JPH0757308B2 - Electrodialysis tank - Google Patents
Electrodialysis tankInfo
- Publication number
- JPH0757308B2 JPH0757308B2 JP62310869A JP31086987A JPH0757308B2 JP H0757308 B2 JPH0757308 B2 JP H0757308B2 JP 62310869 A JP62310869 A JP 62310869A JP 31086987 A JP31086987 A JP 31086987A JP H0757308 B2 JPH0757308 B2 JP H0757308B2
- Authority
- JP
- Japan
- Prior art keywords
- cation
- anion
- membrane
- deionization chamber
- chamber
- 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 - Fee Related
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
- B01D61/44—Ion-selective electrodialysis
- B01D61/46—Apparatus therefor
- B01D61/48—Apparatus therefor having one or more compartments filled with ion-exchange material, e.g. electrodeionisation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
- B01D61/44—Ion-selective electrodialysis
- B01D61/445—Ion-selective electrodialysis with bipolar membranes; Water splitting
Landscapes
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Health & Medical Sciences (AREA)
- Urology & Nephrology (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Description
【発明の詳細な説明】 〔産業上の利用分野〕 本発明は、イオン交換膜とイオン交換樹脂とを組合わせ
て使用した電気透析槽に関するものである。TECHNICAL FIELD The present invention relates to an electrodialysis tank using a combination of an ion exchange membrane and an ion exchange resin.
〔従来の技術及び発明が解決しようとする問題点〕 従来、純水製造方法としては、強酸性カチオン樹脂と強
塩基性及び弱塩基性アニオン交換樹脂を同一イオン交換
塔内に存在させて行なう混床式イオン交換装置、または
単一種のイオン交換樹脂を用いて処理する単床式イオン
交換装置を使用する方法等がある。[Problems to be Solved by Conventional Techniques and Inventions] Conventionally, as a pure water producing method, a mixture of a strongly acidic cation resin and a strongly basic or weakly basic anion exchange resin is used in the same ion exchange column. There is a method of using a bed type ion exchange apparatus or a single bed type ion exchange apparatus in which treatment is performed using a single type of ion exchange resin.
しかし、これらの装置においてはイオン交換樹脂の再生
工程が必要であり、その再生工程は、逆洗，通薬，押
出，洗浄等の操作を行わねばならなかつた。再生工程に
於いて各操作が必要時間を越えると再生剤の損失，洗浄
液の損失をきたし、各操作が必要時間に満たない場合に
は、再生不完全，押出不完全，洗浄不完全等をきたす。
また、各操作は煩雑であり、誤操作を起こすと再生操作
からくり返し始めなければならないといった問題もあっ
た。However, these apparatuses require a step of regenerating the ion exchange resin, and the regenerating step has to be carried out by operations such as backwashing, chemical passing, extrusion and washing. If each operation exceeds the required time in the regeneration process, loss of regenerant and cleaning liquid will occur, and if each operation is less than the required time, incomplete regeneration, incomplete extrusion, incomplete cleaning, etc. will occur. .
In addition, each operation is complicated, and if an erroneous operation occurs, there is a problem that the reproduction operation must be repeated.
近年、この煩雑な操作を解消するために、イオン交換装
置の自動再生機構等が提案されているが、設備が高価で
ある。In recent years, in order to eliminate this complicated operation, an automatic regeneration mechanism of an ion exchange device has been proposed, but the equipment is expensive.
本発明者らは、従来のイオン交換樹脂の再生工程を解消
すると共に高純度の純水を多量に製造する電気透析槽の
開発に成功し、本発明を提案するに至った。The present inventors have succeeded in developing an electrodialysis tank which eliminates the conventional ion exchange resin regeneration step and produces a large amount of high-purity pure water, and has proposed the present invention.
