JPH058059B2 - - Google Patents
Info
- Publication number
- JPH058059B2 JPH058059B2 JP61047189A JP4718986A JPH058059B2 JP H058059 B2 JPH058059 B2 JP H058059B2 JP 61047189 A JP61047189 A JP 61047189A JP 4718986 A JP4718986 A JP 4718986A JP H058059 B2 JPH058059 B2 JP H058059B2
- Authority
- JP
- Japan
- Prior art keywords
- exchange resin
- cation exchange
- tower
- resin
- cation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 124
- 230000008929 regeneration Effects 0.000 claims description 123
- 238000011069 regeneration method Methods 0.000 claims description 123
- 239000003729 cation exchange resin Substances 0.000 claims description 99
- 239000003957 anion exchange resin Substances 0.000 claims description 79
- 239000011347 resin Substances 0.000 claims description 60
- 229920005989 resin Polymers 0.000 claims description 60
- 239000003456 ion exchange resin Substances 0.000 claims description 38
- 229920003303 ion-exchange polymer Polymers 0.000 claims description 38
- 238000002156 mixing Methods 0.000 claims description 29
- 238000000034 method Methods 0.000 claims description 26
- 238000000926 separation method Methods 0.000 claims description 25
- 238000010612 desalination reaction Methods 0.000 claims description 18
- 238000005115 demineralization Methods 0.000 claims description 13
- 230000002328 demineralizing effect Effects 0.000 claims description 13
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 12
- 238000000605 extraction Methods 0.000 claims description 10
- 230000001172 regenerating effect Effects 0.000 claims description 9
- 238000011001 backwashing Methods 0.000 claims description 8
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 6
- 238000005342 ion exchange Methods 0.000 claims description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 4
- 238000005406 washing Methods 0.000 claims description 4
- 239000002253 acid Substances 0.000 claims description 3
- 239000012670 alkaline solution Substances 0.000 claims description 3
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 3
- 239000007788 liquid Substances 0.000 claims description 3
- 239000011707 mineral Substances 0.000 claims description 3
- 239000002699 waste material Substances 0.000 claims description 3
- 150000007513 acids Chemical class 0.000 claims 1
- 150000001768 cations Chemical class 0.000 description 47
- 150000001450 anions Chemical class 0.000 description 39
- 239000010410 layer Substances 0.000 description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 20
- 239000000460 chlorine Substances 0.000 description 13
- 239000011734 sodium Substances 0.000 description 10
- 238000010586 diagram Methods 0.000 description 9
- 239000012535 impurity Substances 0.000 description 6
- 238000011033 desalting Methods 0.000 description 4
- 230000005484 gravity Effects 0.000 description 4
- 150000002500 ions Chemical class 0.000 description 4
- 229910001415 sodium ion Inorganic materials 0.000 description 4
- 238000011109 contamination Methods 0.000 description 3
- 238000007796 conventional method Methods 0.000 description 3
- 235000011121 sodium hydroxide Nutrition 0.000 description 3
- 239000002344 surface layer Substances 0.000 description 3
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000005341 cation exchange Methods 0.000 description 2
- 229940023913 cation exchange resins Drugs 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 235000010755 mineral Nutrition 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical group [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical group [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 description 1
- 238000005349 anion exchange Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- -1 chlorine ions Chemical class 0.000 description 1
- 238000005253 cladding Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000008214 highly purified water Substances 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 230000003287 optical effect Effects 0.000 description 1
- 239000011342 resin composition Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000012498 ultrapure water Substances 0.000 description 1
Landscapes
- Treatment Of Water By Ion Exchange (AREA)
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は塔外再生型の混床式イオン交換脱塩装
置とりわけ復水脱塩装置における混合イオン交換
樹脂の再生方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] The present invention relates to a method for regenerating a mixed ion exchange resin in an out-of-column regeneration type mixed bed ion exchange desalination apparatus, particularly in a condensate desalination apparatus.
火力発電所或は原子力発電所においては多量の
高純度の純水を循環再利用している。タービンを
通過した蒸気は復水器と呼ばれる冷却器で水（以
下復水と称する。）に戻される。この復水中には
系内の不純物が含まれるため循環再利用するため
には、復水脱塩装置で不純物を除去する必要があ
る。復水脱塩装置はカチオン交換樹脂とアニオン
交換樹脂を混合したいわゆる混床式イオン交換脱
塩装置であり、復水をこの混合イオン交換樹脂層
に通水することによつてナトリウムイオン
（Na+）や塩素イオン（Cl-）等のイオンの他、酸
化鉄などの金属酸化物を主体とする懸濁物質（通
常クラツドと称される。）等を除去することがで
きる。
In thermal power plants or nuclear power plants, large amounts of highly purified water are recycled and reused. The steam that has passed through the turbine is returned to water (hereinafter referred to as condensate) in a cooler called a condenser. Since this condensate contains impurities within the system, it is necessary to remove the impurities with a condensate desalination device in order to recycle and reuse the condensate. The condensate desalination equipment is a so-called mixed bed type ion exchange desalination equipment in which a cation exchange resin and an anion exchange resin are mixed, and sodium ions (Na + ) and chlorine ions (Cl - ), as well as suspended solids (usually referred to as cladding) mainly composed of metal oxides such as iron oxide.
このように混床式イオン交換脱塩装置は優れた
性能を有しているが、カチオン交換樹脂とアニオ
ン交換樹脂とを混合して被処理水を処理するた
め、脱塩能力を失つた両イオン交換樹脂を再生す
るためには混合イオン交換樹脂をカチオン交換樹
脂とアニオン交換樹脂とに分離しなければならな
い。この分離方法は通常混合イオン交換樹脂下部
より逆洗を行ない、両イオン交換樹脂が比重差に
よつて二層に成層することで成される。即ち従来
の塔外再生型の混床式イオン交換脱塩装置は基本
的に以下の工程から構成されている。 Although mixed-bed ion exchange desalination equipment has excellent performance as described above, since the water to be treated is treated by mixing cation exchange resin and anion exchange resin, both ion and ion exchangers have lost their desalination ability. In order to regenerate the exchange resin, the mixed ion exchange resin must be separated into a cation exchange resin and an anion exchange resin. This separation method is usually achieved by backwashing from the bottom of the mixed ion exchange resin and forming two layers of both ion exchange resins due to the difference in specific gravity. That is, the conventional mixed bed type ion exchange desalination apparatus of the outside column regeneration type basically consists of the following steps.
