JP2003326271A - Electric regenerative demineralizer - Google Patents
Electric regenerative demineralizerInfo
- Publication number
- JP2003326271A JP2003326271A JP2002136604A JP2002136604A JP2003326271A JP 2003326271 A JP2003326271 A JP 2003326271A JP 2002136604 A JP2002136604 A JP 2002136604A JP 2002136604 A JP2002136604 A JP 2002136604A JP 2003326271 A JP2003326271 A JP 2003326271A
- Authority
- JP
- Japan
- Prior art keywords
- chamber
- desalting
- exchanger
- desalination
- cathode
- 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
- 230000001172 regenerating effect Effects 0.000 title claims abstract description 23
- 238000011033 desalting Methods 0.000 claims abstract description 137
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 115
- 150000002500 ions Chemical class 0.000 claims abstract description 57
- 239000012528 membrane Substances 0.000 claims abstract description 45
- 239000003011 anion exchange membrane Substances 0.000 claims abstract description 31
- 238000005341 cation exchange Methods 0.000 claims abstract description 30
- 238000010612 desalination reaction Methods 0.000 claims description 70
- 150000001450 anions Chemical class 0.000 claims description 60
- 150000001768 cations Chemical class 0.000 claims description 45
- 238000002242 deionisation method Methods 0.000 claims description 17
- 230000008929 regeneration Effects 0.000 claims description 14
- 238000011069 regeneration method Methods 0.000 claims description 14
- 238000005342 ion exchange Methods 0.000 claims description 13
- 125000006850 spacer group Chemical group 0.000 claims description 7
- 238000000034 method Methods 0.000 claims description 6
- 239000000835 fiber Substances 0.000 claims description 5
- 150000003839 salts Chemical class 0.000 claims description 4
- 238000010559 graft polymerization reaction Methods 0.000 claims description 3
- 239000004745 nonwoven fabric Substances 0.000 claims description 3
- 230000005855 radiation Effects 0.000 claims description 2
- 239000002759 woven fabric Substances 0.000 claims description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 12
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 10
- 239000012466 permeate Substances 0.000 description 9
- 239000003014 ion exchange membrane Substances 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 6
- 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 description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 description 5
- 239000001569 carbon dioxide Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 239000003456 ion exchange resin Substances 0.000 description 5
- 229920003303 ion-exchange polymer Polymers 0.000 description 5
- 239000000377 silicon dioxide Substances 0.000 description 5
- 239000002253 acid Substances 0.000 description 4
- 239000003513 alkali Substances 0.000 description 4
- 238000005349 anion exchange Methods 0.000 description 3
- 230000002328 demineralizing effect Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 238000005115 demineralization Methods 0.000 description 2
- 230000003301 hydrolyzing effect Effects 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 102100029777 Eukaryotic translation initiation factor 3 subunit M Human genes 0.000 description 1
- 101001012700 Homo sapiens Eukaryotic translation initiation factor 3 subunit M Proteins 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、電気再生式脱塩装
置に係り、特に、１台の電気再生式脱塩装置で、外部に
異なった２種類の純度の純水を供給することができる電
気再生式脱塩装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an electric regenerative desalination apparatus, and in particular, one electric regenerative desalination apparatus can supply two kinds of pure water having different purities to the outside. The present invention relates to an electric regeneration type desalination device.
【０００２】[0002]
【従来の技術】従来の純水製造方法としては、イオン交
換樹脂を充填した容器に脱塩室入口水を通過させ、脱塩
室入口水中のイオンをＨ+、ＯＨ-イオンに、交換するこ
とにより純水を製造するイオン交換法が知られている。
しかし、このイオン交換法では、イオン交換樹脂の交換
能力が飽和すると、イオン交換樹脂の種類に応じて酸、
アルカリを用いてイオン交換能力の再生をする必要があ
る。イオン交換樹脂の再生操作は、煩雑で、多量の酸、
アルカりの貯蔵、取り扱い及び廃棄に細心の注意が必要
であると共に設備が大きくなる、という問題を有してい
る。それに対し、近年、電気によってイオン交換体を再
生し、連続的に純水を製造する電気再生式脱塩装置が開
発された。これは、図３に示すように、脱塩室入口水１
０中のイオン分を装置の両端に印可した直流電源によ
り、濃縮室出口水１３及び陰極室出口水１５、陽極室出
口水１７に移動させることにより除去する装置であり、
陰極１を有する陰極室２と陽極３を有する陽極室４、陰
極室２と陽極室４の間に陰イオン交換膜５と陽イオン交
換膜６を配置することにより形成された脱塩室７と濃縮
室８を備え、少なくとも脱塩室７内にはイオン交換体９
が充填されているものである。2. Description of the Related Art As a conventional method for producing pure water, the water in the inlet of the desalting chamber is passed through a container filled with an ion exchange resin, and the ions in the water in the inlet of the desalting chamber are exchanged for H + and OH − ions. An ion exchange method for producing pure water is known.
