JP2006254794A - Method for regenerating phenolic absorbing resin in sugar solution refining system and sugar solution refining apparatus - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To reduce the quality of an alkali solution used for regeneration of a phenolic absorbing resin and an ion exchange resin in a sugar solution-refining system having an absorption step for bringing the sugar solution into contact with the phenolic absorbing resin and an ion exchange step for bringing the sugar solution into contact with an ion exchange resin. <P>SOLUTION: An alkaline regeneration waste liquid of the ion exchange resin is used for regeneration of the phenolic absorption resin 12. For example, an alkali solution 64 is introduced from an alkali solution introducing pipe 36 into an anion exchange column 14 to bring the alkali solution 64 into contact with a strongly basic anion exchange resin 16, and then, the alkaline regeneration waste liquid discharged from the anion exchange column is introduced through connection pipes 28 and 34 into an absorption column 10 to bring the alkaline regeneration waste liquid into contact with the phenolic absorbing resin 12. <P>COPYRIGHT: (C)2006,JPO&NCIPI

Description

  The present invention relates to a method for regenerating a phenolic adsorption resin in a sugar liquid purification system using a phenolic adsorption resin and an ion exchange resin, and a sugar liquid purification apparatus using the phenolic adsorption resin and the ion exchange resin.

  Purification of the sugar solution is usually performed by a combination of decolorization treatment by activated carbon treatment, bone charcoal treatment, ion exchange resin treatment, etc., and desalting treatment by ion exchange resin treatment. In addition, as the latter desalting treatment system, in the case of sucrose liquid, a reverse system in which the sucrose liquid is sequentially passed through an anion exchange tower and a cation exchange tower, and the sucrose liquid is a strongly basic anion exchange resin and a weakly acidic cation. Known is a mixed bed system that passes through a mixed bed tower of exchange resin, and a system that sequentially passes sucrose liquid through an anion exchange tower and a mixed bed tower of strong basic anion exchange resin and weakly acidic cation exchange resin. (For example, refer to Patent Document 1).

Japanese Patent No. 2785833

  Currently, the odor generated from the sugar solution after the purification treatment is a problem. It is not known what the odor component contained in the treated sugar solution is, but the odor component remains in the sugar solution even after it has become a product, and the quality of the product is significantly reduced. For this reason, it is necessary to prevent the odorous component from being contained in the processed sugar solution after purification, but it is difficult to remove the odorous component from the sugar solution by the desalting treatment by the ion exchange resin treatment described above. It was.

  On the other hand, the present inventor, as a sugar solution purification system capable of effectively removing odor components contained in a sugar solution, an adsorption step of bringing the sugar solution into contact with a phenolic adsorption resin, and the sugar solution as an ion A sugar solution purification system that performs an ion exchange process in contact with an exchange resin has already been proposed.

  Phenol-based adsorbent resin is excellent in adsorptivity of pigment substances present in the solution because the base resin is hydrophobic, and has an adsorption characteristic similar to activated carbon because the base resin is porous. Also effective in adsorbing. Since the phenolic adsorption resin has a phenolic hydroxyl group as a functional group, when it is brought into contact with an alkaline solution having a certain pH or higher, the hydroxyl group is dissociated, and the hydrophobically adsorbed substance is desorbed to regenerate the resin.

  Phenol-based adsorption resins have the great advantage that they can be regenerated with chemicals as described above, and are used for decolorization and deodorization of amino acid solutions and protein solutions. Adsorbents used for the same applications include granular activated carbon, bone charcoal, and powdered activated carbon. To regenerate granular activated carbon and bone charcoal, it is necessary to install a regenerative furnace or perform consignment regeneration. Because it is disposable, the purchase cost and disposal cost are high.

  The phenolic adsorption resin includes a resin having only a phenolic hydroxyl group as a functional group, and a resin in which an amine is introduced into the base resin and both the phenolic hydroxyl group and the anion exchange group are functional groups. In any resin, an alkali solution is used as a regenerant for regeneration, and an acid solution is used as a neutralizer for the remaining alkali solution.

  In the above-mentioned sugar liquid purification system proposed by the present inventors, the ion exchange resin is used in combination with an anion exchange resin that removes an anion in a solution and a cation exchange resin that removes a cation in the solution. . An alkaline solution is used as the agent for regenerating the anion exchange resin, and an acid solution is used as the agent for regenerating the cation exchange resin. In general, an aqueous sodium hydroxide solution is used as the alkaline solution, and an aqueous hydrochloric acid solution is used as the acid solution.

