JP2001054738A - Column and method for separating mixed ion exchange resins - Google Patents
Column and method for separating mixed ion exchange resinsInfo
- Publication number
- JP2001054738A JP2001054738A JP2000171527A JP2000171527A JP2001054738A JP 2001054738 A JP2001054738 A JP 2001054738A JP 2000171527 A JP2000171527 A JP 2000171527A JP 2000171527 A JP2000171527 A JP 2000171527A JP 2001054738 A JP2001054738 A JP 2001054738A
- Authority
- JP
- Japan
- Prior art keywords
- exchange resin
- resin
- collector
- layer
- mixed
- 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.)
- Granted
Links
Landscapes
- Treatment Of Water By Ion Exchange (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、混合状態で使用し
機能の低下した陽イオン交換樹脂及び陰イオン交換樹脂
を相互に分離し再生するための混合イオン交換樹脂の分
離塔及び該分離塔を用いた混合イオン交換樹脂の分離方
法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a mixed ion exchange resin separation column for separating and regenerating a cation exchange resin and an anion exchange resin having reduced functions, which are used in a mixed state, and a method for separating the same. The present invention relates to a method for separating a mixed ion exchange resin used.
【０００２】[0002]
【従来の技術】超臨界圧ボイラー、原子力発電及び半導
体製造には、極めて高純度な純水が要求されている。従
来、高純度の純水を製造する装置として、陽イオン交換
樹脂及び陰イオン交換樹脂を混合状態で使用する混床式
純水製造装置が広く採用されている。この装置では、使
用によりイオン交換樹脂の能力が低下した場合、これら
の樹脂を再生する必要があるが、再生に当たっては、ま
ずこれらの樹脂を分離塔へ移送する。そこで分離塔では
混合イオン交換樹脂層の下部より水を上向きにいわゆる
逆洗水を流入し、陽イオン交換樹脂及び陰イオン交換樹
脂の比重差を利用して陽イオン交換樹脂層及び陰イオン
交換樹脂層に成層分離する逆洗分離工程が行われる。2. Description of the Related Art Supercritical pressure boilers, nuclear power generation and semiconductor production require extremely high purity pure water. 2. Description of the Related Art Conventionally, as a device for producing high-purity pure water, a mixed-bed type pure water production device using a cation exchange resin and an anion exchange resin in a mixed state has been widely adopted. In this apparatus, when the capacity of the ion exchange resin is reduced by use, it is necessary to regenerate these resins. In the regeneration, these resins are first transferred to a separation column. So, in the separation tower, so-called backwash water flows upward from the lower part of the mixed ion exchange resin layer, and the difference in specific gravity between the cation exchange resin and the anion exchange resin is used. A backwash separation step of stratifying and separating the layers is performed.
【０００３】次いで、逆洗に続く沈静工程の後、この成
層分離した陽イオン交換樹脂層及び陰イオン交換樹脂層
を必要に応じそれぞれを系外に取り出すなどして分離
し、個別に再生剤で再生する再生工程を行う。再生・洗
浄された両イオン交換樹脂はイオン交換装置に戻され混
合工程を経て再び純水製造に供される。上記逆洗分離工
程後の沈静工程では、殆どの陽イオン交換樹脂は下層部
に、陰イオン交換樹脂は上層部に成層分離されるが、両
イオン交換樹脂を完全に分離することは困難で両イオン
交換樹脂層の境界面付近には陽イオン交換樹脂及び陰イ
オン交換樹脂が混在する混合樹脂層が必ず生ずる。[0003] Next, after a settling step following backwashing, the layered cation-exchange resin layer and anion-exchange resin layer are separated as necessary by taking them out of the system, and individually separated with a regenerant. A regenerating step for regenerating is performed. Both of the regenerated and washed ion exchange resins are returned to the ion exchange device, subjected to a mixing step, and again supplied to pure water production. In the settling step after the backwash separation step, most of the cation exchange resin is separated into the lower layer and the anion exchange resin is separated into the upper layer, but it is difficult to completely separate both ion exchange resins. A mixed resin layer in which a cation exchange resin and an anion exchange resin are mixed always occurs near the boundary surface of the ion exchange resin layer.
【０００４】そのため、従来の方法では各々のイオン交
換樹脂層を分離し取り出す際に、この混合樹脂層の一部
がそれぞれのイオン交換樹脂層に同伴されるので、再生
工程、即ち、陰イオン交換樹脂の再生では付随した陽イ
オン交換樹脂は陰イオン交換樹脂の再生剤、例えば水酸
化ナトリウム水溶液に接触してＮａ形に、一方陽イオン
交換樹脂の再生では随伴した陰イオン交換樹脂は陽イオ
ン交換樹脂の再生剤、例えば硫酸に接触してＳＯ4形に
なるいわゆる逆再生現象が生じることは避けられない。
しかして、再生後の両樹脂を用いて高純度の純水を製造
するためには陽イオン交換樹脂は全てＨ形に、陰イオン
交換樹脂は全てＯＨ形にしなければならず、分離の際の
混合樹脂層の同伴は極めて不都合である。Therefore, in the conventional method, when each ion exchange resin layer is separated and taken out, a part of the mixed resin layer is entrained with each ion exchange resin layer. In the regeneration of the resin, the accompanying cation exchange resin is brought into the Na form by contacting with an anion exchange resin regenerant, for example, an aqueous sodium hydroxide solution, while in the regeneration of the cation exchange resin, the accompanying anion exchange resin is converted into a cation exchange resin. It is inevitable that a so-called reverse regeneration phenomenon occurs when the resin comes into contact with a resin regenerant, for example, sulfuric acid, to form SO 4 .
Thus, in order to produce high-purity pure water using both resins after regeneration, all cation exchange resins must be in the H form and all anion exchange resins must be in the OH form. Entrainment of the mixed resin layer is extremely inconvenient.