However, in this ion exchange method, when the exchange capacity of the ion exchange resin is saturated, acid depending on the type of ion exchange resin,
It is necessary to regenerate the ion exchange capacity using alkali. The regeneration operation of the ion exchange resin is complicated, and a large amount of acid,
It requires careful attention to storage, handling, and disposal of the alkali, and also has a problem that the equipment becomes large. On the other hand, in recent years, an electric regeneration type desalination apparatus has been developed which regenerates an ion exchanger by electricity and continuously produces pure water. This is as shown in FIG.
A device for removing the ion content in 0 by moving it to the concentrating chamber outlet water 13, the cathode chamber outlet water 15, and the anode chamber outlet water 17 by a DC power source applied to both ends of the device,
A cathode chamber 2 having a cathode 1 and an anode chamber 4 having an anode 3, and a desalting chamber 7 formed by disposing an anion exchange membrane 5 and a cation exchange membrane 6 between the cathode chamber 2 and the anode chamber 4. A concentrating chamber 8 is provided, and an ion exchanger 9 is provided at least in the desalting chamber 7.
Are filled.
【０００３】ここで、イオン交換体９は、イオン交換樹
脂、イオン交換繊維、グラフト重合法によりイオン交換
基を導入されたイオン交換不織布、スペーサ等のイオン
交換機能を持つ物であればどのようなイオン交換体でも
よく、陰イオン交換体、陽イオン交換体を単一、もしく
は混合、もしくは複層状に充填してある。陰極室２に陰
極室入口水１４を、陽極室４に陽極室入口水１６を、濃
縮室８に濃縮室入口水１２を、脱塩室７に脱塩室入口水
１０を導入し、陰極１と陽極３間に直流電流を印可する
ことにより、脱塩室入口水１０中に含まれているイオン
分は、イオン交換体９の表面を電位の方向に移動し、陰
イオンは陰イオン交換膜５、陽イオンは陽イオン交換膜
６を透過して、濃縮室８中の濃縮水、陰極室２中の陰極
液及び陽極室４中の陽極液に移動し、脱塩室入口水１０
は脱イオン処理され純水１１が製造される。The ion exchanger 9 may be any one having an ion exchange function such as an ion exchange resin, an ion exchange fiber, an ion exchange non-woven fabric having an ion exchange group introduced by a graft polymerization method, and a spacer. It may be an ion exchanger, and the anion exchanger and the cation exchanger are packed in a single form, a mixed form, or a multi-layer form. The cathode chamber inlet water 14 is introduced into the cathode chamber 2, the anode chamber inlet water 16 is introduced into the anode chamber 4, the concentration chamber inlet water 12 is introduced into the concentrating chamber 8, and the desalting chamber inlet water 10 is introduced into the desalting chamber 7. By applying a direct current between the anode 3 and the anode 3, the ion content contained in the deionization chamber inlet water 10 moves in the direction of the potential on the surface of the ion exchanger 9, and the anion is anion exchange membrane. 5. The cations permeate the cation exchange membrane 6, move to the concentrated water in the concentrating chamber 8, the catholyte in the cathodic chamber 2 and the anolyte in the anodic chamber 4, and the desalting chamber inlet water 10
Is deionized and pure water 11 is produced.