  However, the sugar liquid purification system using the phenolic adsorption resin and the ion exchange resin described above has an advantage that the adsorbent can be regenerated by a chemical, but a large amount is required for the regeneration of the phenolic adsorbent resin and the ion exchange resin. Wastewater treatment equipment is required because of the high operating cost and the phenolic adsorption resin regeneration waste liquid contains a lot of organic components. The load of was increased.

  The present invention has been made in view of the above-described circumstances, and in a sugar liquid purification system using a phenolic adsorption resin and an ion exchange resin, the amount of an alkaline solution used for the regeneration of the phenolic adsorption resin and the ion exchange resin is reduced. It aims at providing the technology which can be made to do.

  As a result of various studies to achieve the above object, the present inventor has found that the waste solution of the alkaline solution used for the regeneration of the ion exchange resin is used in the sugar liquid purification system using the phenolic adsorption resin and the ion exchange resin. It was found that it can be used for the regeneration of phenolic adsorption resins. That is, by contacting the alkaline regeneration waste solution used for the regeneration of the ion exchange resin with the phenolic adsorption resin, the pigment component and the odor component adsorbed on the phenolic adsorption resin can be desorbed. It has been found that the amount of alkaline solution used for regeneration can be reduced.

  The present invention has been made based on the above-described knowledge, and phenol in a sugar solution purification system having an adsorption step in which a sugar solution is brought into contact with a phenolic adsorption resin and an ion exchange step in which the sugar solution is brought into contact with an ion exchange resin. There is provided a method for regenerating a phenolic adsorption resin in a sugar liquid purification system, characterized in that an alkaline regeneration waste solution of the ion exchange resin is used for regeneration of the phenolic adsorption resin.

  The present invention also provides an adsorption means for bringing a sugar solution into contact with a phenolic adsorption resin, an ion exchange means for bringing a sugar solution into contact with an ion exchange resin, an alkaline solution in contact with the ion exchange resin of the ion exchange means, There is provided a sugar solution purifying apparatus comprising a regeneration means for bringing an alkaline regeneration waste liquid after contact with an exchange resin into contact with a phenol-based adsorption resin of an adsorption means.

  Hereinafter, the present invention will be described in more detail. In the sugar solution purification system using the regeneration method of the present invention and the adsorption step and the adsorption means in the sugar solution purification apparatus of the present invention, the sugar solution is brought into contact with the phenolic adsorption resin. The phenolic adsorption resin is an adsorption resin having a phenolic hydroxyl group on the surface of a porous aromatic polymer. In the present invention, any adsorption resin having such a structure can be used. Due to the above structure, the phenol-based adsorption resin has both a physical adsorption action like activated carbon by a porous aromatic polymer and an ion exchange action by a phenolic hydroxyl group. Specifically, Ajinomoto Fine Techno Co., Ltd. Hokuetsu (registered trademark, the same applies below) HS, KS, Rohm and Haas Amberlite (registered trademark, the same applies below) XAD761 etc. should be used as the phenolic adsorption resin. Can do.

In the sugar liquid purification system using the regeneration method of the present invention and the ion exchange step and ion exchange means in the sugar liquid purification apparatus of the present invention, the sugar liquid is brought into contact with an ion exchange resin. In this case, for example, when the sugar liquid is a sucrose liquid, a strongly basic anion exchange resin and a weakly acidic cation exchange resin can be used as the ion exchange resin. For example, the resin configurations shown in the following (a) to (c) are used. be able to.
(A) A configuration in which a sugar solution is sequentially passed through a strongly basic anion exchange resin and a weakly acidic cation exchange resin.
(B) A configuration in which the sugar solution is passed through a mixed bed of a strongly basic anion exchange resin and a weakly acidic cation exchange resin.
(C) A configuration in which the sugar solution is sequentially passed through a strongly basic anion exchange resin and a mixed bed of a strongly basic anion exchange resin and a weakly acidic cation exchange tree.