即ち、本発明は、バイポーラー膜，陽イオン交換膜，陰
イオン交換膜及びバイポーラー膜の順に配列され、該バ
イポーラー膜と該陽イオン交換膜とで区画される陽イオ
ン脱塩室には陽イオン交換樹脂が、また、該陰イオン交
換膜と該バイポーラー膜とで区画される陰イオン脱塩室
には陰イオン交換樹脂が夫々充填され、また、該陽イオ
ン交換膜と該陰イオン交換膜とで区画された室が濃縮室
である構造のユニツトが、陰極と陽極との間に１以上配
列されてなり、該陽イオン脱塩室と該陰イオン脱塩室の
いずれか一方には被脱塩液の供給管が、他方には被脱塩
液の排水管が夫々接続されており、更に該陽イオン脱塩
室と該陰イオン脱塩室とは通液管により接続されてなる
ことを特徴とする電気透析槽である。That is, according to the present invention, a bipolar membrane, a cation exchange membrane, an anion exchange membrane and a bipolar membrane are arranged in this order, and a cation deionization chamber defined by the bipolar membrane and the cation exchange membrane is provided. A cation exchange resin and an anion deionization chamber defined by the anion exchange membrane and the bipolar membrane are filled with anion exchange resin, and the cation exchange membrane and the anion are filled. One or more units having a structure in which the chamber partitioned by the exchange membrane is a concentrating chamber are arranged between the cathode and the anode, and the unit is provided in either the cation deionization chamber or the anion deionization chamber. Is connected to a supply pipe for the desalinated liquid, and the drain pipe for the desalted liquid is connected to the other, and the cation deionization chamber and the anion deionization chamber are connected by a liquid passage pipe. It is an electrodialysis tank characterized in that
また、本発明は、陽イオン交換膜，バイポーラー膜及び
陰イオン交換膜の順に配列され、該陽イオン交換膜と該
バイポーラー膜とで区画される陽イオン脱塩室には陽イ
オン交換樹脂が、また該バイポーラー膜と該インイオン
交換膜とで区画される陰イオン脱塩室には陰イオン交換
樹脂が夫々充填された構造のユニツトが、陰極と陽極と
の間に１以上配列されてなり、該陽イオン脱塩室と該陰
イオン脱塩室のいずれか一方には被脱塩液の供給管が、
他方には被脱塩液の排出管が夫々接続されており、更に
該陽イオン脱塩室と該陰イオン脱塩室とは通液管により
接続されてなることを特徴とする電気透析槽である。Further, the present invention provides a cation exchange membrane, a bipolar membrane and an anion exchange membrane, which are arranged in this order, and a cation exchange resin is provided in a cation deionization chamber defined by the cation exchange membrane and the bipolar membrane. However, one or more units each having a structure in which an anion exchange resin is filled in the anion deionization chamber defined by the bipolar membrane and the inion exchange membrane are arranged between the cathode and the anode. And a supply pipe for a liquid to be desalinated is provided in either one of the cation deionization chamber and the anion deionization chamber,
A discharge pipe for the desalted liquid is connected to the other, respectively, and the cation deionization chamber and the anion deionization chamber are connected by a liquid passage pipe. is there.
以下、本発明を図面に従って説明する。The present invention will be described below with reference to the drawings.
第１図は、本発明の電気透析槽を示す概略図である。第
１図に於いて、バイポーラー膜6,陽イオン交換膜7,陰イ
オン交換膜８及びバイポーラー膜６の順に各膜が配列さ
れて１ユニツトが構成されている。バイポーラー膜６と
陽イオン交換膜７とで区画される陽イオン脱塩室２には
陽イオン交換樹脂９が充填され、また、陰イオン交換膜
８とバイポーラー膜６とで区画される陰イオン脱塩室３
には陰イオン交換樹脂10が充填されている。そして、陽
イオン交換膜７と陰イオン交換膜とで区画されることに
よって濃縮室４が形成されている。上記した構造のユニ
ツトが陽極及び陰極の間に、陽極側に陽イオン交換膜が
くるように１以上配列されている。第１図には、上記の
ユニツトが３個配置された例を示したが、一般には、１
〜100個であることが脱塩効率の点から好ましい。上記
した構造のユニツトを複数個配列する場合、隣り合うユ
ニツトのバイポーラー膜同士は、互いに接していても良
く、また離れていても良い。しかし、電気透析を行なう
場合の電圧を低く抑えるためには、上記のバイポーラー
膜同士は、離れているよりは接している方が好ましく、
さらには、第１図に示したように１枚のバイポーラー膜
に置き換えられている方が好ましい。FIG. 1 is a schematic diagram showing the electrodialysis tank of the present invention. In FIG. 1, the bipolar membrane 6, the cation exchange membrane 7, the anion exchange membrane 8 and the bipolar membrane 6 are arranged in this order to form one unit. The cation deionization chamber 2 defined by the bipolar membrane 6 and the cation exchange membrane 7 is filled with a cation exchange resin 9 and is also defined by the anion exchange membrane 8 and the bipolar membrane 6. Ion desalination room 3
Is filled with anion exchange resin 10. The concentrating chamber 4 is formed by being partitioned by the cation exchange membrane 7 and the anion exchange membrane. One or more units having the above structure are arranged between the anode and the cathode so that the cation exchange membrane is on the anode side. FIG. 1 shows an example in which the above three units are arranged.