【０００５】このような混合樹脂層の同伴による不都合
を解消するために、成層分離後の両イオン交換樹脂層の
境界面付近の上部及び下部に二本の樹脂抜き出しコレク
ターを設け、陰イオン交換樹脂層は上部樹脂コレクター
で、また混合樹脂層は下部樹脂コレクターでそれぞれ系
外に取り出すことにより陽イオン交換樹脂層、陰イオン
交換樹脂層及び混合樹脂層に分離し、分離した陽・陰両
イオン交換樹脂層のみを再生して脱塩処理に供する方法
が提案されている（特開昭５６−３８ｌ３６）。この方
法によれば、下部の樹脂コレクターにより混合樹脂層の
殆どを取り出すことができるが、それでも混合樹脂層と
接した陽イオン交換樹脂層の表層面には微量の陰イオン
交換樹脂が安息角状に残留するので、この陽イオン交換
樹脂を再生使用した場合高純度の純水が安定して得られ
ない間題点があった。下部樹脂コレクターから混合樹脂
層を抜き出す際、混合樹脂層付近の陽イオン交換樹脂層
の一部をより多量に除去することで陽イオン交換樹脂へ
の陰イオン交換樹脂の付随問題を避けることもできる
が、その後に分離・再生処理される樹脂量が増える等経
済的に不利であり好ましくない。In order to eliminate such inconvenience due to entrainment of the mixed resin layer, two resin extraction collectors are provided at the upper and lower portions near the boundary between the ion exchange resin layers after stratification and separation, and the anion exchange resin is provided. The layer is taken out of the system by the upper resin collector, and the mixed resin layer is taken out of the system by the lower resin collector, and separated into a cation exchange resin layer, an anion exchange resin layer and a mixed resin layer. A method has been proposed in which only the resin layer is regenerated and subjected to a desalination treatment (JP-A-56-38136). According to this method, most of the mixed resin layer can be taken out by the lower resin collector, but a small amount of anion exchange resin still has a repose angle on the surface of the cation exchange resin layer in contact with the mixed resin layer. Therefore, when this cation exchange resin is recycled, high-purity pure water cannot be stably obtained. When extracting the mixed resin layer from the lower resin collector, a portion of the cation exchange resin layer near the mixed resin layer is removed in a larger amount, thereby avoiding the problem of anion exchange resin accompanying the cation exchange resin. However, it is economically disadvantageous, such as an increase in the amount of resin to be subsequently separated and regenerated, which is not preferable.
【０００６】[0006]
【発明が解決しようとする課題】本発明者等は上記問題
を解消するため、混合イオン交換樹脂の成層分離におけ
る陰・陽イオン交換樹脂層の状態について鋭意検討を加
えた結果、混合イオン交換樹脂の逆洗による成層分離後
の混合樹脂層はその内部において、陽イオン交換樹脂と
陰イオン交換樹脂が不明瞭ながらも境界面を形成し、陽
イオン交換樹脂に富む層と陰イオン交換樹脂に富む層の
二層構造となっており、この混合樹脂層を下部コレクタ
ーで抜き出す場合、陽イオン交換樹脂に富む層次いで陰
イオン交換樹脂に富む層の順に抜き出されるため、この
陰イオン交換樹脂に富む層の陰イオン交換樹脂が陽イオ
ン交換樹脂層の表層面に安息角状に残留することを知見
し本発明に到達した。SUMMARY OF THE INVENTION In order to solve the above-mentioned problems, the present inventors have made intensive studies on the state of the anion / cation exchange resin layer in the stratified separation of the mixed ion exchange resin. In the mixed resin layer after stratification separation by backwashing, the boundary between the cation exchange resin and the anion exchange resin is formed even though the cation exchange resin and the anion exchange resin are unclear, and the cation exchange resin-rich layer and the anion exchange resin are rich It has a two-layer structure, and when this mixed resin layer is extracted with a lower collector, it is extracted in the order of a layer rich in cation exchange resin and then a layer rich in anion exchange resin, so that it is rich in this anion exchange resin The inventors have found that the anion exchange resin in the layer remains on the surface layer of the cation exchange resin layer at a repose angle and arrived at the present invention.
【０００７】[0007]
【課題を解決するための手段】本発明は、脱塩処理等に
使用して機能の低下した混合イオン交換樹脂を逆洗によ
り成層分離して再生処理に付するための混合イオン交換
樹脂の効率的な分離塔及び該分離塔を用いた混合イオン
交換樹脂の分離方法を提供するものである。即ち、本発
明の要旨は、陽イオン交換樹脂と陰イオン交換樹脂から
なる混合イオン交換樹脂を逆洗により相互に成層分離す
る分離塔であり、該塔内に成層分離後の陰イオン交換樹
脂層と陽イオン交換樹脂層との算出分離界面付近に、該
算出分離界面を介して上部樹脂コレクターと下部樹脂コ
レクターが内設され、且つ該上部樹脂コレクターと下部
樹脂コレクターの間に樹脂抜き出しノズルが設置されて
いることを特徴とする混合イオン交換樹脂の分離塔に存
する。SUMMARY OF THE INVENTION The present invention relates to an efficiency of a mixed ion exchange resin which is used for desalination treatment or the like and which has a reduced function and which is subjected to stratification separation by backwashing and subjected to a regeneration treatment. And a method for separating a mixed ion exchange resin using the separation tower. That is, the gist of the present invention is a separation column in which a mixed ion exchange resin composed of a cation exchange resin and an anion exchange resin is stratified and separated from each other by backwashing. An upper resin collector and a lower resin collector are provided in the vicinity of the calculated separation interface between the resin collector and the cation exchange resin layer, and a resin extraction nozzle is provided between the upper resin collector and the lower resin collector. And a separation tower for the mixed ion exchange resin.
【０００８】本発明の他の要旨は、陽イオン交換樹脂と
陰イオン交換樹脂からなる混合イオン交換樹脂を逆洗に
より相互に成層分離する分離塔であり、該塔内に成層分
離後の陰イオン交換樹脂層と陽イオン交換樹脂層との算
出分離界面付近に、該算出分離界面を介して上部樹脂コ
レクターと下部樹脂コレクターが内設され、且つ該上部
樹脂コレクターと下部樹脂コレクターの間に樹脂抜き出
しノズルが設置されている混合イオン交換樹脂の分離塔
を用いて混合イオン交換樹脂を分離する方法において、
該塔に移送された分離すべき陽イオン交換樹脂と陰イオ
ン交換樹脂との混合イオン交換樹脂に該塔底部に設けた
下部集水管より逆洗水を導入して混合イオン交換樹脂を
流動展開させた後、逆洗水の導入を停止して静置させ、
陰イオン交換樹脂層、混合イオン交換樹脂層および陽イ
オン交換樹脂層とに成層分離する第１工程、該塔の頂部
に設けた上部集水管より移送水または加圧空気を導入し
て上部樹脂コレクターより該陰イオン交換樹脂層を抜き
出す第２工程、上部樹脂コレクターを閉じ、下部樹脂コ
レクターより移送水を導入して該混合樹脂層を流動させ
ながら上部集水管から移送水または加圧空気を導入し
て、上部下部両樹脂コレクターの間に設けた樹脂抜き出
しノズルより該混合樹脂層の上層部分を抜き出す第３工
程、下部樹脂コレクターからの移送水の導入を停止し、
更に樹脂抜き出しノズルを閉じて上部集水管から移送水
または加圧空気を導入しながら下部樹脂コレクターより
該混合樹脂の下層部分を取り出す第４工程を順次行うこ
とを特徴とする混合イオン交換樹脂の分離方法に存す
る。Another aspect of the present invention is a separation column for separating and stratifying mixed ion exchange resins comprising a cation exchange resin and an anion exchange resin by backwashing each other. In the vicinity of the calculated separation interface between the exchange resin layer and the cation exchange resin layer, an upper resin collector and a lower resin collector are provided through the calculated separation interface, and the resin is drawn out between the upper resin collector and the lower resin collector. In a method of separating a mixed ion exchange resin using a mixed ion exchange resin separation tower in which a nozzle is installed,
Backwash water is introduced into the mixed ion-exchange resin of the cation-exchange resin and anion-exchange resin to be separated transferred to the column from the lower water collecting tube provided at the bottom of the column to flow and develop the mixed ion-exchange resin. After that, stop introducing backwash water and let it stand,
A first step of forming a layer into an anion exchange resin layer, a mixed ion exchange resin layer and a cation exchange resin layer, and introducing transfer water or pressurized air from an upper collecting pipe provided at the top of the tower to form an upper resin collector A second step of extracting the anion exchange resin layer from the upper resin collector, closing the upper resin collector, introducing transfer water from the lower resin collector and introducing transfer water or pressurized air from the upper collecting pipe while flowing the mixed resin layer. A third step of extracting the upper layer portion of the mixed resin layer from a resin extraction nozzle provided between the upper and lower resin collectors, stopping introduction of transfer water from the lower resin collector,
And separating the mixed ion-exchange resin by sequentially performing a fourth step of removing the lower layer portion of the mixed resin from the lower resin collector while introducing the transfer water or pressurized air from the upper collecting pipe while closing the resin extracting nozzle. Be in the way.