移送工程（）
脱塩工程を終了した脱塩塔内の混合イオン交換
樹脂をカチオン交換樹脂再生塔（以下カチオン再
生塔と称する。）に移送する。 Transfer step () The mixed ion exchange resin in the demineralization tower that has completed the desalination step is transferred to a cation exchange resin regeneration tower (hereinafter referred to as cation regeneration tower).
逆洗分離工程
カチオン再生塔において混合イオン交換樹脂を
逆洗し、比重差により上層のアニオン交換樹脂と
下層のカチオン交換樹脂に分離し成層する。 Backwash separation process The mixed ion exchange resin is backwashed in the cation regeneration tower, and separated into an upper layer of anion exchange resin and a lower layer of cation exchange resin due to the difference in specific gravity, and stratified the resin.
移送工程（）
アニオン交換樹脂をカチオン再生塔からアニオ
ン交換樹脂再生塔（以下アニオン再生塔と称す
る。）に移送する。 Transfer step () The anion exchange resin is transferred from the cation regeneration tower to the anion exchange resin regeneration tower (hereinafter referred to as an anion regeneration tower).
再生工程
カチオン再生塔には鉱酸を通薬し、アニオン再
生塔にはアルカリを通薬して両イオン交換樹脂を
再生し続いて水洗を行なう。 Regeneration process Mineral acid is passed through the cation regeneration tower, and alkali is passed through the anion regeneration tower to regenerate both ion exchange resins, followed by water washing.
移送工程（）
両再生塔より再生済みの両イオン交換樹脂をそ
れぞれ樹脂混合塔に移送する。 Transfer step () Both regenerated ion exchange resins are transferred from both regeneration towers to a resin mixing tower.
混合工程
通常樹脂混合塔底部から空気を導入することに
より両イオン交換樹脂を混合する。 Mixing process Both ion exchange resins are usually mixed by introducing air from the bottom of the resin mixing column.
移送工程（）
必要に応じて樹脂混合塔から脱塩塔に移送し充
填する。 Transfer step () If necessary, the resin is transferred from the resin mixing tower to the demineralization tower and filled.
以上の一連の工程により脱塩−再生を繰返えす
訳である。 Desalting and regeneration are repeated through the above series of steps.
ところで、復水の水質を例に挙げても近年増す
ます水質が厳しく要求されるに至つており、特に
原子力発電所における加圧水型軽水炉（PWR）
の二次系或は沸騰水型軽水炉（BWR）の炉水系
においては、不純物イオン濃度が0.1μｇ／
（ppb）以下のレベルが大きな問題となつている。
このためしばしば復水脱塩装置の処理水水質が純
度不良になるという問題が生じ、安定して不純物
イオン濃度を0.1μｇ／以下に制御することがな
かなか困難であつた。 By the way, taking the water quality of condensate as an example, water quality has become increasingly strict in recent years, especially for pressurized water reactors (PWRs) in nuclear power plants.
In the secondary system of a boiling water reactor (BWR) or the reactor water system of a boiling water reactor (BWR), the impurity ion concentration is 0.1μg/
(ppb) or lower levels are becoming a major problem.
For this reason, a problem arises in that the quality of the water treated by the condensate desalination apparatus often becomes poor in purity, and it has been difficult to stably control the impurity ion concentration to 0.1 μg/or less.
上記純度不良を引き起す主な原因はアニオン交
換樹脂とカチオン交換樹脂とを充分に分離するこ
とができないからである。即ち脱塩塔出口水の水
質を支配する因子は再生工程で再生されなかつた
樹脂、更に正確に言えば再生工程で生じてしまつ
た塩形のイオン交換樹脂例えばナトリウムイオン
形（以下Na+形と称する。）カチオン交換樹脂と
塩化物イオン形（以下Cl-形と称する。）アニオン
交換樹脂の混入率である。
The main reason for the poor purity is that the anion exchange resin and cation exchange resin cannot be sufficiently separated. In other words, the factors governing the water quality of the water at the outlet of the desalination tower are the resins that were not regenerated in the regeneration process, or more precisely, the salt-form ion exchange resins generated during the regeneration process, such as the sodium ion form (hereinafter referred to as Na + form). ) cation exchange resin and chloride ion form (hereinafter referred to as Cl - form) anion exchange resin.
これらNa+形カチオン交換樹脂とCl-形アニオ
ン交換樹脂が再生工程で生成する主な原因は、逆
洗分離工程と移送工程における両樹脂の分離が
不充分なため、カチオン再生塔にはアニオン交換
樹脂が残留し、アニオン再生塔にはカチオン交換
樹脂が持ち込まれてしまうことにある。このため
カチオン再生塔では再生剤には塩酸を用いれば残
留したアニオン交換樹脂は全てCl-形となり、ま
たアニオン再生塔に持ち込まれたカチオン交換樹
脂は苛性ソーダの通薬によつて全てNa+形となつ
てしまう。 The main reason why these Na + type cation exchange resins and Cl - type anion exchange resins are generated in the regeneration process is that the separation of both resins in the backwash separation process and transfer process is insufficient. The problem is that the resin remains and the cation exchange resin is carried into the anion regeneration tower. Therefore, if hydrochloric acid is used as the regenerating agent in the cation regeneration tower, all the remaining anion exchange resin will be in the Cl - form, and all the cation exchange resin brought into the anion regeneration tower will be converted into the Na + form by passing caustic soda. I get used to it.
これら塩形イオン交換樹脂の混入率が増加すれ
ば、処理水中の不純物リーク量も比例して増加す
る。例えば復水中のNa+イオンを0.02μｇ／
（Naとして）、Cl-イオンを0.05μｇ／（Clとし
て）以下にするためには第２図及び第３図に示し
たNa+形カチオン交換樹脂の混入率と脱塩塔出口
のNa+イオン濃度との関係、及びCl-形アニオン
交換樹脂の混入率と脱塩塔出口水のCl-イオン濃
度の関係から、Na+形カチオン交換樹脂の混入率
を約0.65％以下、Cl-形アニオン交換樹脂の混入
率を約９％以下とする必要がある。 If the mixing rate of these salt-type ion exchange resins increases, the amount of impurity leakage into the treated water also increases proportionally. For example, 0.02μg/Na + ion in condensate
(as Na) and Cl - ions to 0.05 μg/(as Cl) or less, the mixing rate of Na + type cation exchange resin and Na + ions at the outlet of the demineralization tower are as shown in Figures 2 and 3. From the relationship between the concentration of the Cl - type anion exchange resin and the Cl - ion concentration of the demineralization tower outlet water, the concentration of the Na + type cation exchange resin should be approximately 0.65% or less, and the Cl - type anion exchange resin concentration should be kept at approximately 0.65% or less. It is necessary to keep the resin mixing rate to about 9% or less.