From the viewpoint of desalination efficiency, it is preferably from 100 to 100. When a plurality of units having the above-described structure are arranged, the bipolar films of the adjacent units may be in contact with each other or may be separated from each other. However, in order to reduce the voltage when performing electrodialysis, it is preferable that the above bipolar membranes are in contact with each other rather than separated from each other,
Furthermore, as shown in FIG. 1, it is preferable to replace with one bipolar film.
さらに、第１図では、被脱塩液の供給管12及び排出管13
は、夫々陽イオン脱塩室２及び陰イオン脱塩室３に接続
されているが、被脱塩液の供給管と排出管は、いずれか
一方が、陽イオン脱塩室に、他方が陰イオン脱塩室に設
けられておれば良い。さらに、陽イオン脱塩室と陰イオ
ン脱塩室とは通液管11により接続されている。通液管11
の入口及び出口は、第１図に示したように陽イオン脱塩
室と陰イオン脱塩室に充填された陽イオン交換樹脂及び
陰イオン交換樹脂をはさんで被脱塩液の供給管及び排出
管の位置と反対側になるように設けることが好ましい。
そして、濃縮室４には濃縮液の供給管14と排出管15が接
続されている。Further, in FIG. 1, a supply pipe 12 and a discharge pipe 13 for the desalination liquid
Are connected to the cation deionization chamber 2 and the anion deionization chamber 3, respectively. One of the supply pipe and the discharge pipe of the liquid to be desalinated is the cation deionization chamber and the other is the anion deionization chamber. It should be provided in the ion deionization chamber. Further, the cation deionization chamber and the anion deionization chamber are connected by a liquid passage pipe 11. Liquid passage 11
As shown in FIG. 1, the inlet and outlet of the cation exchange resin and the anion exchange resin filled in the cation deionization chamber and the anion exchange resin are sandwiched between the supply pipe and It is preferably provided on the side opposite to the position of the discharge pipe.
A supply pipe 14 and a discharge pipe 15 for the concentrated liquid are connected to the concentration chamber 4.
本発明の電気透析槽に使用される陽イオン交換膜，陰イ
オン交換膜，バイポーラー膜及び陽，陰イオン交換樹脂
は、従来公知の膜及び樹脂が適宜採用することができる
が、それぞれ塩の分離，塩の吸着，加水分解と有効な膜
及び樹脂を選択すれば良い。As the cation exchange membrane, the anion exchange membrane, the bipolar membrane and the cation and anion exchange resin used in the electrodialysis tank of the present invention, conventionally known membranes and resins can be appropriately adopted. Separation, salt adsorption, hydrolysis and effective membrane and resin may be selected.
例えば、陽イオン交換膜としては陽イオンのみを選択的
に透過せしめるもので、スルホン酸基，カルボン酸基を
有する公知の膜が使用できる。陰イオン交換膜として
は、陰イオンを選択的に透過せしめるものであれば従来
のいかなる膜でもよい。また、バイポーラー膜として
は、陰イオン交換層と陽イオン交換層とを有し、加水分
解効率が高いものであれば良い。陽，陰イオン交換樹脂
としては従来公知の樹脂が使用できる。For example, as the cation exchange membrane, only a cation can be selectively permeated, and a known membrane having a sulfonic acid group or a carboxylic acid group can be used. As the anion exchange membrane, any conventional membrane may be used as long as it selectively allows the passage of anions. Further, the bipolar membrane may be one having an anion exchange layer and a cation exchange layer and having a high hydrolysis efficiency. Conventionally known resins can be used as the cation and anion exchange resins.