【０００９】本発明の好適な態様として、該樹脂抜き出
しノズルは、ノズル内面の最下端位置が成層分離した陰
イオン交換樹脂層と陽イオン交換樹脂層の算出分離界面
あるいはやや下方に略位置するように設置されているこ
と、該上部樹脂コレクターは、成層分離した陰イオン交
換樹脂層と陽イオン交換樹脂層の算出分離界面から約１
００〜５００ｍｍ上位の陰イオン交換樹脂層内に設置さ
れ、また該下部樹脂コレクターは、成層分離した陰イオ
ン交換樹脂層と陽イオン交換樹脂層の算出分離界面から
約５０〜３００ｍｍ下位の陽イオン交換樹脂層内に設置
されること、該上部樹脂コレクター及び該下部樹脂コレ
クターは、分離塔壁を貫通して設けられ、複数の樹脂抜
き出し穴を有すること、及び該混合イオン交換樹脂が脱
塩処理に使用したものであることよりなる上記混合イオ
ン交換樹脂の分離塔を示すことができる。In a preferred embodiment of the present invention, the lowermost position of the inner surface of the resin extraction nozzle is located substantially below or slightly below the calculated separation interface between the anion exchange resin layer and the cation exchange resin layer, which are stratified and separated. The upper resin collector is located approximately one hour from the calculated separation interface between the stratified and separated anion exchange resin layer and the cation exchange resin layer.
It is installed in the anion-exchange resin layer at a level of 00 to 500 mm, and the lower resin collector is a cation-exchange resin about 50 to 300 mm lower from the calculated separation interface between the stratified and separated anion-exchange resin layer and the cation-exchange resin layer. Being installed in a resin layer, the upper resin collector and the lower resin collector being provided through the separation tower wall, having a plurality of resin extraction holes, and allowing the mixed ion exchange resin to undergo desalination treatment. It is possible to show a separation tower of the mixed ion exchange resin which is used.
【００１０】[0010]
【発明の実施の形態】本発明の混合イオン交換樹脂の分
離塔は、超臨界ボイラーや原子力発電の復水脱塩処理、
或いは超純水の製造などに採用されている混床式純水製
造装置において使用され、機能低下した混合イオン交換
樹脂を再生する際の混合樹脂の相互分離に利用される。
本発明の分離塔に適用される混合イオン交換樹脂の陽イ
オン交換樹脂は、具体的には強酸性陽イオン交換樹脂で
あり、例えばダイヤイオンＰＫ２２８、ＰＫ２１６、Ｓ
Ｋ１Ｂ、ＳＫ１１０、ＳＫ１１２（商品名：三菱化学
（株）製）等の市販品が挙げられ、また陰イオン交換樹
脂は、強塩基性陰イオン交換樹脂であり、ダイヤイオン
ＰＡ３１２、ＰＡ３１６、ＳＡ１０Ａ、ＳＡ１１Ａ、Ｓ
Ａ１２Ａ（商品名：三菱化学（株）製）等の市販品が挙
げられる。［尚、ダイヤイオンは三菱化学（株）の登録
商標である。］BEST MODE FOR CARRYING OUT THE INVENTION A separation tower for a mixed ion exchange resin according to the present invention can be used for a supercritical boiler or a condensate desalination treatment for nuclear power generation.
Alternatively, it is used in a mixed-bed type pure water production apparatus employed for production of ultrapure water and the like, and is used for mutual separation of mixed resins when regenerating a degraded mixed ion exchange resin.
The cation exchange resin of the mixed ion exchange resin applied to the separation column of the present invention is specifically a strongly acidic cation exchange resin, for example, Diaion PK228, PK216, S
Commercially available products such as K1B, SK110, and SK112 (trade name: manufactured by Mitsubishi Chemical Corporation) can be mentioned. The anion exchange resin is a strong basic anion exchange resin, and DIAION PA312, PA316, SA10A, and SA11A. , S
Commercial products such as A12A (trade name: manufactured by Mitsubishi Chemical Corporation) and the like can be mentioned. [Diaion is a registered trademark of Mitsubishi Chemical Corporation. ]
【００１１】次に本発明の混合イオン交換樹脂の分離塔
及び分離塔を用いて混合イオン交換樹脂を分離する方法
を図１に従って説明する。図１は、本発明の分離塔で混
合イオン交換樹脂を逆洗により成層分離した後の状態を
模式的に示す縦断面略図の一例である。図中、１は分離
塔，２は混合イオン交換樹脂の導入管，３は陰イオン交
換樹脂層，４は陽イオン交換樹脂層，５は混合樹脂層，
６は陰イオン交換樹脂層と陽イオン交換樹脂層との分離
境界面，７は上部樹脂コレクター，８は下部樹脂コレク
ター，９は混合樹脂抜き出しノズル，１０は陽イオン交
換樹脂抜き出し管，１１は上部集水管，１２は下部集水
管である。Next, the separation tower of the mixed ion exchange resin of the present invention and the method of separating the mixed ion exchange resin using the separation tower will be described with reference to FIG. FIG. 1 is an example of a schematic vertical cross-sectional view schematically showing a state after a mixed ion exchange resin is separated into layers by backwashing in a separation tower of the present invention. In the figure, 1 is a separation tower, 2 is a mixed ion exchange resin introduction tube, 3 is an anion exchange resin layer, 4 is a cation exchange resin layer, 5 is a mixed resin layer,
6 is a separation interface between the anion exchange resin layer and the cation exchange resin layer, 7 is an upper resin collector, 8 is a lower resin collector, 9 is a mixed resin extraction nozzle, 10 is a cation exchange resin extraction tube, and 11 is an upper portion. A collecting pipe 12 is a lower collecting pipe.