しかし従来法においてはカチオン再生塔が樹脂
分離塔をも兼ねているためカチオン再生塔に残留
するアニオン交換樹脂量を極力少量に抑えること
が不可欠である。しかしながらアニオン交換樹脂
とカチオン交換樹脂とをほぼ完全に分離するため
には以下の条件が大前提となる。 However, in the conventional method, since the cation regeneration tower also serves as a resin separation tower, it is essential to keep the amount of anion exchange resin remaining in the cation regeneration tower as small as possible. However, in order to almost completely separate the anion exchange resin and cation exchange resin, the following conditions are essential.
１ カチオン再生塔においてアニオン交換樹脂と
カチオン交換樹脂の分離界面が常に一定である
こと
２ 上記分離界面が明確でありかつ水平に保たれ
ていること
３ アニオン交換樹脂をカチオン再生塔からアニ
オン再生塔に移送する際に上記分離界面が常に
均一かつ水平に保たれていること
しかし実際には以下に示すようにこれらの条件
を全て満足することはほとんど不可能に近い。即
ちまず脱塩塔は通常１塔のみではなく３〜４塔あ
り必らずしも脱塩塔内の混合イオン交換樹脂を完
全にカチオン再生塔に移送できるとは限らない。
従つて各脱塩塔の混合イオン交換樹脂量が全て同
一である保証はない。実際、長期間脱塩−再生を
繰返えした場合、各脱塩塔の樹脂量は全て異なつ
ていることは多くの調査結果から明らかになつて
いる。従つてカチオン再生塔において分離界面が
常に一定の高さであることはむしろないと考える
のが自然である。1. The separation interface between the anion exchange resin and the cation exchange resin in the cation regeneration tower is always constant. 2. The above separation interface is clear and kept horizontal. 3. The anion exchange resin is transferred from the cation regeneration tower to the anion regeneration tower. The above-mentioned separation interface must always be kept uniform and horizontal during transfer. However, in reality, as shown below, it is almost impossible to satisfy all of these conditions. That is, the number of demineralization towers is usually not only one, but three or four, and it is not always possible to completely transfer the mixed ion exchange resin in the demineralization tower to the cation regeneration tower.
Therefore, there is no guarantee that the amount of mixed ion exchange resin in each demineralization tower is the same. In fact, it has become clear from the results of many studies that when desalination and regeneration are repeated over a long period of time, the amount of resin in each desalination tower is different. Therefore, it is natural to think that the separation interface in a cation regeneration tower is not always at a constant height.
次に、従来のカチオン再生塔において、混合樹
脂を逆洗した場合の両樹脂の分離状態を第７図及
び第８図に示す。第７図において、符号３は従来
のカチオン再生塔を示し、３′はカチオン交換樹
脂とアニオン交換樹脂の分離界面を示す。混合樹
脂を逆洗して分離した場合、両樹脂の比重差から
理論的には両樹脂は第７図に示すように明確に分
離されると考えられるが、実際には第８図のアニ
オン交換樹脂の存在率及びカチオン交換樹脂の存
在率を示す図からわかるように、分離界面付近の
樹脂組成を見るとアニオン交換樹脂とカチオン交
換樹脂は相互に混入した混合層が形成されてお
り、分離界面が明確に存在しえないことは周知の
事実である。更にカチオン再生塔からアニオン再
生塔に移送する場合界面付近の樹脂は流動状態に
あり分離界面が仮に明確に存在したとしても分離
界面を均一かつ水平に維持することはなかなか困
難である。 Next, FIGS. 7 and 8 show the state of separation of both resins when the mixed resin is backwashed in a conventional cation regeneration tower. In FIG. 7, reference numeral 3 indicates a conventional cation regeneration tower, and 3' indicates a separation interface between a cation exchange resin and an anion exchange resin. When a mixed resin is separated by backwashing, theoretically the two resins can be clearly separated as shown in Figure 7 based on the difference in their specific gravity, but in reality the anion exchange shown in Figure 8. As can be seen from the diagram showing the abundance rate of resin and the abundance rate of cation exchange resin, when looking at the resin composition near the separation interface, the anion exchange resin and cation exchange resin are mixed together to form a mixed layer, and the separation interface It is a well-known fact that cannot exist clearly. Furthermore, when transferring from the cation regeneration tower to the anion regeneration tower, the resin near the interface is in a fluid state, and even if a separation interface clearly exists, it is quite difficult to maintain the separation interface uniformly and horizontally.
以上の説明から明らかな様に従来のカチオン再
生塔でアニオン交換樹脂とカチオン交換樹脂を分
離する場合、両イオン交換樹脂をほぼ完全に分離
することはできない。このため再生工程で生じた
Na+形カチオン交換樹脂及びCl-形アニオン交換
樹脂の混入率を低減することはなかなか困難であ
り、従つて脱塩塔出口水の水質を常に安定して高
純度に保つことができないという問題点があつ
た。 As is clear from the above description, when an anion exchange resin and a cation exchange resin are separated using a conventional cation regeneration tower, it is not possible to almost completely separate both ion exchange resins. For this reason, the
It is difficult to reduce the contamination rate of Na + type cation exchange resin and Cl - type anion exchange resin, and the problem is that the water quality of the demineralization tower outlet water cannot always be maintained at a stable high purity. It was hot.
本発明者は上記の問題点を解決すべく、運転管
理が容易で高純度の処理水を安定に供給し得る混
合イオン交換樹脂の再生方法を検討した結果、従
来法とは逆にアニオン再生塔において混合イオン
交換樹脂を分離することで容易に目的を達成しう
ることを知見するに至つた。即ち従来法の技術的
限界は根本的には再生システムにおける塔構成に
問題があることを見出だした。
In order to solve the above problems, the present inventor investigated a method for regenerating a mixed ion exchange resin that is easy to operate and can stably supply high-purity treated water. It was discovered that the objective could be easily achieved by separating mixed ion exchange resins. In other words, it has been discovered that the technical limitations of the conventional method are fundamentally due to problems in the tower configuration in the regeneration system.