本発明の電気透析槽による被脱塩液の脱塩過程を第１図
に従って説明すると次のとおりである。被脱塩液は電気
透析槽の陽イオン脱塩室２に供給される。被脱塩液の陽
イオンは選択的に陽イオン交換膜７を透過するか、陽イ
オン交換樹脂９に吸着される。そして、陽イオン交換樹
脂９に吸着された陽イオンは、バイポーラー膜６から発
生するプロトン（H+）により脱着され、陽イオン交換膜
７を透過する。次いで、陽イオンを排除した被脱塩液は
通液管11を通り、陰イオン脱塩室３に供給される。被脱
塩液の陰イオンは選択的に陰イオン交換膜８を透過する
か、陰イオン交換樹脂10に吸着される。しかし、陰イオ
ン交換樹脂に吸着された陰イオンは、バイポーラー膜６
から発生する水酸イオン（OH-）により脱着され、陰イ
オン交換膜８を透過し排除される。陽，陰イオンを排除
した被脱塩液は高純度の純水として得られる。一方、排
除された陽，陰イオンは濃縮室４で中性塩として排出さ
れる。The desalting process of the liquid to be desalinated by the electrodialysis tank of the present invention will be described below with reference to FIG. The liquid to be desalinated is supplied to the cationic deionization chamber 2 of the electrodialysis tank. The cations of the liquid to be desalted selectively pass through the cation exchange membrane 7 or are adsorbed by the cation exchange resin 9. Then, the cations adsorbed on the cation exchange resin 9 are desorbed by the protons (H + ) generated from the bipolar membrane 6 and permeate the cation exchange membrane 7. Next, the deionized liquid from which the cations have been removed passes through the liquid passage pipe 11 and is supplied to the anion deionization chamber 3. Anions of the liquid to be desalted selectively pass through the anion exchange membrane 8 or are adsorbed on the anion exchange resin 10. However, the anions adsorbed on the anion exchange resin are not
It is desorbed by the hydroxide ion (OH − ) generated from and is permeated through the anion exchange membrane 8 and eliminated. The solution to be desalinated from which cations and anions have been removed is obtained as pure water of high purity. On the other hand, the removed cations and anions are discharged as neutral salts in the concentrating chamber 4.
この工程で高純度の純水を効率的に得るためには、電気
透析を実施する条件を適切に選択すれば良い。In order to efficiently obtain high-purity pure water in this step, the conditions for carrying out electrodialysis may be appropriately selected.
例えば、被脱塩液の供給速度は、0.01〜20cm/sec、好ま
しくは0.05〜2cm/secであり、濃縮室に供給する希薄塩
の濃度は0.01N以上で、供給速度は0.1〜20cm/secであ
り、好ましくは0.5〜6cm/secである。電流密度は0.01〜
30A/dm2であり、好ましくは0.1〜5A/dm2が適用される。
温度は５〜50℃が好ましい。For example, the supply rate of the solution to be desalinated is 0.01 to 20 cm / sec, preferably 0.05 to 2 cm / sec, the concentration of the dilute salt supplied to the concentration chamber is 0.01 N or more, and the supply rate is 0.1 to 20 cm / sec. And preferably 0.5 to 6 cm / sec. Current density is 0.01 ~
30 A / dm 2 , preferably 0.1 to 5 A / dm 2 is applied.
The temperature is preferably 5 to 50 ° C.
また、有機物を含む水を処理して純水を製造する場合は
本発明の電気透析槽の前段に活性炭を充填した処理装置
を設けると良い。Further, in the case of treating water containing an organic substance to produce pure water, it is preferable to provide a treatment device filled with activated carbon in the preceding stage of the electrodialysis tank of the present invention.
次に、本発明の電気透析槽の他の一例を第２図に示し
た。第２図に於いて、陽イオン交換膜7,バイポーラー膜
６及び陰イオン交換膜８の順に各膜が配列されて１ユニ
ツトが構成されている。そして、陽イオン交換膜７とバ
イポーラー膜６とで区画される陽イオン脱塩室２には陽
イオン交換樹脂９が充填され、また、バイポーラー膜６
と陰イオン交換膜８とで区画される陰イオン脱塩室３に
は陰イオン交換樹脂10が充填されている。上記した構造
のユニツトが、陽極と陰極との間に、陽極側に陰イオン
交換膜がくるように１以上配列されている。第２図に
は、上記のユニツトが４個配列された例を示した。上記
した構造のユニツトを複数個配列する場合、隣り合うユ
ニツトの陽イオン交換膜及び陰イオン交換膜を適当な間
隔をあけて配置し、濃縮室４を形成させることが好まし
い。被脱塩液の供給管及び排出管、並びに陽イオン脱塩
室２と陰イオン脱塩室３とを連結する通液管11は、既に
前に説明した電気透析槽と同様である。Next, another example of the electrodialysis tank of the present invention is shown in FIG. In FIG. 2, the cation exchange membrane 7, the bipolar membrane 6 and the anion exchange membrane 8 are arranged in this order to form one unit. The cation deionization chamber 2 defined by the cation exchange membrane 7 and the bipolar membrane 6 is filled with the cation exchange resin 9, and the bipolar membrane 6 is used.
