JP2014100656A - Method for regenerating amphoteric ion exchange resin - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a method for regenerating an amphoteric ion exchange resin, which can allow the amphoteric ion exchange resin to be used for treating the water exuding from a final disposal site even in a region where the quantity of water is hardly ensured.SOLUTION: The method for regenerating the amphoteric ion exchange resin comprises a step of regenerating an amphoteric ion exchange resin 16 by using a liquid (desalted water D), which is already made to pass through the amphoteric ion exchange resin and does not contain an element to be separated by the amphoteric ion exchange resin. When the desalted water D is used, the quantity of industrial water or the like to be used for regenerating the amphoteric ion exchange resin can be reduced. Calcium can be selected as the element to be separated by the amphoteric ion exchange resin. The desalted water D discharged from an electrodialysis device 17, which is disposed on the downstream side of the amphoteric ion exchange resin, can be used as the liquid which is already made to pass through the amphoteric ion exchange resin and does not contain the element to be separated by the amphoteric ion exchange resin.

Description

  The present invention relates to a method for regenerating an amphoteric ion exchange resin, and more particularly to a method for regenerating an amphoteric ion exchange resin used to prevent the generation of scale caused by calcium in a final disposal site.

  Waste disposal sites and other final disposal sites are facilities for disposing of wastes that are difficult to recycle. However, in view of the danger of exhaustion, effective use of wastes that have been treated at the final disposal site so far Is promoted.

  Incineration ash generated when municipal waste is incinerated has recently been recycled as a raw material for cement in view of the danger of depleting the final disposal site. Of municipal incineration ash, fly ash that is carried with gas and collected by the dust collector contains 10 to 20% of chlorine, so water-soluble chlorine contained in fly ash using water washing and desalination equipment After removing the compound with water, it is used as a cement raw material (see, for example, Patent Document 1).

However, in the final disposal site, calcium ions (Ca ²⁺ ) contained in the leachate and calcium sulfate (CaSO ₄ ) are generated from SO ₄ ^2- and adhere to the equipment as a scale in the filtration device and the wastewater treatment process at the later stage. However, there is a problem that stable operation is hindered.

  Therefore, for example, as shown in FIG. 5, in the final disposal site 30, the chemical reaction tank 32 removes calcium and harmful heavy metals that cause scale generation from the leachate W stored in the adjustment tank 31. A chemical such as sodium carbonate is added, and these are precipitated and removed by the filtration device 33, and then desalted by the electrodialysis device 36 through the COD treatment device 34 and the suspended substance removal device 35. As a result, the desalted water D having a water amount of 0.9Q is discharged with respect to the water amount 1Q of the leachate W, and the concentrated water C having a water amount of 0.1Q is evaporated to recover the salt.

  However, in the above method, since a large amount of sodium carbonate needs to be added, there is a problem that the drug cost increases and the operation cost increases.

The present applicant, in Patent Document 2, as shown in FIG. 6, an amphoteric ion exchange resin 41 provided on the downstream side of the suspended solids removing device 35, the leachate W of the final disposal site 30, Ca ²⁺ concentration is low, Cl ^- concentration is higher the first solution L1, high Ca ²⁺ concentration, Cl ^- concentration were separated low and the second solution L2, supplies the first solution L1 to the electrodialysis apparatus 36 In this way, we proposed a method for treating leachate from the final disposal site without the need to add a large amount of sodium carbonate. In addition, in the electrodialysis apparatus 36, the desalted water D of 1.1 to 1.4Q of water and the concentrated water C of 0.1Q of water are obtained with respect to 1Q of the leachate W, and the desalted water D is discharged. The concentrated water C is evaporated to recover the salt. Moreover, 3Q industrial water IW is used for the regeneration of the amphoteric ion exchange resin 41 with respect to the amount 1Q of the leachate W.

Japanese Patent Laid-Open No. 11-100343 Japanese Patent No. 4766719

  The treatment method of the leachate in the final disposal site described in Patent Document 2 is preferable because it does not require the addition of sodium carbonate, and can reduce the cost of the drug. However, as described above, the amphoteric ion exchange resin 41 is used. When regenerating, industrial water IW that is three times as much as leachate W is required, so there is a problem that it cannot be used in areas where it is difficult to secure the amount of water.

  Therefore, the present invention has been made in view of the above-described problems in the prior art, and uses an amphoteric ion exchange resin for the treatment of leachate in the final disposal site even in areas where it is difficult to secure the amount of water. The purpose is to make it possible.