本発明は、カチオン再生塔が樹脂分離塔を兼ね
るのではなく、アニオン再生塔で混合イオン交換
樹脂の分離を行ない、分離されたカチオン交換樹
脂をアニオン再生塔からカチオン再生塔へ移送す
ることにより、カチオン再生塔の塔径をできる限
り小さくし、カチオン再生塔にアニオン交換樹脂
を極力残留させないようにすることにより、不純
物リークのきわめて少ないかつ運転管理が容易な
混合イオン交換樹脂の再生方法を提供することを
目的とするものである。 In the present invention, the cation regeneration tower does not also serve as a resin separation tower, but the anion regeneration tower separates the mixed ion exchange resin, and the separated cation exchange resin is transferred from the anion regeneration tower to the cation regeneration tower. To provide a method for regenerating a mixed ion exchange resin that causes extremely little leakage of impurities and facilitates operational management by reducing the diameter of the cation regeneration tower as much as possible and preventing the anion exchange resin from remaining in the cation regeneration tower as much as possible. The purpose is to
本発明の特徴は、
(a) 脱塩工程を終了した脱塩塔の混合イオン交換
樹脂を、あらかじめ別途に用意した混合イオン
交換樹脂を底部に装入したアニオン交換樹脂再
生塔に移送する工程
(b) 該アニオン再生塔内で逆洗を行ない下層がカ
チオン交換樹脂、上層がアニオン交換樹脂層と
なるように混合イオン交換樹脂を上下二層に分
離成層させる工程
(c) 該アニオン再生塔底部よりカチオン交換樹脂
を引き抜いてカチオン再生塔に移送する工程
(d) 該カチオン再生塔においてカチオン交換樹脂
を逆洗し、該カチオン交換樹脂層中に位置する
カチオン交換樹脂引き抜き口から、該カチオン
交換樹脂引き抜き口より上層の樹脂を引き抜い
てアニオン再生塔に移送する工程
(e) カチオン再生塔には塩酸もしくは硫酸等の鉱
酸を通薬し、続いて洗浄を行ない、またアニオ
ン再生塔においては再度逆洗を行ない上層がア
ニオン交換樹脂、下層がカチオン交換樹脂の上
下二層となるように分離成層したのち、水酸化
ナトリウム等のアルカリ溶液を通薬しアニオン
交換樹脂層中に位置する排水管よりアルカリ廃
液を塔外に排出し続いて洗浄を行なう工程
(f) カチオン再生塔内のカチオン交換樹脂を樹脂
混合塔に移送し、またアニオン再生塔において
は、前記排水塔より上側でかつアニオン交換樹
脂層中に位置するアニオン交換樹脂引き抜き口
から、該アニオン交換樹脂を引き抜いて前記樹
脂混合塔に移送し、続いて樹脂混合塔内の樹脂
を混合する工程
(g) 該樹脂混合塔内で混合された樹脂を続いて前
記脱塩塔に移送する工程
以上の一連の工程によつて構成することにあ
る。The features of the present invention are as follows: (a) A step of transferring the mixed ion exchange resin from the desalting tower that has completed the desalting process to an anion exchange resin regeneration tower in which a mixed ion exchange resin prepared separately in advance is charged at the bottom. b) A step of backwashing in the anion regeneration tower to separate and stratify the mixed ion exchange resin into upper and lower layers so that the lower layer is a cation exchange resin layer and the upper layer is an anion exchange resin layer (c) From the bottom of the anion regeneration tower Step (d) of extracting the cation exchange resin and transferring it to the cation regeneration tower; backwashing the cation exchange resin in the cation regeneration tower, and withdrawing the cation exchange resin from the cation exchange resin extraction port located in the cation exchange resin layer; Step (e) of pulling out the resin in the upper layer from the mouth and transferring it to the anion regeneration tower.The cation regeneration tower is passed through with a mineral acid such as hydrochloric acid or sulfuric acid, followed by washing, and the anion regeneration tower is backwashed again. The upper layer is an anion exchange resin, and the lower layer is a cation exchange resin. After that, an alkaline solution such as sodium hydroxide is passed through the anion exchange resin layer, and the alkaline waste liquid is discharged from the drain pipe located in the anion exchange resin layer. (f) The cation exchange resin in the cation regeneration tower is transferred to the resin mixing tower, and in the anion regeneration tower, the cation exchange resin is discharged from the tower and then washed. Step (g) of drawing out the anion exchange resin from the anion exchange resin draw-out port located at and transferring it to the resin mixing tower, and then mixing the resin in the resin mixing tower. and the step of subsequently transferring the demineralizer to the desalination tower.
ここでカチオン交換樹脂をアニオン再生塔から
カチオン再生塔へ移送する際の制御方法に関して
更に詳しく説明すれば、前記工程(c)において、カ
チオン交換樹脂の移送時間をあらかじめ設定して
おくことにより、カチオン交換樹脂の引き抜き量
を容易に制御することができる。 To explain in more detail the control method when transferring the cation exchange resin from the anion regeneration tower to the cation regeneration tower, in step (c), by setting the transfer time of the cation exchange resin in advance, The amount of exchange resin withdrawn can be easily controlled.
更に、厳密に該カチオン交換樹脂の引き抜き量
を制御する場合には、前記分離界面位置を検知す
る手段を持ち、カチオン交換樹脂の移送工程の進
行に伴つて下降する該分離界面の位置が所定位置
に達した時点をもつて移送を終了することができ
る。 Furthermore, in the case of strictly controlling the amount of the cation exchange resin withdrawn, a means for detecting the position of the separation interface is provided, and the position of the separation interface, which is lowered as the cation exchange resin transfer process progresses, is at a predetermined position. The transfer can be terminated at the point in time when .
本発明をその一実施態様を示す第１図、第４
図、第５図及び第６図に基いて説明する。
FIGS. 1 and 4 show one embodiment of the present invention.
The explanation will be made based on FIGS. 5 and 6.