【０００４】脱塩室７内に充填されたイオン交換体９
は、水解によって発生するＨ+、ＯＨ-により連続的に再
生されるため、酸あるいはアルカリによる再生作業は必
要なく、このようにして純水１１を連続的に製造するこ
とが可能となる（特許第１７８２９４３、特許第２７５
１０９０、特許第２６９９２５６号各明細書、特願平１
０−１５３６９７号）。また、最近では、脱塩室７を中
間イオン交換膜で２つの脱塩室に分割し、片方の脱塩室
の流出水をもう片方の脱塩室に導入することで、脱塩性
能を改善した電気再生式脱塩装置も開発されている（特
開２００１−２３９２７０、特開２００１−３２７９７
１号各公報）。Ion exchanger 9 filled in the desalting chamber 7
Is continuously regenerated by H + and OH − generated by hydrolyzing, so that it is not necessary to regenerate with acid or alkali, and pure water 11 can be continuously produced in this way (Patent No. 1782943, Patent No. 275
1090, Japanese Patent No. 2699256, each specification, Japanese Patent Application No. 1
0-153697). Further, recently, the desalting chamber 7 is divided into two desalting chambers by an intermediate ion exchange membrane, and the outflow water of one desalting chamber is introduced into the other desalting chamber to improve the desalination performance. The electric regeneration type desalination device described above has also been developed (Japanese Patent Laid-Open Nos. 2001-239270 and 2001-32797).
No. 1).
【０００５】前記従来の電気再生式脱塩装置では、炭
酸、シリカなどの弱陰イオン成分の除去能力が、他のイ
オン分の除去能力に比べて劣っていることが一般に知ら
れている。これらの弱陰イオン成分は、電気再生式脱塩
装置に直流電流を過大に印可すれば、その除去率が多少
改善することも知られているが、その場合でも、弱陰イ
オン成分は十分には除去できなく、単位流量当りの消費
電力は大きくなってしまう。そのため、残存弱陰イオン
成分の除去には、必要に応じてカートリッジポリッシャ
ーや電気再生式脱塩装置を後段に設置する必要があり、
設置面積、機器数の増加、価格の上昇を招くことにな
る。また、純水の使用箇所によっては、比抵抗の高い純
水と、比抵抗の比較的低い純水の２種類の純水を使用す
ることがあり、そのような場合は、比抵抗の高い純水
に、炭酸ガス等を添加することにより比抵抗を下げる操
作を行うこともある。しかし、このような処置を行うこ
とは、一度高度に脱塩した純水に不純物を添加するた
め、炭酸ガス等の添加装置やその制御などが必要にな
り、設置面積、機器数の増加、価格の上昇を招くことに
なる。It is generally known that in the conventional electric regenerative desalting apparatus, the ability to remove weak anion components such as carbonic acid and silica is inferior to the ability to remove other ion components. It is also known that the removal rate of these weak anion components can be improved to some extent if a direct current is applied to the electric regeneration type desalination device excessively. Cannot be removed, and the power consumption per unit flow rate increases. Therefore, in order to remove residual weak anion components, it is necessary to install a cartridge polisher or an electric regenerative desalting device in the subsequent stage, if necessary.
This will increase the installation area, the number of devices, and the price. Depending on the place of use of pure water, pure water with high specific resistance and pure water with relatively low specific resistance may be used. In such a case, pure water with high specific resistance is used. The operation of lowering the specific resistance may be performed by adding carbon dioxide gas or the like to water. However, performing such a treatment adds impurities to pure water that has been highly desalted once, so that it is necessary to add a device such as carbon dioxide and control it, which increases the installation area, the number of devices, and the price. Will lead to a rise.
【０００６】[0006]
【発明が解決しようとする課題】本発明は、上記従来技
術の問題点を解消し、電気再生式脱塩装置の弱陰イオン
成分の除去性能を高めると共に、外部に２種以上の水質
の異なる純水を供給することができる電気再生式脱塩装
置を提供することを課題とする。DISCLOSURE OF THE INVENTION The present invention solves the above-mentioned problems of the prior art, enhances the performance of removing weak anion components of an electric regenerative desalination apparatus, and has two or more kinds of different water qualities externally. An object of the present invention is to provide an electric regenerative desalination apparatus that can supply pure water.