The anion deionization chamber 3 partitioned by the anion exchange membrane 8 is filled with anion exchange resin 10. One or more units having the above-described structure are arranged between the anode and the cathode so that the anion exchange membrane is located on the anode side. FIG. 2 shows an example in which four of the above units are arranged. When a plurality of units having the above-mentioned structure are arranged, it is preferable to form the concentrating chamber 4 by arranging the cation exchange membrane and the anion exchange membrane of the adjacent units with an appropriate interval. The supply pipe and the discharge pipe of the liquid to be desalinated, and the liquid passage pipe 11 connecting the cation deionization chamber 2 and the anion deionization chamber 3 are the same as those of the electrodialysis tank described above.
イオン交換膜及びイオン交換樹脂の種類も、既述のもの
が何ら制限なく採用される。As the types of the ion exchange membrane and the ion exchange resin, those already described can be adopted without any limitation.
尚、上記のユニツトと陽極及び陰極の各電極室５との間
に、第２図に示すように緩衝室16を夫々設け、これら２
つの緩衝室16を連結して夫々の緩衝室に蓄積する陽イオ
ン及び陰イオンを中性塩として排出させることもでき
る。A buffer chamber 16 is provided between the unit and each of the anode and cathode electrode chambers 5 as shown in FIG.
It is also possible to connect the two buffer chambers 16 and discharge the cations and anions accumulated in the respective buffer chambers as neutral salts.
上記のように、本発明によれば、高純度の純水を多量に
得ることができる。また、イオン交換樹脂の再生が不要
であるため、長期にわたって連続して安定に電気透析槽
の運転をすることができる。As described above, according to the present invention, a large amount of high-purity pure water can be obtained. Further, since it is not necessary to regenerate the ion exchange resin, the electrodialysis tank can be operated continuously and stably for a long period of time.
〔実施例〕 以下に本発明を更に具体的に示すために実施例を示す
が、本発明は上記説明及び下記の実施例によって何ら限
定されるものではない。[Examples] Examples are shown below to more specifically illustrate the present invention, but the present invention is not limited to the above description and the following examples.
実施例１ 工業用水を被脱塩液として第１図に示した電気透析槽で
ユニツト数20のものを用いて処理した。被脱塩液の分析
値は、第１表に示すとおりであった。電気透析槽として
は、ネオセプタCM及びネオセプタAM（それぞれ徳山曹達
（株）製の強酸性陽イオン交換膜と強塩基性陰イオン交
換膜）とバイポーラーBPM（徳山曹達（株）製，強酸性
陽イオン交換基と強塩基性陰イオン交換基を有したバイ
ポーラー膜）により、陽イオン脱塩室，陰イオン脱塩
室，濃縮室とに区画し、陽イオン脱塩室にはアンバーラ
イト（登録商標）IR−120（強酸性カチオン樹脂）500g
と陰イオン脱塩室にはアンバーライト（登録商標）IRA
−400（強塩基性アニオン交換樹脂）500gを充填した電
気透析槽（徳山曹達（株）製，有効膜面積2dm2）を使用
した。Example 1 Industrial water was used as a desalination solution in the electrodialysis tank shown in FIG. 1 using a unit having a unit number of 20. The analytical values of the desalinated liquid were as shown in Table 1. As electrodialysis tanks, Neosepta CM and Neosepta AM (strong acid cation exchange membrane and strong basic anion exchange membrane manufactured by Tokuyama Soda Co., Ltd.) and bipolar BPM (Tokuyama Soda Co., Ltd., strong acid cation exchange membrane, respectively) It is divided into a cation desalting chamber, an anion desalting chamber and a concentrating chamber by a bipolar membrane having an ion exchange group and a strongly basic anion exchange group, and Amberlite (registered in the cation desalination chamber) Trademark) IR-120 (strongly acidic cationic resin) 500g
And Amberlite® IRA in the anion desalination chamber
An electrodialysis tank (manufactured by Tokuyama Soda Co., Ltd., effective membrane area 2 dm 2 ) filled with 500 g of −400 (strongly basic anion exchange resin) was used.