  Any strong basic anion exchange resin and weak acid cation exchange resin may be used as long as the sugar solution can be desalted without causing sugar conversion. More specifically, as the strongly basic anion exchange resin, for example, Amberlite IRA-402BL, IRA-900, IRA-411S, XT-5007, Mitsubishi Chemical Corporation Diaion (registered trademark, hereinafter the same) PA-308, As PA-412 and a weakly acidic cation exchange resin, for example, Amberlite IRC-76, IRC-50, and Diaion WK-11 can be used.

  In the sugar liquid purification system using the regeneration method of the present invention and the sugar liquid purification apparatus of the present invention, the sugar liquid may be contacted with the phenolic adsorption resin and then contacted with the ion exchange resin, or may be contacted with the ion exchange resin. Although it may be brought into contact with the phenolic adsorption resin later, the former is preferred for the following reasons. That is, when the sugar solution is brought into contact with the phenolic adsorption resin, depending on the method for regenerating the phenolic adsorption resin, acid or alkali is eluted from the phenolic adsorption resin, so that the pH of the sugar solution becomes acidic or becomes alkaline. However, when the sugar solution is brought into contact with the phenolic adsorption resin and then brought into contact with the ion exchange resin, the pH of the sugar solution that has become acidic or alkaline due to contact with the phenolic adsorption resin is ion-exchanged. There is an advantage that it can be restored to near neutrality by contact with the resin. In addition, since the phenolic adsorption resin has a decoloring action, when the sugar solution is brought into contact with the phenolic adsorption resin and then brought into contact with the ion exchange resin, the load of the ion exchange resin in the subsequent stage can be lowered, and therefore In the subsequent purification step using the ion-exchange resin, there is also an advantage that a large throughput can be obtained while maintaining the quality of the treated sugar solution at high purity.

  The phenolic adsorption resin used in the present invention adsorbs odor components and pigment components under acidic conditions or neutral conditions, changes surface properties under alkaline conditions, and desorbs adsorbates. For this reason, the sugar solution is usually brought into contact with the phenolic adsorption resin under acidic conditions or neutral conditions, and when the adsorption capacity of the phenolic adsorption resin decreases, the liquid passage is stopped, and an alkali solution such as aqueous sodium hydroxide or aqueous ammonia is used. The phenolic adsorption resin is regenerated using the solution. In the present invention, an alkaline regeneration waste solution of an ion exchange resin is used for regeneration of the phenol-based adsorption resin. That is, the ion exchange resin is regenerated using an alkaline solution such as an aqueous sodium hydroxide solution or an aqueous ammonia solution, and the phenol-based adsorbent resin is regenerated using the regenerated waste liquid.

  In this case, as the alkaline regeneration waste liquid of the ion exchange resin, specifically, the regeneration waste liquid of the anion exchange resin or the regeneration waste liquid of the cation exchange resin can be used, and the regeneration waste liquid of the strongly basic anion exchange resin is particularly preferable. That is, when a strongly basic anion exchange resin is used in the ion exchange treatment, a large amount of alkaline regeneration waste liquid is generated. This is due to the strong adsorbing power of the strongly basic anion exchange resin and low regeneration efficiency. Since the phenolic hydroxyl group of the phenolic adsorption resin starts to dissociate at around pH 10, the regeneration of the phenolic resin is possible if the pH of the alkaline regeneration waste liquid of the ion exchange resin is 10 or more. It is desirable that the alkaline regeneration waste solution of the ion exchange resin has a pH of 12 or more, and the regeneration waste solution of the strongly basic anion exchange resin satisfies this condition.

  In addition, as the sugar liquid to be processed in the sugar liquid purification system using the regeneration method of the present invention and the sugar liquid purification apparatus of the present invention, any sugar liquid such as starch sugar liquid may be used in addition to the sucrose liquid described above. In the case of a sucrose solution, a purified sugar solution that has undergone steps such as sugar washing, dissolution, carbonation saturation, filtration, and decolorization of the raw sugar is usually used, but is not limited thereto.

  As described above, according to the present invention, in the sugar liquid purification system using the phenolic adsorption resin and the ion exchange resin, the amount of the alkaline solution used for the regeneration of the phenolic adsorption resin and the ion exchange resin is reduced, and the operation is performed. Cost can be reduced.