  In order to achieve the above object, the present invention provides a method for regenerating an amphoteric ion exchange resin, which is a liquid that has passed through the amphoteric ion exchange resin to regenerate the amphoteric ion exchange resin. A liquid that does not contain the target element to be separated is used.

  According to the present invention, a solution that has passed through the amphoteric ion exchange resin and does not contain the target element separated by the amphoteric ion exchange resin is used for the regeneration of the amphoteric ion exchange resin. Since the amount of industrial water used for resin regeneration can be reduced, amphoteric ion exchange resins can be used for the treatment of leachate in final disposal sites even in areas where it is difficult to secure the amount of water. Become.

  In the above ampholytic ion exchange resin regeneration method, the target element to be separated by the amphoteric ion exchange resin can be calcium, and calcium can be separated while reducing the amount of industrial water used for the regeneration. .

  Further, the liquid that has passed through the amphoteric ion exchange resin and does not contain the target element to be separated is used as demineralized water discharged from the electrodialysis apparatus disposed downstream of the amphoteric ion exchange resin. It is possible to reduce the amount of industrial water used for regeneration while utilizing the desalted water of the electrodialyzer.

Furthermore, demineralized water containing SO ₄ ^2- ions can be used for the regeneration of the amphoteric ion exchange resin. This makes it possible to use a monovalent selective anion exchange membrane for the anion exchange membrane of the electrodialysis apparatus.

Further, in the reproducing method of the amphoteric ion-exchange resins, amphoteric ion exchange resin, the final disposal site leachate, low Ca ²⁺ concentration, Cl ^- first and solution concentration is high, the Ca ²⁺ concentration high, Cl ^- can be used to separate into a lower concentration second solution. This makes it possible to use the amphoteric ion exchange resin for the treatment of the leachate in the final disposal site even in areas where it is difficult to ensure the amount of water.

  As described above, by using the amphoteric ion exchange resin regeneration method according to the present invention, the amphoteric ion exchange resin can be used for the treatment of leachate in the final disposal site even in areas where it is difficult to secure the amount of water. Is possible.

It is the schematic for demonstrating an example of the processing method of the leachate of the final disposal site to which the regeneration method of the amphoteric ion exchange resin which concerns on this invention is applied. The density | concentration of each component contained in the process liquid which passed the amphoteric ion exchange resin at the time of processing the leachate of a final disposal site using industrial water for the regeneration water of an amphoteric ion exchange resin is shown. The density | concentration of each component contained in the process liquid which passed the amphoteric ion exchange resin at the time of processing the leachate of a final disposal site using the demineralized water of an electrodialyzer for the regeneration water of an amphoteric ion exchange resin is shown. It is the schematic for demonstrating the other example of the processing method of the leachate of the final disposal site to which the regeneration method of the amphoteric ion exchange resin which concerns on this invention is applied. It is the schematic for demonstrating an example of the processing method of the leachate of the conventional final disposal site. It is the schematic for demonstrating the other example of the processing method of the leachate of the conventional final disposal site.

  Next, modes for carrying out the present invention will be described with reference to the drawings. In the following description, an example will be described in which amphoteric ion exchange resin is used for the treatment of leachate in the final disposal site and the amphoteric ion exchange resin is regenerated in the course of this treatment.

  FIG. 1 shows an example of a leachate treatment system (hereinafter abbreviated as “treatment system”) at a final disposal site. This treatment system 1 removes harmful heavy metals from leachate W stored in a regulating tank 11. The chemical reaction tank 12 for adding chemicals, the thickener 13 for precipitating and removing heavy metals, the COD treatment device 14, the suspended solid removal device 15, the amphoteric ion exchange resin 16, and the electrodialysis device 17 Is done. This apparatus configuration is the same as that of the conventional processing system shown in FIG.

  The amphoteric ion exchange resin 16 is provided for removing calcium contained in the leachate W discharged from the suspended substance removing device 15. The amphoteric ion exchange resin has a function of allowing ion exchange with both cation and anion by making the base material cross-linked polystyrene or the like and having a quaternary ammonium group and a carboxylic acid group in the same functional group chain. Resin. For example, amphoteric ion exchange resin, Diaion (registered trademark), AMP03 manufactured by Mitsubishi Chemical Corporation can be used. The amphoteric ion exchange resin 16 can separate the electrolyte and the non-electrolyte in the aqueous solution and can also separate the electrolytes from each other.