【００１２】本発明の分離塔において、上部樹脂コレク
ター７は陰イオン交換樹脂の抜き出し管であり、その設
置位置は成層分離後の陰イオン交換樹脂層３の内部でか
つ陰イオン交換樹脂の有効利用の面からはできるだけ該
樹脂層の下層部が望ましい。しかし、陽イオン交換樹脂
の混入を防止するためには、分離塔に導入される陰・陽
両イオン交換樹脂量から算出される計算上の陽イオン交
換樹脂層および陰イオン交換樹脂層の分離界面から上方
約１００〜５００ｍｍの位置に設けるのが好ましい。In the separation tower of the present invention, the upper resin collector 7 is a pipe for extracting an anion exchange resin, and its installation position is inside the anion exchange resin layer 3 after the stratification and effective use of the anion exchange resin. In view of the above, the lower part of the resin layer is desirable as much as possible. However, in order to prevent contamination of the cation exchange resin, the separation interface between the cation exchange resin layer and the anion exchange resin layer calculated from the amount of the anion and cation exchange resin introduced into the separation column is calculated. It is preferably provided at a position of about 100 to 500 mm above.
【００１３】また下部樹脂コレクター８は、混合樹脂層
の一部抜き出し管であると同時に混合樹脂層の上層部分
の抜き出しの際の移送水の供給管でもある。それ故、混
合樹脂層の抜き出しでは、その設置位置は陽イオン交換
樹脂層４の内部でかつ陽イオン交換樹脂の層の上部にで
きるだけ近い位置が望ましいが、混合樹脂層を流動化
し、混合樹脂抜き出しノズル９から効率良く抜き出すた
めの移送水を導入するので、算出した分離界面から下方
約５０〜３００ｍｍの位置に設けるのが好ましい。各樹
脂コレクターの形状は特に制限されないが、複数の樹脂
抜き出し穴を有するものが好ましく、例えば一本の抜き
出し管に適宜の間隔で複数の樹脂抜き出し穴をあけたも
の、あるいは一本の抜き出し集合管に複数本の枝管を設
け各枝管には適宣の間隔で複数の樹脂抜き出し穴を設け
たもの等があげられる。これらの樹脂コレクターは塔壁
から貫通して取り付ける。図４Ａ、図４Ｂ及び図５Ａ、
図５Ｂに、上部、下部樹脂コレクターの概略図を示す。The lower resin collector 8 is a pipe for partially extracting the mixed resin layer and also a supply pipe for transporting water when extracting the upper layer of the mixed resin layer. Therefore, when extracting the mixed resin layer, it is desirable that the installation position be inside the cation exchange resin layer 4 and as close as possible to the upper part of the cation exchange resin layer. However, the mixed resin layer is fluidized and the mixed resin is extracted. Since the transfer water for efficiently extracting from the nozzle 9 is introduced, it is preferable that the transfer water is provided at a position about 50 to 300 mm below the calculated separation interface. The shape of each resin collector is not particularly limited, but preferably has a plurality of resin extraction holes, for example, one in which a plurality of resin extraction holes are formed at an appropriate interval in one extraction pipe, or one extraction collecting pipe. And a plurality of branch pipes provided with a plurality of resin extraction holes at appropriate intervals. These resin collectors are mounted through the tower wall. 4A, 4B and 5A,
FIG. 5B shows a schematic view of the upper and lower resin collectors.
【００１４】さらに、本発明の分離塔に於いては上記の
上部及び下部各樹脂コレクターの間に混合樹脂を取り出
す為の樹脂抜き出しノズル９を設けることが必須であ
る。樹脂抜き出しノズル９の設置位置は、算出分離境界
面付近で、好ましくは該分離境界面或いは該分離界面よ
りやや下方の位置に設置すると良い。図２及び図３に樹
脂抜き出しノズル９の取り付け例の断面略図を示すが、
図２のように塔壁に開口設置しても良く、図３のように
コレクターとして塔内に抜き出し管状に設けても良い。
その場合ノズルの内面の最下端及びコレクターの穴の最
下端が両樹脂層の算出分離界面に相当する位置になるよ
うにするのが良い。Further, in the separation tower of the present invention, it is essential to provide a resin extracting nozzle 9 for extracting the mixed resin between the upper and lower resin collectors. The resin extraction nozzle 9 is preferably installed near the calculated separation boundary, preferably at a position slightly below the separation boundary or the separation interface. FIGS. 2 and 3 show schematic cross-sectional views of an example of mounting the resin extraction nozzle 9.
As shown in FIG. 2, an opening may be provided in the tower wall, or as shown in FIG.
In this case, it is preferable that the lowermost end of the inner surface of the nozzle and the lowermost end of the hole of the collector are located at positions corresponding to the calculated separation interface between the two resin layers.
【００１５】次に、本発明の分離塔を用いて混合イオン
交換樹脂を分離する方法を図１に従って説明する。先
ず、分離塔１には混床式純水製造装置で使用された混合
イオン交換樹脂及び別途中間樹脂貯槽に貯槽されていた
混合樹脂が移送水と共に導入管２を通じて導入される。
次に下部集水管１２より逆洗水を流入させ上部集水管１
１より排出しながら混合イオン交換樹脂を流動展開させ
る。しばらくの間展開させた後、逆洗水の流入を停止し
静置させる第１工程を行う。流動していたイオン交換樹
脂は比重差により沈降しながら上部に陰イオン交換樹脂
層３、下部に陽イオン交換樹脂層４、両イオン交換樹脂
層の分離境界面６付近には両イオン交換樹脂の混合樹脂
層５が形成される。図１は、この時点に於ける状態を示
すものである。Next, a method for separating a mixed ion exchange resin using the separation column of the present invention will be described with reference to FIG. First, the mixed ion-exchange resin used in the mixed-bed type pure water production apparatus and the mixed resin separately stored in the intermediate resin storage tank are introduced into the separation tower 1 through the introduction pipe 2 together with the transfer water.
Next, backwash water flows from the lower collecting pipe 12 and the upper collecting pipe 1
The mixed ion exchange resin is fluidized and developed while being discharged from 1. After being developed for a while, the first step of stopping the inflow of the backwash water and allowing it to stand still is performed. The flowing ion-exchange resin settles due to the difference in specific gravity, while the anion-exchange resin layer 3 is at the top, the cation-exchange resin layer 4 is at the bottom, and both ion-exchange resins are near the separation boundary 6 between the two ion-exchange resin layers. The mixed resin layer 5 is formed. FIG. 1 shows the state at this point.