  FIG. 1 is a flow diagram showing an example of a sugar liquid purification apparatus according to the present invention. In FIG. 1, 10 is an adsorption tower filled with a phenolic adsorption resin 12 inside, 14 is an anion exchange tower filled with a strongly basic anion exchange resin 16, and 18 is a weak acidic cation exchange resin 20 inside. Fig. 2 shows a packed cation exchange column. In the figure, 22 is a raw sugar solution introduction pipe connected to the upper part of the adsorption tower 10, 24 is a communication pipe provided between the lower part of the adsorption tower 10 and the upper part of the anion exchange tower 14, and 26 is a communication pipe 24. , A waste liquid discharge pipe 28 connected to the lower part of the anion exchange column 14 and the upper part of the cation exchange tower 18, 30 a waste liquid discharge pipe connected to the communication pipe 28, and 32 a cation exchange. A processing liquid discharge pipe connected to the lower part of the tower 18, 34 a communication pipe provided between the communication pipe 28 and the upper part of the adsorption tower 10, and 36 an alkaline solution introduction pipe connected to the upper part of the anion exchange tower 14. , 38 is a washing water introduction pipe connected to the upper part of the anion exchange column 14, 40 is an acid solution introduction pipe connected to the upper part of the adsorption tower 10, and 42 to 60 are open / close valves provided in the respective pipes. . In the sugar liquid purification apparatus of this example, the adsorption tower 10 constitutes an adsorption means, and the anion exchange tower 14 and the cation exchange tower 18 constitute an ion exchange means.

  When the sugar solution is purified by the sugar solution purifying apparatus of this example, as shown in FIG. 2, the raw sugar solution 62 is introduced from the raw sugar solution introduction tube 22 into the adsorption tower 10 and brought into contact with the phenolic adsorption resin 12. Then, after the sugar solution exiting the adsorption tower 10 is introduced into the anion exchange tower 14 via the connecting tube 24 and brought into contact with the strongly basic anion exchange resin 16, the sugar solution exiting the anion exchange tower 14 is connected to the connecting tube. By introducing into the cation exchange tower 18 via 28 and bringing it into contact with the weakly acidic cation exchange resin 20, a purified treated sugar solution having no odor is obtained from the treated solution discharge pipe 32.

  Moreover, when reproducing | regenerating the phenol type adsorption resin 12 and the strongly basic anion exchange resin 16 of the sugar liquid refiner | purifier of this example, it carries out as follows. First, as shown in FIG. 3, an alkaline solution 64 is introduced into the anion exchange column 14 from the alkaline solution introduction pipe 36 and brought into contact with the strongly basic anion exchange resin 16, and then the alkaline regeneration waste liquid exiting the anion exchange column 14. Is introduced into the adsorption tower 10 through the connecting pipes 28 and 34 and brought into contact with the phenolic adsorption resin 12. The recycled waste liquid after coming into contact with the phenolic adsorption resin 12 is discharged out of the system through the communication pipe 24 and the waste liquid discharge pipe 26. Therefore, in the sugar liquid purification apparatus of this example, the regeneration means is constituted by the alkaline solution introduction pipe 36, the communication pipes 28, 34, 24, the waste liquid discharge pipe 26, and the on-off valve interposed therebetween.

  Next, as shown in FIG. 4, the washing water 66 was introduced into the anion exchange column 14 through the washing water introduction pipe 38 to wash the strong basic anion exchange resin 16 with washing water, and then exited the anion exchange column 14. Washing water is introduced into the adsorption tower 10 through the connecting pipes 28 and 34 to wash the phenolic adsorption resin 12 with the washing water. The washing water after washing the phenolic adsorption resin 12 is discharged out of the system through the communication pipe 24 and the waste liquid discharge pipe 26. In the present invention, as in this example, the ion exchange resin of the ion exchange means is washed with washing water, and the washing means for washing the phenolic adsorption resin of the adsorption means with the washing water washed with the ion exchange resin is purified by sugar solution. It is preferable to provide in an apparatus, and this can reduce the usage-amount of washing water. In the sugar liquid refining apparatus of this example, the washing means is constituted by the washing water introduction pipe 38, the communication pipes 28, 34, 24, the waste liquid discharge pipe 26, and the open / close valve interposed therebetween. However, washing of the strongly basic anion exchange resin 16 in the anion exchange tower 14 and washing of the phenol-based adsorption resin 12 in the adsorption tower 10 are performed by separately introducing washing water into the anion exchange tower 14 and the adsorption tower 10, respectively. Also good.