【０００７】[0007]
【課題を解決するための手段】上記課題を解決するため
に、本発明では、陰極を有する陰極室と、陽極を有する
陽極室とを有し、該両極室間に、陽極側に陽イオン交換
膜、陰極側に陰イオン交換膜を配置して構成される濃縮
室と、次の（ａ）〜（ｅ）の脱塩室、（ａ）陰極側に陽
イオン交換膜陽極側に陰イオン交換膜を配置し、内部に
イオン交換体を充填した脱塩室、（ｂ）両側に陽イオン
交換膜を配置し、内部にイオン交換体を充填した脱塩
室、（ｃ）両側に陰イオン交換膜を配置し、内部にイオ
ン交換体を充填した脱塩室、（ｄ）陰極側に陽イオン交
換膜、陽極側にバイポーラ膜を配置し、内部にイオン交
換体を充填した脱塩室、（ｅ）陰極側にバイポーラ膜、
陽極側に陰イオン交換膜を配置し、内部にイオン交換体
を充填した脱塩室、のいずれか１種類以上の脱塩室とを
配置して構成される電気再生式脱塩装置であって、前記
脱塩室として、両側に濃縮室を配置した前記いずれかの
脱塩室と、間に濃縮室を介さずに前記いずれか１種類以
上の脱塩室を複数隣接して配置した脱塩室群とを、それ
ぞれ１以上有することとしたものである。In order to solve the above-mentioned problems, the present invention has a cathode chamber having a cathode and an anode chamber having an anode, and cation exchange on the anode side between the both electrode chambers. Membrane, concentrating chamber configured by arranging anion exchange membrane on the cathode side, demineralization chamber of the following (a) to (e), (a) cation exchange membrane on the cathode side and anion exchange on the anode side A desalting chamber with a membrane placed inside and an ion exchanger filled in, (b) a cation exchange membrane placed on both sides inside, a desalting chamber filled with an ion exchanger inside, (c) anion exchange placed on both sides A desalting chamber in which a membrane is arranged and filled with an ion exchanger, (d) a cation exchange membrane on the cathode side, a bipolar membrane on the anode side, and a desalting chamber in which an ion exchanger is filled inside ( e) Bipolar film on the cathode side,
An electric regenerative desalination device comprising an anion exchange membrane disposed on the anode side and a desalination chamber filled with an ion exchanger, and at least one desalination chamber disposed therein. As the desalting chamber, any one of the desalting chambers having concentrating chambers arranged on both sides and a desalting chamber in which a plurality of the one or more desalting chambers are arranged adjacent to each other without a concentrating chamber therebetween The number of chamber groups is one or more.
【０００８】前記電気再生式脱塩装置において、濃縮室
を介さずに配置した脱塩室群は、前記脱塩室群を構成す
る第１の脱塩室に導入された被処理水が、第１の脱塩室
から前記脱塩室群を構成する最終の脱塩室まで、順次直
列で通水して脱塩処理されるように接続するのがよく、
前記（ａ）の脱塩室に充填されるイオン交換体は、陰イ
オン交換体、陽イオン交換体、又は陰イオン交換体と陽
イオン交換体の両方のイオン交換体であり、前記（ｂ）
の脱塩室に充填されるイオン交換体は、陽イオン交換体
であり、前記（ｃ）の脱塩室に充填されるイオン交換体
は、陰イオン交換体であり、前記（ｄ）の脱塩室に充填
されるイオン交換体は、陽イオン交換体であり、前記
（ｅ）の脱塩室に充填されるイオン交換体は陰イオン交
換体であるのがよく、また、前記イオン交換体は、放射
線グラフト重合法によりイオン交換基が導入されたイオ
ン交換繊維からなるイオン交換体であり、イオン交換繊
維からなるイオン交換体は、不織布又は織布、及び網目
状のスペーサとすることができる。In the electric regeneration type desalination apparatus, the desalination chamber group arranged without the concentration chamber is such that the water to be treated introduced into the first desalination chamber constituting the desalination chamber group is From the desalination chamber No. 1 to the final desalination chamber constituting the group of desalination chambers, it is preferable to connect so as to perform desalination treatment by sequentially passing water in series.
The ion exchanger packed in the desalting chamber of (a) is an anion exchanger, a cation exchanger, or both an anion exchanger and a cation exchanger, and (b)
The ion exchanger packed in the desalting chamber of is a cation exchanger, and the ion exchanger packed in the desalting chamber of (c) is an anion exchanger. The ion exchanger packed in the salt chamber is preferably a cation exchanger, and the ion exchanger packed in the desalting chamber in (e) is preferably an anion exchanger. Is an ion exchanger comprising ion exchange fibers having ion exchange groups introduced by a radiation graft polymerization method, and the ion exchanger comprising ion exchange fibers may be a non-woven fabric or a woven fabric, and a mesh spacer. .