【００１６】次に、上部集水管１１より移送水または加
圧空気を導入して上部樹脂コレクタ−７より陰イオン交
換樹脂層３を抜き出す第２工程を行い、該陰イオン交換
樹脂層３は陰イオン交換樹脂再生塔へ移送し再生され
る。 次いで、上部樹脂コレクタ−７を閉じ、下部樹脂
コレクター８より移送水を導入して混合樹脂層５を流動
させながら上部集水管１１からも移送水または加圧空気
を導入して、上部下部両樹脂コレクターの間に設けた混
合樹脂抜き出しノズル９より混合樹脂層５の上層部分を
抜き出す第３工程を行う。本発明では、下部樹脂コレク
ター８から移送水を供給することによって、混合樹脂層
の上層部分が混合樹脂抜き出しノズル９からより効率的
に除去することができる。次いで、下部樹脂コレクター
８からの移送水の流入を停止し、更に混合樹脂抜き出し
ノズル９を閉じて上部集水管１１から移送水または加圧
空気を導入しながら下部樹脂コレクター８より混合樹脂
層５の下層部分を取り出す第４工程を行う。Next, a second step of introducing transfer water or pressurized air from the upper collecting pipe 11 and extracting the anion exchange resin layer 3 from the upper resin collector 7 is performed. It is transferred to the ion exchange resin regeneration tower and regenerated. Next, the upper resin collector 7 is closed, transfer water is introduced from the lower resin collector 8 and transfer water or pressurized air is also introduced from the upper water collecting pipe 11 while flowing the mixed resin layer 5 so that the upper and lower resin are mixed. A third step of extracting the upper layer portion of the mixed resin layer 5 from the mixed resin extraction nozzle 9 provided between the collectors is performed. In the present invention, by supplying the transfer water from the lower resin collector 8, the upper layer portion of the mixed resin layer can be more efficiently removed from the mixed resin extracting nozzle 9. Next, the inflow of the transfer water from the lower resin collector 8 is stopped, the mixed resin extraction nozzle 9 is closed, and the transfer resin or the pressurized air is introduced from the upper water collecting pipe 11 so that the mixed resin layer 5 is removed from the lower resin collector 8. A fourth step of removing the lower layer portion is performed.
【００１７】本発明では、この様に操作することによ
り、陰イオン交換樹脂に富んだ部分である混合樹脂層５
の上層部分が、ノズル９により取り除かれた後で、下部
樹脂コレクター８により混合樹脂層の下層部分を取り出
すので、陽イオン交換樹脂に富む下層部分と接する陽イ
オン交換樹脂層への陰イオン交換樹脂の残留が避けられ
るのである。第３工程で取り出された混合樹脂層５の上
層部分である陰イオン交換樹脂に富んだ部分と、第４工
程で取り出された混合樹脂層５の下層部分の陽イオン交
換樹脂に富んだ部分は、中間樹脂貯槽に移送され貯槽さ
れる。混合樹脂層が取り出された分離塔内には、純粋な
陽イオン交換樹脂層が残留する。この陽イオン交換樹脂
層は、必要に応じ陽イオン交換樹脂抜き出し管１０によ
り取り出し、陽イオン交換樹脂再生塔に移送し再生して
もよいし、そのまま分離塔内で再生処理することもでき
る。In the present invention, by operating as described above, the mixed resin layer 5 which is a portion rich in anion exchange resin is formed.
After the upper layer is removed by the nozzle 9, the lower layer of the mixed resin layer is taken out by the lower resin collector 8, so that the anion exchange resin to the cation exchange resin layer in contact with the cation exchange resin-rich lower layer is removed. The residue of the is avoided. The portion rich in the anion exchange resin, which is the upper layer portion of the mixed resin layer 5 taken out in the third step, and the portion rich in the cation exchange resin, which is the lower layer portion of the mixed resin layer 5 taken out in the fourth step, Is transferred to the intermediate resin storage tank and stored there. The pure cation exchange resin layer remains in the separation tower from which the mixed resin layer has been removed. This cation-exchange resin layer may be taken out through the cation-exchange resin withdrawal tube 10 as necessary, and transferred to a cation-exchange resin regeneration tower for regeneration, or may be directly regenerated in the separation tower.
【００１８】上記の方法により混合イオン交換樹脂を分
離した場合、通常、陰イオン交換樹脂再生塔には純粋な
陰イオン交換樹脂が、又この分離塔１には純粋な陽イオ
ン交換樹脂が分離貯槽される。この分離された各イオン
交換樹脂は酸またはアルカリの再生剤を用いて各々再生
され、再生後の両樹脂を混合状態にした後、純水製造装
置に供される。一方、混合樹脂抜き出しノズル９及び下
部樹脂コレクター８により分離して中間樹脂貯槽に移送
し貯槽された混合樹脂は、純水製造装置における次回の
混合イオン交換樹脂の分離の際まで待機し、その分離の
際に分離塔に移送供給して一緒に分離操作に付する。こ
のような操作により混合イオン交換樹脂は、純粋な陽イ
オン交換樹脂および陰イオン交換樹脂に分離でき、しか
も樹脂の損失量も低減できる。When the mixed ion-exchange resin is separated by the above method, a pure anion-exchange resin is usually contained in the anion-exchange resin regenerating tower, and a pure cation-exchange resin is contained in the separation tower 1 in a separation tank. Is done. Each of the separated ion-exchange resins is regenerated by using an acid or alkali regenerant, and the two resins after regeneration are mixed to be supplied to a pure water production apparatus. On the other hand, the mixed resin that has been separated by the mixed resin extraction nozzle 9 and the lower resin collector 8 and transferred to the intermediate resin storage tank and stored therein waits until the next separation of the mixed ion exchange resin in the pure water production apparatus, and the separation is performed. At this time, the mixture is supplied to a separation tower and subjected to a separation operation together. By such an operation, the mixed ion exchange resin can be separated into a pure cation exchange resin and an anion exchange resin, and the amount of resin loss can be reduced.
【００１９】以上のように、本発明の分離塔を用いれ
ば、純水の製造に使用されて機能の低下した混合イオン
交換樹脂を分離し再生するに際し、陰イオン交換樹脂は
もちろん、陽イオン交換樹脂層も表層部に陰イオン交換
樹脂を残留させることなく純粋な状態で分離される。従
って、この様にして得た陰イオン交換樹脂及び陽イオン
交換樹脂はそれぞれ純度が高く、各々の樹脂は再生時の
再生剤によるＮａ形の陽イオン交換樹脂及びＳＯ4形の
陰イオン交換樹脂の発生を随伴することもないので、再
生後の両樹脂を用いて高純度の純水を安定して製造する
ことが出来る。As described above, by using the separation tower of the present invention, not only the anion exchange resin but also the cation exchange resin can be used for separating and regenerating the mixed ion exchange resin having a reduced function used in the production of pure water. The resin layer is also separated in a pure state without leaving the anion exchange resin on the surface layer. Therefore, such an anion exchange resin obtained by and cation exchange resin has a high purity, respectively, each of the resin of the Na type by the playback time of the regenerant of the cation exchange resin and SO 4 form of anion exchange resin Since generation is not accompanied, high-purity pure water can be stably produced using both resins after regeneration.