  Further, when neutralizing the phenolic adsorption resin 12 after the regeneration and washing treatment, as shown in FIG. 5, the acid solution 68 is introduced into the adsorption tower 10 from the acid solution introduction tube 40 and the phenolic adsorption resin 12 is introduced. To neutralize the alkaline solution remaining in the phenolic adsorption resin 12. The acid solution after contacting the phenolic adsorption resin 12 is discharged out of the system through the communication pipe 24 and the waste liquid discharge pipe 26. After the neutralization treatment, washing water is introduced from the raw sugar solution introduction pipe 22 into the adsorption tower 10 to wash away the salt and excess acid in the phenolic adsorption resin 12. The washing water after washing the phenolic adsorption resin 12 is discharged out of the system through the communication pipe 24 and the waste liquid discharge pipe 26.

  For neutralization of the alkaline solution remaining in the phenol-based adsorption resin 12 described above, an acidic regeneration waste solution of the weakly acidic cation exchange resin 20 in the cation exchange tower 18 can be used. In this case, after the acid solution is introduced into the cation exchange column 18 to regenerate the weak acid cation exchange resin 20, a part of the regeneration waste liquid may be introduced into the adsorption column 10.

  2 to 5 show only the piping to be used. At the time of the operation shown in FIGS. 2 to 5, the open / close valve interposed in the illustrated pipe may be opened and the open / close valve interposed in the unillustrated pipe may be closed.

  The amount of the regenerant used can be reduced by performing the above steps and utilizing the alkaline regeneration waste solution of the ion exchange resin for the regeneration of the phenolic adsorption resin. When the phenolic adsorption resin is regenerated using an alkaline regeneration waste solution of an ion exchange resin, a regeneration effect equivalent to that when the phenolic adsorption resin is regenerated using an unused alkaline solution can be obtained.

  In the present invention, the amount of the alkaline solution used for the regeneration of the phenolic adsorption resin and the ion exchange resin can be appropriately set according to the ratio of the amount of the phenolic adsorption resin and the amount of the ion exchange resin. It is also possible that the amount of the alkaline solution required for the regeneration of the phenolic adsorption resin is not sufficient for the alkaline regeneration waste liquid of the ion exchange resin. In this case, an unused alkaline liquid is used for the alkaline regeneration waste liquid of the ion exchange resin. In order to improve the regeneration efficiency of the ion exchange resin, it is preferable to increase the amount of the alkaline solution used for regeneration of the amount of the ion exchange resin, rather than replenishing it with the phenolic adsorption resin.

  Furthermore, depending on the ratio of the load applied to the phenolic adsorption resin and the ion exchange resin, it is not always necessary to regenerate the phenolic adsorption resin when the ion exchange resin is regenerated, for example, once every several cycles of the ion exchange resin regeneration cycle. It is also conceivable to regenerate the phenolic adsorption resin at a frequency.

The present invention will be specifically described below with reference to examples. However, the present invention is not limited to these examples.
(Example)
1 is an experimental apparatus having the same configuration as the purification apparatus shown in FIG. 1, and the adsorption column (adsorption tower) is filled with 100 mL of Hokuetsu HS as a phenolic adsorption resin, and the anion exchange column (anion exchange tower) is strongly basic anion exchange. A purification apparatus was prepared in which 100 mL of Amberlite IRA402BL was packed as a resin, and 50 mL of Amberlite IRC-76 was charged as a weakly acidic cation exchange resin in a cation exchange column (cation exchange column). Using this purification apparatus, the following purification step, regeneration step, neutralization step, and adsorption column flow step were performed.
<Purification process>
Purify 5000 ml of sucrose solution (raw sugar solution) with the properties shown in Table 1 in the order of adsorption column, anion exchange column, and cation exchange column under conditions of a flow rate of 50 ° C. and a flow rate of 400 ml / h. A treated sugar solution was obtained. Bx in Table 1 indicates the Brix sugar concentration (%), pH and electrical conductivity indicate values at 20 ° C., and color value (ICUMSA unit) indicates a value calculated by the following formula.