第１図は、本発明のイオン交換樹脂の再生工程
を説明するための図面であつて、符号１はアニオ
ン再生塔、２はカチオン再生塔、３は樹脂混合
塔、４は混合樹脂移送管、５はカチオン交換樹脂
移送管、６はカチオン交換樹脂引き抜き口、７は
カチオン交換樹脂移送管、８は排水管、９はアニ
オン交換樹脂引き抜き口、１０はアニオン交換樹
脂移送管、１１はカチオン交換樹脂移送管、１２
は検出器を示す。また、第４図は再生塔の直径と
塔断面積の関係を示す図であり、第５図及び第６
図は検知器を用いて二層に分離したカチオン交換
樹脂とアニオン交換樹脂の界面を検知する状態を
示すもので、第５図はアニオン再生塔において両
樹脂を二層に分離した状態を示す図、第６図はカ
チオン交換樹脂をカチオン交換樹脂移送管から抜
き出し、両樹脂の界面が検知器１２の位置に達し
た状態（この時点でカチオン交換樹脂の抜き出し
を停止する）を示す図であつて、第５図及び第６
図に付した符号は第１図に関し説明した符号と同
一のものは同じ意味を有し、第５図において３′
は両樹脂の界面を示す。なお、第１図、第５図お
よび第６図において〓は混合イオン交換樹脂を、
〓はアニオン交換樹脂を〓はカチオン交換樹脂を
示す。 FIG. 1 is a diagram for explaining the ion exchange resin regeneration process of the present invention, in which reference numeral 1 is an anion regeneration tower, 2 is a cation regeneration tower, 3 is a resin mixing tower, 4 is a mixed resin transfer pipe, 5 is a cation exchange resin transfer pipe, 6 is a cation exchange resin extraction port, 7 is a cation exchange resin transfer pipe, 8 is a drain pipe, 9 is an anion exchange resin extraction port, 10 is an anion exchange resin transfer pipe, 11 is a cation exchange resin Transfer pipe, 12
indicates a detector. In addition, Figure 4 is a diagram showing the relationship between the diameter of the regeneration tower and the cross-sectional area of the tower, and Figures 5 and 6
The figure shows a state in which a detector is used to detect the interface between a cation exchange resin and an anion exchange resin that have been separated into two layers. Figure 5 shows a state in which both resins have been separated into two layers in an anion regeneration tower. , FIG. 6 is a diagram showing a state in which the cation exchange resin is extracted from the cation exchange resin transfer pipe and the interface between both resins reaches the position of the detector 12 (at this point, the extraction of the cation exchange resin is stopped). , Figures 5 and 6
The same reference numerals in the figures as those explained in relation to Fig. 1 have the same meanings, and in Fig. 5 3'
indicates the interface between both resins. In addition, in Fig. 1, Fig. 5, and Fig. 6, 〓 indicates mixed ion exchange resin,
〓 indicates anion exchange resin, 〓 indicates cation exchange resin.
第１図ａに示すようにアニオン再生塔１の塔底
にあらかじめ別途に用意した混合イオン交換樹脂
を装入しておく。脱塩工程を終了した脱塩塔より
混合イオン交換樹脂を混合樹脂移送管４にてアニ
オン再生塔１に移送し充填したのち、逆洗を行な
い上層がアニオン交換樹脂層、下層がカチオン交
換樹脂層の上下二層に分離成層する（第１図ｂ）。
次にアニオン再生塔１底部よりカチオン交換樹脂
移送管５を介してカチオン再生塔２へ移送し、カ
チオン再生塔２内の樹脂を逆洗分離する（第１図
ｃ）。アニオン再生塔１からカチオン再生塔２へ
カチオン交換樹脂を移送する際、アニオン交換樹
脂がカチオン再生塔２に多少持ち込まれたとして
も構わない。即ち第４図に示したように再生塔の
直径が例えば２ｍである場合塔断面積は3.14m2で
あるが、該再生塔の直径が1.4ｍとなれば塔断面
積は1.54m2となり半減する。仮にカチオン再生塔
に残留するアニオン交換樹脂の層高が、カチオン
再生塔直径２ｍの場合と1.4ｍの場合で同じであ
るとしたならば、そのアニオン交換樹脂残留量は
後者の方が前者の約1/2となることは明白である。 As shown in FIG. 1a, a separately prepared mixed ion exchange resin is charged to the bottom of the anion regeneration tower 1. After completing the desalting process, the mixed ion exchange resin is transferred from the desalination tower to the anion regeneration tower 1 through the mixed resin transfer pipe 4 and filled, and then backwashed to form an anion exchange resin layer in the upper layer and a cation exchange resin layer in the lower layer. It is separated and stratified into two layers, upper and lower (Fig. 1b).
Next, the resin is transferred from the bottom of the anion regeneration tower 1 to the cation exchange resin transfer pipe 5 to the cation regeneration tower 2, and the resin in the cation regeneration tower 2 is backwashed and separated (FIG. 1c). When transferring the cation exchange resin from the anion regeneration tower 1 to the cation regeneration tower 2, it does not matter if some of the anion exchange resin is brought into the cation regeneration tower 2. That is, as shown in Figure 4, if the diameter of the regeneration tower is, for example, 2 m, the tower cross-sectional area is 3.14 m2 , but if the diameter of the regeneration tower is 1.4 m, the tower cross-sectional area is halved to 1.54 m2 . do. If the bed height of the anion exchange resin remaining in the cation regeneration tower is the same when the cation regeneration tower is 2 m in diameter and 1.4 m in diameter, the amount of anion exchange resin remaining in the latter is about the same as in the former. It is clear that it will be 1/2.
しかしながら、従来カチオン再生塔でアニオン
交換樹脂とカチオン交換樹脂を逆洗分離するた
め、カチオン再生塔にはアニオン交換樹脂とカチ
オン交換樹脂を充填し得る容積が必要となり、塔
直径を小さくすることは塔高の制限からして実質
的に困難である。 However, since the anion exchange resin and cation exchange resin are conventionally backwashed and separated in the cation regeneration tower, the cation regeneration tower requires a volume that can be filled with the anion exchange resin and the cation exchange resin. It is practically difficult due to the height limitation.
そこで本発明のごとくアニオン再生塔でアニオ
ン交換樹脂とカチオン交換樹脂を分離するなら
ば、カチオン再生塔はカチオン交換樹脂とわずか
に持ち込まれるアニオン交換樹脂を充填し得る容
積があれば良く、かつカチオン交換樹脂はアニオ
ン交換樹脂よりも比重が大きいため逆洗時に必要
な塔高も小さくなる利点がある。 Therefore, if an anion exchange resin and a cation exchange resin are separated in an anion regeneration tower as in the present invention, the cation regeneration tower only needs to have a volume that can fill the cation exchange resin and a small amount of the anion exchange resin brought in, and the cation exchange Since the resin has a higher specific gravity than an anion exchange resin, it has the advantage that the column height required for backwashing is also smaller.