  The electrodialyzer 17 is provided for concentration and desalting of the salinity of the leachate W discharged from the suspended substance removing device 15. A monovalent selective anion exchange membrane can also be used for the anion exchange membrane of the electrodialyzer.

  Next, the operation of the processing system 1 having the above configuration will be described with reference to FIG.

  In the final disposal site 10, in order to remove harmful heavy metals from the leachate W stored in the adjustment tank 11, chemicals are added in the chemical reaction tank 12, these are precipitated and removed by the thickener 13, the COD processing device 14, the suspension Calcium is removed by the amphoteric ion exchange resin 16 through the turbid substance removing device 15. The operations related to calcium removal and resin regeneration in the amphoteric ion exchange resin 16 will be described later.

In amphoteric ion exchange resin 16, suspended leachate W from substance remover 15, low Ca ²⁺ concentration, Cl ^- concentration is higher the first solution L1, high Ca ²⁺ concentration, Cl ^- concentration The solution is separated into a low second solution L2, and the first solution L1 is supplied to the electrodialyzer 17 for desalting. In the electrodialysis apparatus 17, the desalted water D having a water amount of 1.1 to 1.4Q is returned to the amphoteric ion exchange resin 16 as regenerated water of the amphoteric ion exchange resin 16 with respect to the water amount 1Q of the leachate W, and the water amount is 0.1Q. Concentrated water C is evaporated to recover the salt.

  Next, calcium removal and regeneration of the amphoteric ion exchange resin will be described with reference to FIGS. 2 and 3.

  FIG. 2 shows that the amphoteric ion exchange resin 41 shown in FIG. 6 is passed through the leachate W of the final disposal site 30 as raw water, and industrial water (new water) IW is three times the amount of leachate W as reclaimed water. The relationship between the amount of liquid that has passed through and the concentration of each component contained in the processing liquid that has passed through the amphoteric ion exchange resin 41 is shown. The amphoteric ion exchange resin 41 column has a diameter of 40 mm × H 760 mm and a resin amount of 955 ml. After 955 ml of leachate W was passed through this column, 2865 (955 × 3) ml of industrial water IW was passed through and discharged. The concentration of the solution was measured. Water was passed at a rate 4 times the SV of 955 ml (SV: 4) per hour.

As clearly shown in FIG. 2, while the leachate W is flowing, water containing some calcium chloride (CaCl ₂ water) is discharged from the amphoteric ion exchange resin 41, and then the industrial water IW is passed. then, firstly, low Ca ²⁺ concentration, Cl ^- concentration is discharged a high first solution (Ca-free water), then a high Ca ²⁺ concentration, Cl ^- concentration is lower second solution (CaCl ₂ water) is discharged. Tables 1 and 2 show the calcium components and the amount of water of each of the Ca removal water and CaCl ₂ water.

  FIG. 3 shows the amphoteric ion exchange resin 16 shown in FIG. 1 in which the leachate W from the final disposal site 10 is passed as raw water, and the demineralized water D is three times the amount of leachate W as reclaimed water. The first solution (Ca-removed water) L1 discharged from the exchange resin 16 passes through the amphoteric ion exchange resin 16 when the water obtained by desalting the electrolyzer 17 is passed through the amphoteric ion exchange resin 16. The relationship of the density | concentration of each component contained in the processed liquid is shown. The amphoteric ion exchange resin 16 column had a diameter of 40 mm × H 760 mm and a resin amount of 955 ml. After 955 ml of leachate W was passed through this column, 2865 (955 × 3) ml of desalted water D was passed through and discharged. The concentration of the solution was measured. Water was passed at a rate 4 times the SV of 955 ml (SV: 4) per hour.

As clearly shown in FIG. 3, while the leachate W is flowing, water containing Cl ⁻ is discharged from the amphoteric ion exchange resin 16 (region A), and then the desalted water D is passed. First, a first solution (Ca-removed water) having a low Ca ²⁺ concentration and a high Cl ⁻ concentration is discharged (region B), and then a second solution having a high Ca ²⁺ concentration and a low Cl ⁻ concentration. The solution (CaCl ₂ water) is discharged (region C). The chlorine and calcium components and the amount of water in each region are as shown in Tables 3 and 4.