＜再生工程＞
上記精製工程終了後、水で各カラムを洗浄して糖液を各カラムから押し出した。また、アニオン交換カラムと吸着カラムとを直列に連続した。そして、１ｍｏｌ／Ｌの水酸化ナトリウム水溶液２００ｍｌを流速４００ｍｌ／Ｌでアニオン交換カラムおよび吸着カラムにこの順で通液した。次いで、水をアニオン交換カラムおよび吸着カラムにこの順で通液して両カラムを洗浄した。また、カチオン交換カラムに１ｍｏｌ／Ｌの塩酸水溶液１００ｍｌを通液した後、水でカチオン交換カラムを洗浄した。
＜中和工程＞
０．２ｍｏｌ／Ｌの塩酸水溶液１００ｍｌを流速４００ｍｌ／Ｌで吸着カラムに通液して中和を行い、さらに水で吸着カラムを洗浄した。

<Regeneration process>
After the purification step, each column was washed with water and the sugar solution was pushed out from each column. Moreover, the anion exchange column and the adsorption column were continued in series. Then, 200 ml of a 1 mol / L sodium hydroxide aqueous solution was passed through the anion exchange column and the adsorption column in this order at a flow rate of 400 ml / L. Next, water was passed through the anion exchange column and the adsorption column in this order to wash both columns. Further, 100 ml of a 1 mol / L hydrochloric acid aqueous solution was passed through the cation exchange column, and then the cation exchange column was washed with water.
<Neutralization process>
Neutralization was performed by passing 100 ml of a 0.2 mol / L hydrochloric acid aqueous solution through the adsorption column at a flow rate of 400 ml / L, and the adsorption column was washed with water.

  The amount of chemicals (NaOH and HCl) and the amount of washing water required for regeneration of phenolic adsorption resins, strong basic anion exchange resins, and weakly acidic cation exchange resins, and the amount of waste liquid generated during the regeneration (drug amount and amount of washing water) Total) is shown in Table 2.

＜吸着カラム通液工程＞
上記再生工程および中和工程を行った後、吸着カラムのみに表１に示した性状の原糖液５０００ｍｌを通液した。得られた処理液（吸着カラム出口の処理液）の品質を表１に示した。
（比較例）
実施例と同じ装置を用い、下記精製工程、再生工程、中和工程、吸着カラム通液工程を行った。
＜精製工程＞
実施例と同様の操作を行った。
＜再生工程＞
水で各カラムを洗浄して糖液を各カラムから押し出した。そして、１ｍｏｌ／Ｌの水酸化ナトリウム水溶液２００ｍｌを吸着カラムに通液した後、水で吸着カラムを洗浄した。また、１ｍｏｌ／Ｌの水酸化ナトリウム水溶液２００ｍｌをアニオン交換カラム通液した後、水でアニオン交換カラムを洗浄した。さらに、カチオン交換カラムに１ｍｏｌ／Ｌの塩酸水溶液１００ｍｌを通液した後、水でカチオン交換カラムを洗浄した。
＜中和工程＞
０．２ｍｏｌ／Ｌの塩酸水溶液１００ｍｌを吸着カラムに通液して中和を行い、さらに水で吸着カラムを洗浄した。

<Adsorption column flow process>
After the regeneration step and the neutralization step, 5000 ml of the raw sugar solution having the properties shown in Table 1 was passed through only the adsorption column. The quality of the obtained treatment liquid (treatment liquid at the adsorption column outlet) is shown in Table 1.
(Comparative example)
Using the same apparatus as in the examples, the following purification step, regeneration step, neutralization step, and adsorption column flow step were performed.
<Purification process>
The same operation as in the example was performed.
<Regeneration process>
Each column was washed with water, and the sugar solution was pushed out from each column. Then, 200 ml of a 1 mol / L sodium hydroxide aqueous solution was passed through the adsorption column, and then the adsorption column was washed with water. Further, 200 ml of 1 mol / L sodium hydroxide aqueous solution was passed through the anion exchange column, and then the anion exchange column was washed with water. Further, 100 ml of a 1 mol / L hydrochloric acid aqueous solution was passed through the cation exchange column, and then the cation exchange column was washed with water.
<Neutralization process>
Neutralization was performed by passing 100 ml of 0.2 mol / L hydrochloric acid aqueous solution through the adsorption column, and the adsorption column was washed with water.

The amount of chemicals (NaOH and HCl) and the amount of washing water required for regeneration of phenolic adsorption resins, strong basic anion exchange resins, and weakly acidic cation exchange resins, and the amount of waste liquid generated during the regeneration (drug amount and amount of washing water) Total) is shown in Table 2.
<Adsorption column flow process>
After the regeneration step and the neutralization step, 5000 ml of the raw sugar solution having the properties shown in Table 1 was passed through only the adsorption column. The quality of the obtained treatment liquid (treatment liquid at the adsorption column outlet) is shown in Table 1.