【０００９】[0009]
【発明の実施の形態】本発明によれば、両側に濃縮室が
隣接する通常の脱塩室と、間に濃縮室を介さずに複数の
脱塩室を配置した弱陰イオン分の除去性能が高い脱塩室
群とを用いて、１台の電気再生式脱塩装置を構成するこ
とで、弱陰イオン分の除去性能を高めた比抵抗の高い純
水を得ることができると共に、従来の電気再生式脱塩装
置で得られる程度の純水をも同時に得られるため、２種
類の水質の純水を外部に供給することができる。DETAILED DESCRIPTION OF THE INVENTION According to the present invention, a weak deionizing component removal performance is obtained by arranging a normal desalting chamber having adjacent concentrating chambers on both sides and a plurality of desalting chambers without a concentrating chamber therebetween. It is possible to obtain pure water with high specific resistance and improved removal performance of weak anions by constructing a single electric regenerative desalination device using a high desalination chamber group. Since it is possible to simultaneously obtain pure water to the extent that can be obtained with the electric regenerating type desalination apparatus, it is possible to supply pure water of two types of water quality to the outside.
【００１０】次に、図面を用いて本発明を詳細に説明す
る。図１は、本発明による電気再生式脱塩装置の一例を
示す概略構成図であり、図１では、前記した図３に示す
構成と同一構成を同一符号で示して説明する。陰極１を
有する陰極室２と、陽極３を有する陽極室４を対向して
配置し、この陰極室２と陽極室４の間に、陰極１側に陰
イオン交換膜５を、陽極３側に陽イオン交換膜６を配置
して構成された濃縮室８と、陰極１側に陽イオン交換膜
６を、陽極３側に陰イオン交換膜５を配置して構成され
た脱塩室７と、両側に陰イオン交換膜５を配置して構成
された脱塩室７１、７２と、陰極１側に陽イオン交換膜
６を、陽極３側に陰イオン交換膜５を配置して構成され
た脱塩室７３とから、間に濃縮室を介さずに構成した脱
塩室群７０とにより、本発明による電気再生式脱塩装置
が構成される。Next, the present invention will be described in detail with reference to the drawings. FIG. 1 is a schematic configuration diagram showing an example of an electric regeneration type desalination apparatus according to the present invention. In FIG. 1, the same configuration as the configuration shown in FIG. A cathode chamber 2 having a cathode 1 and an anode chamber 4 having an anode 3 are arranged so as to face each other, and between the cathode chamber 2 and the anode chamber 4, an anion exchange membrane 5 is provided on the cathode 1 side and on the anode 3 side. A concentrating chamber 8 configured by arranging a cation exchange membrane 6, a desalting chamber 7 configured by arranging a cation exchange membrane 6 on the cathode 1 side and an anion exchange membrane 5 on the anode 3 side, Desalination chambers 71 and 72 configured by arranging anion exchange membrane 5 on both sides, and a deionization chamber configured by cation exchange membrane 6 on the cathode 1 side and anion exchange membrane 5 on the anode 3 side. An electrically regenerative desalination apparatus according to the present invention is configured by the salt chamber 73 and the desalination chamber group 70 configured without a concentrating chamber therebetween.