このようにカチオン再生塔の直径を小さくする
ことによりカチオン再生塔に残留するアニオン交
換樹脂を従来の1/2以下に容易に抑えることがで
きる。更にカチオン再生塔２に持ち込まれるアニ
オン交換樹脂を低減するためにアニオン再生塔１
からカチオン再生塔２へ移送する際に、アニオン
再生塔１内のカチオン交換樹脂層とアニオン交換
樹脂層の分離界面近傍のカチオン交換樹脂が引き
抜かれ始める前にカチオン交換樹脂の移送を停止
する。この理由は第８図に示したように分離界面
近傍の樹脂層は、両イオン交換樹脂が相互に混入
した混合層となつているからである。このカチオ
ン交換樹脂の引き抜き量を制御するには、あらか
じめカチオン交換樹脂の移送時間をタイマ等にて
設定しておくことにより容易に行なうことができ
る。 By reducing the diameter of the cation regeneration tower in this manner, the amount of anion exchange resin remaining in the cation regeneration tower can be easily reduced to 1/2 or less of the conventional value. Furthermore, in order to reduce the anion exchange resin brought into the cation regeneration tower 2, the anion regeneration tower 1
When transferring the cation exchange resin to the cation regeneration tower 2, the transfer of the cation exchange resin is stopped before the cation exchange resin near the separation interface between the cation exchange resin layer and the anion exchange resin layer in the anion regeneration tower 1 starts to be extracted. The reason for this is that, as shown in FIG. 8, the resin layer near the separation interface is a mixed layer in which both ion exchange resins are mixed together. The amount of cation exchange resin withdrawn can be easily controlled by setting the transfer time of the cation exchange resin in advance using a timer or the like.
更に、厳密にカチオン交換樹脂の引き抜き量を
制御する必要がある場合には第５図及び第６図に
示すように、分離界面位置を検知する手段１２例
えば導電率検出器、色調または輝度を検出する光
学的検出器等を用いれば良い。これらの手段はす
でに公知のものであり、検出器の取付け位置をカ
チオン交換樹脂引き抜き口より上部でかつ排水管
８より下部に設定することで容易に目的が達成す
ることができる。 Furthermore, if it is necessary to strictly control the amount of cation exchange resin withdrawn, as shown in FIGS. 5 and 6, a means 12 for detecting the separation interface position, such as a conductivity detector, color tone or brightness detection, is used. An optical detector etc. that can be used may be used. These means are already known, and the purpose can be easily achieved by installing the detector above the cation exchange resin outlet and below the drain pipe 8.
次にカチオン再生塔２においてカチオン交換樹
脂引き抜き口６より表層部の樹脂を引き抜き、カ
チオン交換樹脂移送管７を介してアニオン再生塔
１に移送し再度アニオン再生塔１で逆洗する（第
１図ｄ）。これによりカチオン再生塔２にアニオ
ン交換樹脂が仮にわずかであるが持ち込まれたと
しても逆洗を行なうことでカチオン交換樹脂の表
層部に分離されるため、表層部の樹脂をアニオン
再生塔１に移送することによりアニオン交換樹脂
のカチオン再生塔２での混入率を更に低減するこ
とができる利点がある。 Next, in the cation regeneration tower 2, the resin in the surface layer is extracted from the cation exchange resin extraction port 6, transferred to the anion regeneration tower 1 via the cation exchange resin transfer pipe 7, and backwashed in the anion regeneration tower 1 again (Fig. 1). d). As a result, even if a small amount of anion exchange resin is brought into the cation regeneration tower 2, it will be separated into the surface layer of the cation exchange resin by backwashing, and the resin in the surface layer will be transferred to the anion regeneration tower 1. By doing so, there is an advantage that the mixing rate of the anion exchange resin in the cation regeneration tower 2 can be further reduced.
また、第２の利点はカチオン交換樹脂をアニオ
ン再生塔１からカチオン再生塔２に移送するに際
して、移送するカチオン交換樹脂の樹脂量をあま
り厳密に制御する必要がないことである。この移
送に際して注意しなければならない点は、アニオ
ン再生塔１内のカチオン交換樹脂を再生に必要な
カチオン交換樹脂よりも少し過剰にカチオン再生
塔２へ移送すること即ちカチオン交換樹脂引き抜
き口６よりもカチオン交換樹脂層表面が上になる
ようにすることであり、かつアニオン再生塔１に
おける分離界面近傍の樹脂をカチオン再生塔２に
持ち込まないことだけである。これらの注意点は
カチオン交換樹脂量に余裕さえあれば容易に解決
がつくことである。 The second advantage is that when the cation exchange resin is transferred from the anion regeneration tower 1 to the cation regeneration tower 2, it is not necessary to control the amount of the cation exchange resin transferred very strictly. The point to be noted during this transfer is that the cation exchange resin in the anion regeneration tower 1 should be transferred to the cation regeneration tower 2 in a slightly excess amount than the cation exchange resin necessary for regeneration, that is, the cation exchange resin in the anion regeneration tower 1 should be transferred to the cation exchange tower 2 in excess of the cation exchange resin required for regeneration. The only thing to do is to make sure that the surface of the cation exchange resin layer is on top, and to not bring the resin near the separation interface in the anion regeneration tower 1 into the cation regeneration tower 2. These precautions can be easily solved if there is enough cation exchange resin.
次にアニオン再生塔１においてアニオン交換樹
脂を再生する際に、苛性ソーダ等のアルカリ溶液
を通薬するがアニオン再生塔１の塔底部より上側
でかつアニオン交換樹脂層中に位置する排水管８
からアルカリ廃液を塔外に排出し、続いて洗浄を
行う。ここで排水管８の位置を更に詳しく説明す
れば、逆洗によつてアニオン再生塔１の底部に分
離されたカチオン交換樹脂よりもできる限り上側
でかつアニオン交換樹脂引き抜き口９より下側に
設置する。この排水管８の位置は厳密に考慮され
る必要はなく、樹脂混合塔３に移送するに必要な
アニオン交換樹脂よりも過剰となるようあらかじ
め別途にアニオン交換樹脂をアニオン再生塔１に
充填しておけば良い、即ち過剰のアニオン交換樹
脂の樹脂量が多い程排水管８の位置を更に上側に
設置することができ、アニオン再生塔１の底部に
あるカチオン交換樹脂との距離を隔離させること
が容易となる。従つて該カチオン交換樹脂がアル
カリと接触することなくアニオン交換樹脂の再生
が行なえるため、Na+形等のカチオン交換樹脂が
再生工程で生じることを未然に防止できる。更に
アニオン再生塔１から樹脂混合塔３へアニオン交
換樹脂を移送する際、排水管８より上側でかつア
ニオン交換樹脂層中に位置するアニオン交換樹脂
引き抜き口９より上層のアニオン交換樹脂をアニ
オン交換樹脂移送管１０を介して樹脂混合塔３へ
移送することにより、アニオン再生塔１内のカチ
オン交換樹脂が樹脂混合塔３に持ち込まれること
を極力防止することができる。 Next, when regenerating the anion exchange resin in the anion regeneration tower 1, an alkaline solution such as caustic soda is passed through the drain pipe 8, which is located above the bottom of the anion regeneration tower 1 and in the anion exchange resin layer.