電気透析槽は、温度27℃，平均電流密度1A/dm2,被脱塩
液供給速度0.5cm/sec,濃縮液に0.1Nの食塩水溶液を供給
速度2cm/secで供給し、２カ月連続して運転した。The electrodialysis tank was operated at a temperature of 27 ° C, an average current density of 1 A / dm 2 , a desalination solution supply rate of 0.5 cm / sec, and a 0.1N saline solution as a concentrate solution at a supply rate of 2 cm / sec for 2 consecutive months. I drove.
その結果、電気比抵抗が1.0×107Ωcm以上の純水が得ら
れた。As a result, pure water having an electric resistivity of 1.0 × 10 7 Ωcm or more was obtained.
また、電槽内の陽イオン交換樹脂と陰イオン交換樹脂を
取り出し、ドナン塩の濃度を測定した。Further, the cation exchange resin and the anion exchange resin in the battery case were taken out, and the concentration of the Donan salt was measured.
その結果、陽イオン交換樹脂からはCa2+,Mg2+,Na+,K+等
が約2ppm検出され、陰イオン交換樹脂からは▲SO2- 4▼,
Cl-,▲NO- 3▼等が約3ppm検出された。この分析結果よ
り、イオン交換樹脂はそのほとんどがＨ型又はOH型であ
り、再生処理を行なう必要はなかった。As a result, Ca 2+ from the cation exchange resin, Mg 2+, Na +, K + and the like are approximately 2ppm detected, from the anion exchange resin ▲ SO 2- 4 ▼,
Cl -, ▲ NO - 3 ▼ like is about 3ppm detected. From the results of this analysis, most of the ion exchange resins were H type or OH type, and it was not necessary to regenerate them.
実施例２ 第２図に示した電気透析槽でユニツト数20のものを使用
した他は実施例１と同様にして被脱塩液の処理を２カ月
連続して行なった。その結果、電気抵抗が1.0×107Ωcm
以上の純水が得られ、また実施例１と同様に陽・陰イオ
ン交換樹脂のドナン塩の濃度を調べたが、実施例１とほ
ぼ同じ分析値であった。この結果よりイオン交換樹脂は
ほとんどがＨ型又はOH型であり、イオン交換樹脂の再生
処理を行なう必要はなかった。 Example 2 The desalination solution was continuously treated for 2 months in the same manner as in Example 1 except that the electrodialysis tank shown in FIG. 2 having a unit number of 20 was used. As a result, the electric resistance is 1.0 × 10 7 Ωcm.
The above pure water was obtained, and the concentration of the Donan salt of the cation / anion exchange resin was examined in the same manner as in Example 1, but the analytical values were almost the same as in Example 1. From these results, most of the ion exchange resins were H type or OH type, and it was not necessary to regenerate the ion exchange resin.
【図面の簡単な説明】 第１図及び第２図は本発明の電気透析槽の概略図であ
る。図中、１は電気透析槽,2は陽イオン脱塩室,3は陰イ
オン脱塩室,4は濃縮室,5は電極室,6はバイポーラー膜,7
は陽イオン交換膜,8は陰イオン交換膜,9は陽イオン交換
樹脂,10は陰イオン交換樹脂,11は通液管,12は被脱塩液
の供給管,13は被脱塩液の排出管,14は濃縮液の供給管,1
5は濃縮液の排出管,15は緩衝室,17は緩衝室液の給排管
を夫々示す。BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 and FIG. 2 are schematic views of an electrodialysis tank of the present invention. In the figure, 1 is an electrodialysis tank, 2 is a cation deionization chamber, 3 is an anion deionization chamber, 4 is a concentration chamber, 5 is an electrode chamber, 6 is a bipolar membrane, 7
Is a cation exchange membrane, 8 is an anion exchange membrane, 9 is a cation exchange resin, 10 is an anion exchange resin, 11 is a liquid passage pipe, 12 is a supply pipe for the desalinated liquid, and 13 is a desalination liquid. Discharge pipe, 14 is concentrated liquid supply pipe, 1
Reference numeral 5 is a concentrated liquid discharge pipe, 15 is a buffer chamber, and 17 is a buffer chamber liquid supply / discharge pipe.