  Thus, even when the demineralized water D is used as the regenerated water for the amphoteric ion exchange resin 16, calcium can be separated from the leachate W. Therefore, as shown in FIG. The industrial water IW having a water amount of 1.9 to 1.6Q and the desalted water D having a water amount of 1.1 to 1.4Q are used as reclaimed water with respect to the water amount 1Q of W. The first solution L1 and the second solution L2 having an amount of water of 2.5 to 2.8Q can be obtained, and the first solution L1 is processed by the electrodialyzer 17 to discharge the second solution L2.

  As described above, in this embodiment, the amount of industrial water IW used for regeneration of the amphoteric ion exchange resin 16 is obtained by using the desalted water D of the electrodialyzer 17 as a part of the regenerated water of the amphoteric ion exchange resin 16. , Calcium can be separated from the leachate W while reducing the conventional 2/3 to 1/2.

  Next, another example of a method for treating leachate in a final disposal site to which the amphoteric ion exchange resin regeneration method according to the present invention is applied will be described with reference to FIG.

  The processing system 21 shown in the figure is the same as the processing system 1 only in that the amphoteric ion exchange resin 16 arranged at the rear stage of the suspended substance removing device 15 in the processing system 1 shown in FIG. Different. Since the other configuration is the same as that of the processing system 1 of FIG. 1, the same components are denoted by the same reference numerals, and description thereof will be omitted.

In this treatment system 21, the leachate W from the adjustment tank 11 is directly introduced into the amphoteric ion exchange resin 16, and the desalted water D of the electrodialyzer 17 is used as a part of the regenerated water of the amphoteric ion exchange resin 16. in the ion exchange resin 16 Ca ²⁺ concentration is low, Cl ^- concentration is higher the first solution L1, high Ca ²⁺ concentration, Cl ^- concentration were separated low and the second solution L2, the first solution After passing L1 through the chemical reaction tank 12, the thickener 13 that precipitates and removes heavy metals, the COD processing device 14, and the suspended solids removal device 15, it is supplied to the electrodialysis device 17 for desalting. In the electrodialysis apparatus 17, the desalted water D having a water amount of 1.1 to 1.4Q is returned to the amphoteric ion exchange resin 16 as regenerated water of the amphoteric ion exchange resin 16 with respect to the water amount 1Q of the leachate W, and the water amount is 0.1Q. Concentrated water C is evaporated to recover the salt. On the other hand, the second solution L2 from the amphoteric ion exchange resin 16 is discharged. The chlorine concentration and calcium concentration of the leachate W and the demineralized water D are as shown in Table 5.

  In this processing system 21, since the second solution L2 from the amphoteric ion exchange resin 16 is discharged, the configuration can be realized when no harmful substances are contained in the second solution L2. By using the desalted water D of the electrodialyzer 17 as a part of the regenerated water of the amphoteric ion exchange resin 16, the amount of industrial water IW used for the regeneration of the amphoteric ion exchange resin 16 is reduced to 2/3 to 1/2 of the conventional water. Calcium can be separated from the leachate W while being reduced.

DESCRIPTION OF SYMBOLS 1 Processing system 10 Final disposal site 11 Adjustment tank 12 Chemical reaction tank 13 Thickener 14 COD processing apparatus 15 Suspended substance removal apparatus 16 Amphoteric ion exchange resin 17 Electrodialysis apparatus 21 Processing system C Concentrated water D Desalted water IW Industrial water L1 1st Solution L2 second solution W leachate

Claims (5)

  Regeneration of an amphoteric ion exchange resin using a liquid that has passed through the amphoteric ion exchange resin and does not contain a target element separated by the amphoteric ion exchange resin Method.   The method for regenerating an amphoteric ion exchange resin according to claim 1, wherein the target element separated by the amphoteric ion exchange resin is calcium.   The liquid that has passed through the amphoteric ion exchange resin and does not contain the target element to be separated is demineralized water discharged from an electrodialysis apparatus disposed downstream of the amphoteric ion exchange resin. The method for regenerating an amphoteric ion exchange resin according to claim 1 or 2. The method for regenerating an amphoteric ion exchange resin according to claim 3, wherein the desalted water contains SO ₄ ^2- ions. Amphoteric ion exchange resin, the final disposal site leachate, low Ca ²⁺ concentration, Cl ^- and a high concentration of the first solution, high Ca ²⁺ concentration, Cl ^- concentration is lower the second solution and The method for regenerating an amphoteric ion exchange resin according to any one of claims 1 to 4, wherein the amphoteric ion exchange resin is used for the separation of the amphoteric ion exchange resin.

Images