The alkaline waste liquid is discharged to the outside of the tower and then washed. To explain the position of the drain pipe 8 in more detail, it is installed as far as possible above the cation exchange resin separated at the bottom of the anion regeneration tower 1 by backwashing and below the anion exchange resin outlet 9. do. The position of this drain pipe 8 does not need to be strictly considered, and the anion regeneration tower 1 is separately filled with anion exchange resin in advance so that the anion exchange resin is in excess of the anion exchange resin required to be transferred to the resin mixing tower 3. In other words, the greater the amount of excess anion exchange resin, the higher the position of the drain pipe 8 can be installed, and the more it is possible to isolate the distance from the cation exchange resin at the bottom of the anion regeneration tower 1. It becomes easier. Therefore, since the anion exchange resin can be regenerated without the cation exchange resin coming into contact with an alkali, it is possible to prevent the generation of cation exchange resin such as Na + form during the regeneration process. Furthermore, when transferring the anion exchange resin from the anion regeneration tower 1 to the resin mixing tower 3, the anion exchange resin in the layer above the anion exchange resin extraction port 9 located above the drain pipe 8 and in the anion exchange resin layer is converted into an anion exchange resin. By transferring the resin to the resin mixing tower 3 via the transfer pipe 10, it is possible to prevent the cation exchange resin in the anion regeneration tower 1 from being carried into the resin mixing tower 3 as much as possible.
また、再生されたカチオン交換樹脂はカチオン
再生塔２よりカチオン交換樹脂移送管１１を介し
て樹脂混合塔３へ移送し、樹脂混合塔３内の樹脂
を通常空気を導入することで均一に混合する。こ
の混合された樹脂は必要に応じて脱塩塔に移送す
るか、もしくは樹脂混合塔３内に保管する。 In addition, the regenerated cation exchange resin is transferred from the cation regeneration tower 2 to the resin mixing tower 3 via the cation exchange resin transfer pipe 11, and the resin in the resin mixing tower 3 is mixed uniformly by usually introducing air. . This mixed resin is transferred to a demineralization tower or stored in the resin mixing tower 3 as required.
以上の一連の工程によつて混合イオン交換樹脂
の再生工程を構成することで、何ら特別な装置や
より高度な技術を用いることなく、更に再生シス
テムで塔の数を増加すうことなく、容易に高純度
な純水を得ることができる。 By configuring the regeneration process of mixed ion exchange resin through the above series of steps, it can be easily performed without using any special equipment or more advanced technology, and without increasing the number of columns in the regeneration system. High purity water can be obtained.
〔発明の効果〕
以上述べたことからも明らかなように、本発明
は従来カチオン再生塔で行なわれたアニオン交換
樹脂とカチオン交換樹脂の分離をアニオン再生塔
で行なうことにより、カチオン再生塔の塔直径を
できる限り小さくし、更に各再生塔間で樹脂を移
送する操作を単に繰り返えすことによつて、従来
法とは比較にならない程の両イオン交換樹脂の分
離を可能とし、脱塩塔処理水の水質を飛躍的に向
上することができる。 [Effects of the Invention] As is clear from the above, the present invention enables the separation of anion exchange resin and cation exchange resin, which was conventionally performed in a cation regeneration tower, into an anion regeneration tower. By making the diameter as small as possible and simply repeating the operation of transferring the resin between each regeneration tower, it is possible to separate both ion exchange resins to a degree that is incomparable to conventional methods. The quality of treated water can be dramatically improved.
第１図は、本発明のイオン交換樹脂の再生工程
を説明するための図、第２図は脱塩塔における
Na+形カチオン交換樹脂混入率と脱塩塔出口水の
Na+イオン濃度との関係を示す図、第３図は脱塩
塔におけるCl-形アニオン交換樹脂混入率と脱塩
塔出口水のCl-イオン濃度との関係を示す図、第
４図は再生塔の直径と塔断面積の関係を示す図、
第５図及び第６図は検知器を用いてカチオン交換
樹脂とアニオン交換樹脂の界面を検知する状態を
説明するための図面、第７図及び第８図は二層に
分離されたカチオン交換樹脂とアニオン交換樹脂
の界面並びに界面における両イオン交換樹脂の混
入状態を説明するための図面である。
１……アニオン再生塔、２……カチオン再生
塔、３……樹脂混合塔、４……混合樹脂移送管、
５……カチオン交換樹脂移送管、６……カチオン
交換樹脂引き抜き口、７……カチオン交換樹脂移
送管、８……排水管、９……アニオン交換樹脂引
き抜き口、１０……アニオン交換樹脂移送管、１
１……カチオン交換樹脂移送管、１２……検出
器。
Figure 1 is a diagram for explaining the regeneration process of the ion exchange resin of the present invention, and Figure 2 is a diagram for explaining the regeneration process of the ion exchange resin of the present invention.
Contamination rate of Na + type cation exchange resin and demineralization tower outlet water
Figure 3 shows the relationship between the Na + ion concentration, Figure 3 shows the relationship between the Cl - form anion exchange resin contamination rate in the demineralization tower and the Cl - ion concentration in the demineralization tower outlet water, and Figure 4 shows the regeneration Diagram showing the relationship between tower diameter and tower cross-sectional area,
Figures 5 and 6 are diagrams for explaining how a detector is used to detect the interface between a cation exchange resin and an anion exchange resin, and Figures 7 and 8 are cation exchange resins separated into two layers. FIG. 2 is a diagram for explaining the interface between the anion exchange resin and the anion exchange resin, and the state of mixing of both ion exchange resins at the interface. 1... Anion regeneration tower, 2... Cation regeneration tower, 3... Resin mixing tower, 4... Mixed resin transfer pipe,
5...Cation exchange resin transfer pipe, 6...Cation exchange resin extraction port, 7...Cation exchange resin transfer pipe, 8...Drain pipe, 9...Anion exchange resin extraction port, 10...Anion exchange resin transfer pipe ,1
1...Cation exchange resin transfer tube, 12...Detector.