  From the results shown in Table 1, in the sugar liquid purification system using the phenolic adsorption resin and the anion exchange resin, when the alkaline regeneration waste liquid of the anion exchange resin is used for the regeneration of the phenolic adsorption resin, an unused alkali as a regenerant is used. It turns out that the reproduction | regeneration effect equivalent to the case where a solution is used is acquired. In addition, from the results in Table 2, when the alkaline regeneration waste liquid of anion exchange resin was used for regeneration of phenolic adsorption resin, the phenolic adsorption resin and anion were compared with the case of using alkaline solution for regeneration of phenolic adsorption resin. It can be seen that the amount of alkaline solution and the amount of washing water required for regeneration of the exchange resin are reduced. Therefore, according to the present invention, according to the present invention, it is possible to reduce the amount of the alkaline solution used for the regeneration of the phenolic adsorption resin and the ion exchange resin in the sugar liquid purification system using the phenolic adsorption resin and the ion exchange resin. confirmed.

It is a flowchart which shows an example of the sugar liquid refinement | purification apparatus which concerns on this invention. It is explanatory drawing which shows the sugar liquid refinement | purification process of the sugar liquid refinement | purification apparatus of FIG. It is explanatory drawing which shows the reproduction | regeneration process of the sugar liquid refinement | purification apparatus of FIG. It is explanatory drawing which shows the washing | cleaning process of the sugar liquid refinement | purification apparatus of FIG. It is explanatory drawing which shows the neutralization process of the sugar liquid refinement | purification apparatus of FIG.

Explanation of symbols

DESCRIPTION OF SYMBOLS 10 Adsorption tower 12 Phenolic adsorption resin 14 Anion exchange tower 16 Strongly basic anion exchange resin 18 Cation exchange tower 20 Weak acidic cation exchange resin 22 Raw sugar liquid introduction pipe 32 Treatment liquid discharge pipe 36 Alkaline solution introduction pipe 38 Washing water introduction pipe 40 Acid solution introduction tube

Claims (6)

  A method for regenerating a phenolic adsorption resin in a sugar solution purification system comprising an adsorption step of bringing a sugar solution into contact with a phenolic adsorption resin, and an ion exchange step of bringing the sugar solution into contact with an ion exchange resin, A method for regenerating a phenolic adsorption resin in a sugar liquid purification system, wherein an alkaline regeneration waste liquid is used for the regeneration of the phenolic adsorption resin.   2. The regeneration of the phenolic adsorption resin according to claim 1, wherein the alkaline solution is brought into contact with the ion exchange resin, and the alkaline regeneration waste liquid after being brought into contact with the ion exchange resin is brought into contact with the phenolic adsorption resin. A method for regenerating a phenolic adsorption resin in a sugar liquid purification system.   The alkaline solution is brought into contact with the ion exchange resin, and the regeneration process in which the alkaline regeneration waste liquid after coming into contact with the ion exchange resin is brought into contact with the phenolic adsorption resin. The ion exchange resin is washed with washing water and the ion exchange resin is washed. The method for regenerating a phenolic adsorption resin in a sugar liquid purification system according to claim 1 or 2, wherein a washing step of washing the phenolic adsorption resin with the washed water is sequentially performed.   In the sugar liquid purification system according to any one of claims 1 to 3, wherein the alkaline regeneration waste liquid of the ion exchange resin is a regeneration waste liquid of a strongly basic anion exchange resin used in the ion exchange step. Regeneration method of phenolic adsorption resin.   Adsorption means for bringing sugar liquid into contact with phenolic adsorption resin, ion exchange means for bringing sugar liquid into contact with ion exchange resin, and contacting alkaline solution with ion exchange resin in ion exchange means and after contacting ion exchange resin And a regeneration means for bringing the alkaline regeneration waste liquid into contact with the phenolic adsorption resin of the adsorption means. The ion exchange resin of the ion exchange means is washed with washing water, and the washing means for washing the phenolic adsorption resin of the adsorption means with the washing water after washing the ion exchange resin is provided. Sugar solution purification equipment.

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