Claims (2)
ン交換膜及びバイポーラー膜の順に配列され、該バイポ
ーラー膜と該陽イオン交換膜とで区画される陽イオン脱
塩室には陽イオン交換樹脂が、また、該陰イオン交換膜
と該バイポーラー膜とで区画される陰イオン脱塩室には
陰イオン交換樹脂が夫々充填され、また、該陽イオン交
換膜と該陰イオン交換膜とで区画された室が濃縮室であ
る構造のユニツトが、陰極と陽極との間に１以上配列さ
れてなり、該陽イオン脱塩室と該陰イオン脱塩室のいず
れか一方には被脱塩液の供給管が、他方には被脱塩液の
排水管が夫々接続されており、更に該陽イオン脱塩室と
該陰イオン脱塩室とは通液管により接続されてなること
を特徴とする電気透析槽。1. A cation deionization chamber, which comprises a bipolar membrane, a cation exchange membrane, an anion exchange membrane and a bipolar membrane, which are arranged in this order, and which is partitioned by the bipolar membrane and the cation exchange membrane. Anion exchange resin is filled in the anion deionization chamber defined by the anion exchange membrane and the bipolar membrane, and the cation exchange membrane and the anion exchange resin are filled. One or more units each having a structure in which the chamber partitioned by the membrane is a concentrating chamber are arranged between the cathode and the anode, and one of the cation deionization chamber and the anion deionization chamber is provided. A supply pipe for the liquid to be desalted is connected to a drain pipe for the liquid to be desalted, and the drainage pipe for the liquid to be desalted is connected to each other, and the cation deionization chamber and the anion deionization chamber are connected by a liquid passage pipe. An electrodialysis tank characterized in that
オン交換膜の順に配列され、該陽イオン交換膜と該バイ
ポーラー膜とで区画される陽イオン脱塩室には陽イオン
交換樹脂が、また該バイポーラー膜と該インイオン交換
膜とで区画される陰イオン脱塩室には陰イオン交換樹脂
が夫々充填された構造のユニツトが、陰極と陽極との間
に１以上配列されてなり、該陽イオン脱塩室と該陰イオ
ン脱塩室のいずれか一方には被脱塩液の供給管が、他方
には被脱塩液の排出管が夫々接続されており、更に該陽
イオン脱塩室と該陰イオン脱塩室とは通液管により接続
されてなることを特徴とする電気透析槽。2. A cation exchange membrane, a bipolar membrane and an anion exchange membrane are arranged in this order, and a cation exchange resin is placed in a cation deionization chamber defined by the cation exchange membrane and the bipolar membrane. Further, one or more units each having a structure in which an anion exchange resin is filled in the anion deionization chamber defined by the bipolar membrane and the inion exchange membrane are arranged between the cathode and the anode. A supply pipe for the desalination liquid is connected to one of the cation deionization chamber and the anion deionization chamber, and a discharge pipe for the desalination liquid is connected to the other, respectively. An electrodialysis tank characterized in that the ion deionization chamber and the anion deionization chamber are connected by a liquid passage pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62310869A JPH0757308B2 (en) | 1987-12-10 | 1987-12-10 | Electrodialysis tank |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62310869A JPH0757308B2 (en) | 1987-12-10 | 1987-12-10 | Electrodialysis tank |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH01151911A JPH01151911A (en) | 1989-06-14 |
| JPH0757308B2 true JPH0757308B2 (en) | 1995-06-21 |
Family
ID=18010368
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62310869A Expired - Fee Related JPH0757308B2 (en) | 1987-12-10 | 1987-12-10 | Electrodialysis tank |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0757308B2 (en) |
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| JP6042234B2 (en) * | 2013-03-01 | 2016-12-14 | オルガノ株式会社 | Desalination method and desalting apparatus |
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Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5543808B2 (en) | 2010-01-25 | 2014-07-09 | 株式会社ブリヂストン | Photopolymerizable composition and functional panel using the same |
-
1987
- 1987-12-10 JP JP62310869A patent/JPH0757308B2/en not_active Expired - Fee Related
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5543808B2 (en) | 2010-01-25 | 2014-07-09 | 株式会社ブリヂストン | Photopolymerizable composition and functional panel using the same |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2012236171A (en) * | 2011-05-13 | 2012-12-06 | Panasonic Corp | Water softener |
| JP2012236172A (en) * | 2011-05-13 | 2012-12-06 | Panasonic Corp | Regenerative water softening device |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH01151911A (en) | 1989-06-14 |
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