【００２０】[0020]
【実施例】以下に、実施例を挙げて本発明をより詳細に
説明するが、本発明はその要旨を超えない限りこれら実
施例に限定されるものではない。 実施例 図１に示す内径２１００ｍｍ、直胴部高さ５８００ｍｍ
の分離塔に、下部の樹脂支持板より上方１４８０ｍｍの
位置に下部樹脂コレクター、その上方５００ｍｍに上部
樹脂コレクターを水平に内設し、さらに下部樹脂コレク
ターより上方１５０ｍｍの位置の側壁に樹脂抜き出しノ
ズルを開口した。各樹脂コレクター及びノズルの内径は
１００ｍｍであり、設置位置は管の中心からの距離であ
る。また、上部、下部樹脂コレクターは、一本の抜き出
し集合管に５本の枝管を設け、各枝管には内径７ｍｍの
複数の樹脂抜き出し孔を等間隔にあけたものを用いた。EXAMPLES Hereinafter, the present invention will be described in more detail with reference to examples, but the present invention is not limited to these examples unless it exceeds the gist. Example 2100 mm in inner diameter and 5800 mm in height of a straight body shown in FIG.
In the separation tower, the lower resin collector is installed horizontally at 1480 mm above the lower resin support plate, the upper resin collector is installed horizontally at 500 mm above, and the resin extraction nozzle is installed at the side wall at 150 mm above the lower resin collector. Opened. The inner diameter of each resin collector and nozzle is 100 mm, and the installation position is the distance from the center of the tube. As the upper and lower resin collectors, one branch pipe was provided with five branch pipes, and each branch pipe was provided with a plurality of resin extraction holes having an inner diameter of 7 mm at equal intervals.
【００２１】この分離塔に復水脱塩処理のアンモニア形
運転により機能の低下した強酸性陽イオン交換樹脂ダイ
ヤイオン（登録商標）ＰＫ２２８，５３５０リツトル
（Ｈ形での体積）と強塩基性陰イオン交換樹脂ダイヤイ
オンＰＡ３１２，３１５０リットル（ＯＨ形での体積）
との混合樹脂を移送した後、続いて中間樹脂貯槽に貯槽
していた混合樹脂［ダイヤイオン（登録商標）ＰＫ２２
８，５５０リットル（Ｈ形での体積）、ダイヤイオンＰ
Ａ３１２，１２００リットル（ＯＨ形での体積）］を移
送した。次いでこの分離塔の下部集水管より逆洗水をＬ
Ｖ８ｍ／ｈで流入しイオン交換樹脂を逆洗分離後沈静さ
せ、陽イオン交換樹脂層、混合樹脂層、陰イオン交換樹
脂層に成層分離した。In this separation column, a strongly acidic cation exchange resin Diaion (registered trademark) PK228,5350 liters (volume in H form) and a strongly basic anion whose functions have been reduced by the ammonia type operation of condensate and desalination treatment Exchange resin DIAION PA312, 3150 liters (volume in OH form)
After transferring the mixed resin with the mixed resin [Diaion (registered trademark) PK22] stored in the intermediate resin storage tank,
8,550 liters (volume in H form), Diaion P
A3, 1200 liters (volume in OH form)]. Then, the backwash water was removed from the lower collecting pipe of this separation tower by L
After flowing in at a flow rate of 8 m / h, the ion exchange resin was backwashed and separated, then settled, and separated into a cation exchange resin layer, a mixed resin layer and an anion exchange resin layer.
【００２２】次に、分離塔の上部集水管よりＬＶ９ｍ／
ｈで移送水を流入して、上部樹脂コレクターより陰イオ
ン交換樹脂を抜き出し陰イオン交換樹脂再生塔に移送し
た。次いで、上部樹脂コレクターを閉じ、上部集水管よ
り移送水（ＬＶ９ｍ／ｈ）を流入すると共に下部樹脂コ
レクターからもＬＶ２ｍ／ｈで移送水を流入して混合樹
脂層の上層部を樹脂抜き出しノズルより抜き出した。そ
の後ノズルを閉じ、且つ下部樹脂コレクターからの移送
水の流入を停止し、上部集水管より移送水を流入しなが
ら下部樹脂コレクターから混合樹脂層の下層部を抜き出
し、ノズル及び下部樹脂コレクターから抜き出した混合
樹脂層は中間樹脂貯槽に移送し貯槽した。Next, an LV of 9 m / cm.
At h, the transfer water was introduced, an anion exchange resin was extracted from the upper resin collector, and transferred to the anion exchange resin regeneration tower. Next, the upper resin collector is closed, the transfer water (LV 9 m / h) flows from the upper water collecting pipe, and the transfer water also flows from the lower resin collector at LV 2 m / h, and the upper part of the mixed resin layer is drawn out from the resin discharge nozzle. Was. Thereafter, the nozzle was closed, and the flow of the transfer water from the lower resin collector was stopped, and the lower layer of the mixed resin layer was extracted from the lower resin collector while the transfer water was flowing from the upper water collecting pipe, and was then extracted from the nozzle and the lower resin collector. The mixed resin layer was transferred to an intermediate resin storage tank and stored therein.
【００２３】上記の操作により分離塔に残留した陽イオ
ン交換樹脂を十分に混合した後、この陽イオン交換樹脂
を約８リットル採取し、これを内径１００ｍｍ、高さ２
０００ｍｍのアクリル製カラムに充填した。カラムの底
から逆洗水をＬＶ１０ｍ／ｈで３０分間流入して逆洗
し、沈静後の陽イオン交換樹脂層の表層に積層した陰イ
オン交換樹脂を採取してその体積を測定した。次にカラ
ムに残った陽イオン交換樹脂の層高からその体積を算出
し、陽イオン交換樹脂に対する陰イオン交換樹脂の混入
率を求めた。結果を表１に示す。After sufficiently mixing the cation exchange resin remaining in the separation column by the above operation, about 8 liters of the cation exchange resin was collected, and was collected with an inner diameter of 100 mm and a height of 2 mm.
It was packed in a 000 mm acrylic column. Backwash water was introduced from the bottom of the column at an LV of 10 m / h for 30 minutes to backwash, and the anion exchange resin laminated on the surface of the cation exchange resin layer after settling was collected and its volume was measured. Next, the volume of the cation exchange resin remaining in the column was calculated from the layer height, and the mixing ratio of the anion exchange resin to the cation exchange resin was determined. Table 1 shows the results.