【００１１】ここで脱塩室群は、第１の脱塩室７１の出
口が第２の脱塩室７２の入口に、第２の脱塩室７２の出
口が第３の脱塩室７３の入口に接続されており、第１の
脱塩室７１、第２の脱塩室７２の両側に存在するイオン
交換膜は陰イオン父換膜５であるため、内部に充填する
イオン交換体９は陰イオン交換体とし、第３の脱塩室７
３、及び脱塩室７は陰イオン交換膜５と陽イオン交換膜
６で形成されているため、充填するイオン交換体９は、
陰イオン交換体と陽イオン交換体の混合イオン交換体と
した。これは、脱塩室の両側にあるイオン交換膜が陰イ
オン交換膜５と陽イオン交換膜６である場合には、電極
間に直流電流を印可すると、被処理水中の陰イオンは陰
イオン交換膜５を通過して濃縮室８へ、陽イオンは陽イ
オン交換膜６を通過して濃縮室８へ移動するため、陰イ
オン交換体と陽イオン交換体の両方を脱塩室に充填する
と脱イオン効果があるのに対し、脱塩室の両側にあるイ
オン交換膜が両方とも陰イオン交換膜５の場合は、被処
理水中の陽イオンは陰イオン交換膜５を通過できないた
め、陽イオン交換体を内部に充填していても連続脱塩効
果が期待できないためである。In the desalting chamber group, the outlet of the first desalting chamber 71 is the inlet of the second desalting chamber 72 and the outlet of the second desalting chamber 72 is the third desalting chamber 73. Since the ion exchange membranes connected to the inlet and existing on both sides of the first desalting chamber 71 and the second desalting chamber 72 are the anion father exchange membranes 5, the ion exchanger 9 filled inside is Anion exchanger, third desalting chamber 7
Since 3 and the desalting chamber 7 are formed by the anion exchange membrane 5 and the cation exchange membrane 6, the filling ion exchanger 9 is
A mixed ion exchanger of an anion exchanger and a cation exchanger was used. This is because, when the ion exchange membranes on both sides of the desalting chamber are the anion exchange membrane 5 and the cation exchange membrane 6, when a direct current is applied between the electrodes, the anions in the water to be treated are anion exchanged. Since the cations pass through the membrane 5 to the concentrating chamber 8 and the cations pass through the cation exchange membrane 6 to the concentrating chamber 8, when both the anion exchanger and the cation exchanger are filled in the desalting chamber, they are desorbed. In contrast to the ion effect, when the ion exchange membranes on both sides of the desalting chamber are both anion exchange membranes 5, the cations in the water to be treated cannot pass through the anion exchange membranes 5, so the cation exchange This is because a continuous desalting effect cannot be expected even if the body is filled inside.
【００１２】同様に、両側に陽イオン交換膜６を配置し
た脱塩室を用いる場合には、陰イオンは陽イオン交換膜
６を通過できないため、内部には陽イオン交換体のみを
充填するのがよい。また、濃縮室８、及び両極室２、４
にも、イオン交換体９を充填することが望ましく、この
イオン交換体９は、その形状、種類に特に制限はない
が、濃縮室８には陽イオン交換体と陰イオン交換体の両
者を使用し、陽イオン交換膜側に陽イオン交換体を、陰
イオン交換膜側に陰イオン交換体を配置するのが析出の
防止に効果的である。陰極室２には、脱塩室７が隣接す
る場合には陽イオン交換体を、濃縮室８が隣接する場合
には陰イオン交換体を充填するのがよく、陽極室４に
は、脱塩室７が隣接する場合には陰イオン交換体を、濃
縮室８が隣接する場合には陽イオン交換体を充填するの
がよい。濃縮室８、両極室２、４には、一部にイオン交
換体以外の、例えばスペーサを充填することもできる。Similarly, when a desalting chamber having cation exchange membranes 6 arranged on both sides is used, anions cannot pass through the cation exchange membranes 6, so that only the cation exchanger is filled inside. Is good. In addition, the concentrating chamber 8 and the bipolar chambers 2 and 4
In addition, it is desirable to fill with the ion exchanger 9. The ion exchanger 9 is not particularly limited in shape and type, but both the cation exchanger and the anion exchanger are used in the concentrating chamber 8. However, it is effective to prevent precipitation by disposing a cation exchanger on the cation exchange membrane side and an anion exchanger on the anion exchange membrane side. The cathode chamber 2 is preferably filled with a cation exchanger when the desalting chamber 7 is adjacent to it, and the anion exchanger when the concentrating chamber 8 is adjacent to the cathode chamber 2. It is advisable to fill the anion exchanger when the chambers 7 are adjacent and the cation exchanger when the concentrating chambers 8 are adjacent. The concentration chamber 8 and the bipolar chambers 2 and 4 can be partially filled with a spacer other than the ion exchanger, for example.