Claims (1)
ける混合イオン交換樹脂の再生方法において、 (a) 脱塩工程を終了した脱塩塔の混合イオン交換
樹脂を、あらかじめ別途に用意した混合イオン
交換樹脂を底部に装入したアニオン交換樹脂再
生塔に移送する工程。 (b) 該アニオン交換樹脂再生塔内で逆洗を行ない
下層がカチオン交換樹脂、上層がアニオン交換
樹脂層となるように混合イオン交換樹脂を上下
二層に分離成層させる工程。 (c) 該アニオン交換樹脂再生塔底部よりカチオン
交換樹脂を引き抜いてカチオン交換樹脂再生塔
に移送する工程。 (d) 該カチオン交換樹脂再生塔においてカチオン
交換樹脂を逆洗し、該カチオン交換樹脂層中に
位置するカチオン交換樹脂引き抜き口から、該
カチオン交換樹脂引き抜き口より上層の樹脂を
引き抜いてアニオン交換樹脂再生塔に移送する
工程。 (e) カチオン交換樹脂再生塔には塩酸もしくは硫
酸等の鉱酸を通薬し、続いて洗浄を行ない、ま
たアニオン交換樹脂再生塔においては再度逆洗
を行ない上層がアニオン交換樹脂、下層がカチ
オン交換樹脂の上下二層となるように分離成層
したのち、水酸化ナトリウム等のアルカリ溶液
を通薬しアニオン交換樹脂層中に位置する排水
管よりアルカリ廃液を塔外に排出し、続いて洗
浄を行なう工程。 (f) カチオン交換樹脂再生塔内のカチオン交換樹
脂を樹脂混合塔に移送し、またアニオン交換樹
脂再生塔においては、前記排水管より上側でか
つアニオン交換樹脂層中に位置するアニオン交
換樹脂引き抜き口から、該アニオン交換樹脂を
引き抜いて前記樹脂混合塔に移送し、続いて樹
脂混合塔内の樹脂を混合する工程。 (g) 該樹脂混合塔内で混合された樹脂を続いて前
記脱塩塔に移送する工程。 以上の一連の工程によつて構成することを特徴
とする混合イオン交換樹脂の再生方法。 ２ 前記工程(c)において、カチオン交換樹脂の移
送時間をあらかじめ設定しておくことによりカチ
オン交換樹脂の引き抜き量を制御する特許請求の
範囲第１項に記載の混合イオン交換樹脂の再生方
法。 ３ 前記工程(c)において、二層に成層した分離界
面位置を検知する手段を持ち、カチオン交換樹脂
の移送工程の進行に伴つて下降する前記分離界面
の位置が所定位置に達した時点をもつて移送を終
了することにより、カチオン交換樹脂の引き抜き
量を制御する特許請求の範囲第１項に記載の混合
イオン交換樹脂の再生方法。[Scope of Claims] 1. In a method for regenerating a mixed ion exchange resin in an external regeneration type mixed bed ion exchange desalination apparatus, (a) the mixed ion exchange resin of a desalination tower that has completed a desalination process is A process of transferring a separately prepared mixed ion exchange resin to an anion exchange resin regeneration tower charged at the bottom. (b) A step of performing backwashing in the anion exchange resin regeneration tower to separate and stratify the mixed ion exchange resin into two layers, an upper layer and an upper layer, such that the lower layer is a cation exchange resin layer and the upper layer is an anion exchange resin layer. (c) A step of extracting the cation exchange resin from the bottom of the anion exchange resin regeneration tower and transferring it to the cation exchange resin regeneration tower. (d) The cation exchange resin is backwashed in the cation exchange resin regeneration tower, and the resin in the layer above the cation exchange resin extraction port is pulled out from the cation exchange resin extraction port located in the cation exchange resin layer to regenerate the anion exchange resin. The process of transferring to the regeneration tower. (e) Mineral acids such as hydrochloric acid or sulfuric acid are passed through the cation exchange resin regeneration tower, followed by washing, and the anion exchange resin regeneration tower is backwashed again so that the upper layer contains the anion exchange resin and the lower layer contains the cation exchange resin. After separating and stratifying the exchange resin into upper and lower layers, an alkaline solution such as sodium hydroxide is passed through the anion exchange resin layer, and the alkaline waste liquid is discharged outside the tower from a drain pipe located in the anion exchange resin layer, followed by washing. process to perform. (f) The cation exchange resin in the cation exchange resin regeneration tower is transferred to the resin mixing tower, and in the anion exchange resin regeneration tower, the anion exchange resin withdrawal port is located above the drain pipe and in the anion exchange resin layer. A step of extracting the anion exchange resin from the resin mixing column and transferring it to the resin mixing column, and then mixing the resin in the resin mixing column. (g) A step of subsequently transferring the resin mixed in the resin mixing tower to the demineralization tower. A method for regenerating a mixed ion exchange resin, characterized by comprising the above series of steps. 2. The method for regenerating a mixed ion exchange resin according to claim 1, wherein in the step (c), the amount of cation exchange resin withdrawn is controlled by setting the transfer time of the cation exchange resin in advance. 3. In step (c), the method includes a means for detecting the position of the separation interface formed in two layers, and has a point in time when the position of the separation interface, which descends as the cation exchange resin transfer step progresses, reaches a predetermined position. 2. The method for regenerating a mixed ion exchange resin according to claim 1, wherein the amount of cation exchange resin withdrawn is controlled by terminating the transfer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61047189A JPS62204855A (en) | 1986-03-06 | 1986-03-06 | Regeneration of ion exchange resin mixture |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61047189A JPS62204855A (en) | 1986-03-06 | 1986-03-06 | Regeneration of ion exchange resin mixture |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS62204855A JPS62204855A (en) | 1987-09-09 |
| JPH058059B2 true JPH058059B2 (en) | 1993-02-01 |
Family
ID=12768158
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61047189A Granted JPS62204855A (en) | 1986-03-06 | 1986-03-06 | Regeneration of ion exchange resin mixture |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS62204855A (en) |
-
1986
- 1986-03-06 JP JP61047189A patent/JPS62204855A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS62204855A (en) | 1987-09-09 |
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