【００２４】比較例 実施例の分離塔においてノズルを設け無かった以外は同
じ仕様の分離塔を用いて従来の方法による混合イオン交
換樹脂の分離を行った。イオン交換樹脂の仕様条件及び
逆洗による混合イオン交換樹脂の成層分離条件は、実施
例と同一条件とした。陰イオン交換樹脂の抜き出しは実
施例と同様の操作により上部樹脂コレクターにより行っ
た。次いで、上部集水管より移送水をＬＶ９ｍ／ｈで流
入しながら下部樹脂コレクターより混合樹脂層を抜き出
した。上記の操作後分離塔に残留する陽イオン交換樹脂
を十分に混合した後、この陽イオン交換樹脂を約８リッ
トル採取し、実施例と同様な操作手順により陽イオン交
換樹脂に対する陰イオン交換樹脂の混入率求めた。結果
を表１に示す。Comparative Example A mixed ion exchange resin was separated by a conventional method using a separation tower of the same specifications except that no nozzle was provided in the separation tower of the example. The specification conditions of the ion-exchange resin and the conditions for stratified separation of the mixed ion-exchange resin by backwashing were the same as those in the examples. Extraction of the anion exchange resin was performed by the upper resin collector in the same manner as in the example. Next, the mixed resin layer was extracted from the lower resin collector while the transfer water was introduced at an LV of 9 m / h from the upper collecting pipe. After sufficiently mixing the cation exchange resin remaining in the separation tower after the above operation, about 8 liters of this cation exchange resin were collected, and the cation exchange resin was converted to the cation exchange resin by the same operation procedure as in the example. The mixing ratio was determined. Table 1 shows the results.
【００２５】[0025]
【表１】 表１ 陰イオン交換樹脂体積 陽イオン交換樹脂体積 混入率 実施例 ５ミリリットル ７７６０ミリリットル ０．０６％ 比較例 ６８ミリリットル ７６９０ミリリットル ０．８８％ TABLE 1 anion exchange resin volume cation exchange resin volume mixing ratio Example 5 ml 7760 ml 0.06% Comparative Example 68 ml 7690 ml 0.88%
【００２６】[0026]
【発明の効果】本発明の分離塔を採用すれば、混合イオ
ン交換樹脂から陰・陽イオン交換樹脂を相互分離するに
当たり、陽イオン交換樹脂の表層面に陰イオン交換樹脂
が残留することがないので、純粋な陽イオン交換樹脂と
陰イオン交換樹脂とに分離できる。According to the present invention, when the anion / cation exchange resin is separated from the mixed ion exchange resin, the anion exchange resin does not remain on the surface of the cation exchange resin. Therefore, it can be separated into pure cation exchange resin and anion exchange resin.
【図１】本発明の混合イオン交換樹脂の分離塔の実施態
様を説明するための縦断面概略図である。FIG. 1 is a schematic longitudinal sectional view illustrating an embodiment of a separation tower for a mixed ion exchange resin of the present invention.
【図２】本発明の樹脂抜き出しノズルの実施形態の一例
を示す縦断面概略図である。FIG. 2 is a schematic longitudinal sectional view showing an example of an embodiment of a resin extraction nozzle of the present invention.
【図３】本発明の樹脂抜き出しノズルの実施形態の一例
を示す縦断面概略図である。FIG. 3 is a schematic longitudinal sectional view showing an example of an embodiment of a resin extraction nozzle of the present invention.
【図４】本発明の上部、下部樹脂コレクターの実施形態
の一例を示す縦断面概略図（図４Ａ）、及び平面概略図
（図４Ｂ）である。FIG. 4 is a schematic longitudinal sectional view (FIG. 4A) and a schematic plan view (FIG. 4B) showing an example of an embodiment of the upper and lower resin collectors of the present invention.
【図５】本発明の上部、下部樹脂コレクターの実施形態
の一例を示す縦断面概略図（図５Ａ）、及び平面概略図
（図５Ｂ）である。FIG. 5 is a schematic longitudinal sectional view (FIG. 5A) and a schematic plan view (FIG. 5B) showing an example of an embodiment of the upper and lower resin collectors of the present invention.
１ 分離塔 ２ 混合イオン交換樹脂導入管 ３ 陰イオン交換樹脂層 ４ 陽イオン交換樹脂層 ５ 混合樹脂層 ６ 分離境界面 ７ 上部樹脂コレクター ８ 下部樹脂コレクター ９ 混合樹脂抜き出しノズル １０ 陽イオン交換樹脂抜き出し管 １１ 上部集水管 １２ 下部集水管 １３ 樹脂支持板 １４ 樹脂抜き出し孔 １５ 枝管 DESCRIPTION OF SYMBOLS 1 Separation tower 2 Mixed ion exchange resin introduction pipe 3 Anion exchange resin layer 4 Cation exchange resin layer 5 Mixed resin layer 6 Separation boundary surface 7 Upper resin collector 8 Lower resin collector 9 Mixed resin extraction nozzle 10 Cation exchange resin extraction pipe DESCRIPTION OF SYMBOLS 11 Upper collecting pipe 12 Lower collecting pipe 13 Resin support plate 14 Resin extraction hole 15 Branch pipe
───────────────────────────────────────────────────── フロントページの続き (72)発明者 中 貢 東京都豊島区南大塚３丁目43番11号 日本 錬水株式会社内 (72)発明者 寺山 弘晃 神奈川県横浜市青葉区鴨志田町1000番地 日本錬水株式会社研究所内 (72)発明者 尾崎 隆 神奈川県横浜市青葉区鴨志田町1000番地 日本錬水株式会社研究所内 ──────────────────────────────────────────────────続 き Continued on the front page (72) Inventor Nakatsugu 3-43-11 Minami-Otsuka, Toshima-ku, Tokyo Japan Renishui Co., Ltd. (72) Inventor Hiroaki Terayama 1000 Kamoshida-cho, Aoba-ku, Aoba-ku, Yokohama, Japan Japan (72) Inventor Takashi Ozaki 1000 Kamoshida-cho, Aoba-ku, Yokohama-shi, Kanagawa Japan Refinery Co., Ltd.
Claims (7)
なる混合イオン交換樹脂を逆洗により相互に成層分離す
る分離塔であり、該塔内に成層分離後の陰イオン交換樹
脂層と陽イオン交換樹脂層との算出分離界面付近に、該
算出分離界面を介して上部樹脂コレクターと下部樹脂コ
レクターが内設され、且つ該上部樹脂コレクターと下部
樹脂コレクターの間に樹脂抜き出しノズルが設置されて
いることを特徴とする混合イオン交換樹脂の分離塔。1. A separation column for stratifying and separating a mixed ion exchange resin comprising a cation exchange resin and an anion exchange resin from each other by backwashing. Near the calculated separation interface with the exchange resin layer, an upper resin collector and a lower resin collector are provided inside through the calculated separation interface, and a resin extraction nozzle is provided between the upper resin collector and the lower resin collector. A mixed ion exchange resin separation tower characterized by the above-mentioned.
