system of the ion-exchange purified water according to claim 1, wherein the mixing cation-exchange resin and the anion exchange resin portion of the mixed-bed water purification unit by blowing air from the end face. 3. A system having the hydrogen type strong acid cation exchange resin layer of the polishing section below the mixed resin layer of the mixed bed type pure water producing section, wherein the hydrogen type strong acid cation exchange resin layer of the polishing section is first prepared. The mixed resin layer is separated into a strong basic anion-exchange resin layer as an upper layer and a strong acidic cation-exchange resin layer as a lower layer by backwashing with water flowing upward from the lower part. The caustic is passed through the exchange resin layer in a downward flow to regenerate it, while the strong acid cation exchange resin layer is passed through with a mineral acid in an upward flow from below the strong acid cation exchange resin layer in the polishing section, Continuously, by passing through the strong acid cation exchange resin layer of the mixed bed type pure water production section to regenerate both strong acid cation exchange resin layers and washing each resin layer with water, air is blown from the bottom of all resin layers. Blowing in all Io After mixing the exchange resin layer, after the hydrogen-type strongly acidic cation exchange resin layer of the polishing part has settled to the lower layer, water is allowed to flow downward from the top of the mixed resin layer and discharged to fix the mixed resin layer. The deodorizing system for ion-exchanged pure water according to claim 1. 4. The hydrogen-type strongly acidic cation exchange resin used in the polishing section is one having a sedimentation rate higher than that of the strongly acidic cation exchange resin used in the mixed bed type pure water production section. 3. A deodorizing system for ion-exchanged pure water according to 3.