下端位置が成層分離した陰イオン交換樹脂層と陽イオン
交換樹脂層の算出分離界面或いはやや下方に略位置する
ように設置されていることを特徴とする請求項ｌ記載の
混合イオン交換樹脂の分離塔。2. The resin extraction nozzle is installed such that the lowermost position of the inner surface of the nozzle is substantially located slightly below the calculated separation interface between the anion-exchange resin layer and the cation-exchange resin layer, which are stratified and separated. The separation column for a mixed ion exchange resin according to claim 1, characterized in that:
イオン交換樹脂層と陽イオン交換樹脂層の算出分離界面
から約１００〜５００ｍｍ上位の陰イオン交換樹脂層内
に設置されることを特徴とする請求項１又は２記載の混
合イオン交換樹脂の分離塔。3. The method according to claim 1, wherein the upper resin collector is installed in the anion exchange resin layer approximately 100 to 500 mm higher than the calculated separation interface between the anion exchange resin layer and the cation exchange resin layer that have been separated into layers. The separation column for a mixed ion exchange resin according to claim 1 or 2, wherein:
イオン交換樹脂層と陽イオン交換樹脂層の算出分離界面
から約５０〜３００ｍｍ下位の陽イオン交換樹脂層内に
設置されることを特徴とする請求項１乃至３のいずれか
１項記載の混合イオン交換樹脂の分離塔。4. The lower resin collector is installed in the cation exchange resin layer about 50 to 300 mm below the calculated separation interface between the anion exchange resin layer and the cation exchange resin layer which have been stratified and separated. The separation column for a mixed ion exchange resin according to any one of claims 1 to 3.
クターは、分離塔壁を貫通して設けられ、複数の樹脂抜
き出し穴を有することを特徴とする請求項１，３および
４のいずれか１項記載の混合イオン交換樹脂の分離塔。5. The resin collector according to claim 1, wherein said upper resin collector and said lower resin collector are provided so as to penetrate through a separation tower wall and have a plurality of resin extraction holes. A separation tower for the mixed ion exchange resin according to the above.
たものであることを特徴とする請求項１乃至５のいずれ
か１項記載の混合イオン交換樹脂の分離塔。6. The mixed ion exchange resin separation column according to claim 1, wherein the mixed ion exchange resin is used for desalting.
なる混合イオン交換樹脂を逆洗により相互に成層分離す
る分離塔であり、該塔内に成層分離後の陰イオン交換樹
脂層と陽イオン交換樹脂層との算出分離界面付近に、該
算出分離界面を介して上部樹脂コレクターと下部樹脂コ
レクターが内設され、且つ該上部樹脂コレクターと下部
樹脂コレクターの間に樹脂抜き出しノズルが設置されて
いる混合イオン交換樹脂の分離塔を用いて混合イオン交
換樹脂を分離する方法において、該塔に移送された分離
すべき陽イオン交換樹脂と陰イオン交換樹脂との混合イ
オン交換樹脂に該塔底部に設けた下部集水管より逆洗水
を導入して混合イオン交換樹脂を流動展開させた後、逆
洗水の導入を停止して静置させ、陰イオン交換樹脂層、
混合イオン交換樹脂層および陽イオン交換樹脂層とに成
層分離する第１工程、該塔の頂部に設けた上部集水管よ
り移送水または加圧空気を導入して上部樹脂コレクター
より該陰イオン交換樹脂層を抜き出す第２工程、上部樹
脂コレクターを閉じ、下部樹脂コレクターより移送水を
導入して該混合樹脂層を流動させながら上部集水管から
移送水または加圧空気を導入して、上部下部両樹脂コレ
クターの間に設けた樹脂抜き出しノズルより該混合樹脂
層の上層部分を抜き出す第３工程、下部樹脂コレクター
からの移送水の導入を停止し、更に樹脂抜き出しノズル
を閉じて上部集水管から移送水または加圧空気を導入し
ながら下部樹脂コレクターより該混合樹脂の下層部分を
取り出す第４工程を順次行うことを特徴とする混合イオ
ン交換樹脂の分離方法。7. A separation column in which a mixed ion exchange resin composed of a cation exchange resin and an anion exchange resin is layered and separated from each other by backwashing. Near the calculated separation interface with the exchange resin layer, an upper resin collector and a lower resin collector are provided inside through the calculated separation interface, and a resin extraction nozzle is provided between the upper resin collector and the lower resin collector. In the method of separating a mixed ion exchange resin using a separation column of the mixed ion exchange resin, the mixed ion exchange resin of the cation exchange resin and the anion exchange resin to be separated transferred to the column is provided at the bottom of the column. After introducing the backwash water from the lower collecting pipe to flow and develop the mixed ion exchange resin, the introduction of the backwash water was stopped and allowed to stand, and the anion exchange resin layer was removed.
A first step of forming a mixed ion-exchange resin layer and a cation-exchange resin layer in a stratified manner; introducing transfer water or pressurized air from an upper water collecting pipe provided at the top of the column; In the second step of extracting the layer, the upper resin collector is closed, transfer water is introduced from the lower resin collector, and transfer water or pressurized air is introduced from the upper collecting pipe while flowing the mixed resin layer. The third step of extracting the upper layer portion of the mixed resin layer from the resin extraction nozzle provided between the collectors, stopping the introduction of transfer water from the lower resin collector, further closing the resin extraction nozzle, and transferring the transfer water or water from the upper collecting pipe. Separating the mixed ion-exchange resin by sequentially performing a fourth step of removing the lower layer portion of the mixed resin from the lower resin collector while introducing pressurized air. Law.
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|---|---|---|---|
| JP2000171527A JP4346214B2 (en) | 1999-06-09 | 2000-06-08 | Separation method of mixed ion exchange resin |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11-162304 | 1999-06-09 | ||
| JP16230499 | 1999-06-09 | ||
| JP2000171527A JP4346214B2 (en) | 1999-06-09 | 2000-06-08 | Separation method of mixed ion exchange resin |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2009113154A Division JP5075159B2 (en) | 1999-06-09 | 2009-05-08 | Separation tower for mixed ion exchange resin |
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| Publication Number | Publication Date |
|---|---|
| JP2001054738A true JP2001054738A (en) | 2001-02-27 |
| JP4346214B2 JP4346214B2 (en) | 2009-10-21 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2018192443A (en) * | 2017-05-19 | 2018-12-06 | オルガノ株式会社 | Regeneration method of anion resin and cation resin, and condensate demineralizer |
| CN109939748A (en) * | 2018-11-26 | 2019-06-28 | 西安热工研究院有限公司 | A kind of mixture iron exchange resin separator |
-
2000
- 2000-06-08 JP JP2000171527A patent/JP4346214B2/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2018192443A (en) * | 2017-05-19 | 2018-12-06 | オルガノ株式会社 | Regeneration method of anion resin and cation resin, and condensate demineralizer |
| CN109939748A (en) * | 2018-11-26 | 2019-06-28 | 西安热工研究院有限公司 | A kind of mixture iron exchange resin separator |
| CN109939748B (en) * | 2018-11-26 | 2024-05-28 | 西安热工研究院有限公司 | Mixed ion exchange resin separation device |
Also Published As
| Publication number | Publication date |
|---|---|
| JP4346214B2 (en) | 2009-10-21 |
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