【００１３】陰極室２に陰極室入口水１４を、陽極室４
に陽極室入口水１６を、濃縮室８に濃縮室入口水１２
を、脱塩室７に脱塩室入口水１０を、脱塩室群７０のう
ちの第１の脱塩室７１に脱塩室群入口水１８を導入し、
陰極１と陽極３間に直流電流を印可することにより、脱
塩室入口水１０及び脱塩室群入口水１８中に含まれてい
るイオン分は、イ才ン交換体９の表面を電位の方向に移
動し、陰イオンは陰イオン交換膜５、陽イオンは陽イオ
ン交換膜６を透過して、濃縮室８中の濃縮水、陰極室２
中の陰極水、陽極室４中の陽極水に移動し系外に排出さ
れ、脱塩室入口水１０及び脱塩室群入口水１８は脱イオ
ン処理され、脱塩室出口純水１１及び脱塩室群出口純水
１９が製造される。１以上の脱塩室７と１以上の脱塩室
群７０は、各々同じ脱塩室入口水１０を処理しても、別
の水を処理してもかまわず、脱塩室７と脱塩室群７０の
出口水は、別々に外部に供給してもかまわず、混合して
供給してもよい。また、脱塩室７の出口水を脱塩室群７
０を構成している第１の脱塩室７１に導入してさらに脱
塩処理しても、脱塩室群７０を構成している最終の脱塩
室７３の出口水を脱塩室７の入口水として用いることも
可能である。The cathode chamber inlet water 14 is supplied to the cathode chamber 2 and the cathode chamber 4 is supplied with water.
To the anode chamber inlet water 16 and to the concentration chamber 8 to the concentration chamber inlet water 12
To the desalting chamber inlet water 10 to the desalting chamber 7 and the desalting chamber group inlet water 18 to the first desalting chamber 71 of the desalting chamber group 70,
By applying a direct current between the cathode 1 and the anode 3, the ionic components contained in the desalting compartment inlet water 10 and the desalting compartment group inlet water 18 have a potential on the surface of the ion exchanger 9. Direction, the anions permeate the anion exchange membrane 5 and the cations permeate the cation exchange membrane 6, and the concentrated water in the concentrating chamber 8 and the cathode chamber 2
It moves to the cathode water inside and the anode water in the anode chamber 4 and is discharged to the outside of the system. The desalting chamber inlet water 10 and the desalting chamber group inlet water 18 are deionized, and the desalting chamber outlet pure water 11 and The salt chamber group outlet pure water 19 is produced. The one or more desalting chambers 7 and the one or more desalting chamber groups 70 may each treat the same desalting chamber inlet water 10 or different water. The outlet water of the chamber group 70 may be separately supplied to the outside, or may be mixed and supplied. In addition, the outlet water of the desalination chamber 7 is used
Even if it is introduced into the first desalting chamber 71 that constitutes 0 and further desalting treatment, the outlet water of the final desalting chamber 73 that constitutes the desalting chamber group 70 will be It can also be used as inlet water.
【００１４】脱塩室７の出口水１１を脱塩室群７０に導
入する場合、及び脱塩室群７０の出口水１９を脱塩室７
に導入する場合は さらに高度の脱塩効果が期待でき
る。脱塩室群７０の作用について詳しく説明すると、第
１の脱塩室７１に導入された脱塩室入口水１０中の陰イ
オン分は、両極に印可された直流電流により陽極３側に
移動し、陰イオン交換膜５を透過して濃縮室８中に移動
する。陽イオン分は、陰極側に配置されている陰イオン
交換膜５を透過することができないため、第１の脱塩室
７１に留まる。これにより、第１の脱塩室７１内は陰イ
オン分のみが減少するためｐＨが高くなり、弱アニオン
成分もイオン化することで除去しやすくなる。陰極側に
配置されているイオン交換膜５からは、第２の脱塩室７
２で除去される残存陰イオン分とＯＨ-が第１の脱塩室
７１に透過してくる。このＯＨ-の作用で、第１の脱塩
室７１内に充填されている陰イオン交換体は再生され、
再び脱塩室入口水１０中の陰イオン分を除去できるよう
になる。When the outlet water 11 from the desalting chamber 7 is introduced into the desalting chamber group 70, and the outlet water 19 from the desalting chamber group 70 is supplied to the desalting chamber 7.
When it is introduced into, a higher degree of desalting effect can be expected. The operation of the desalting chamber group 70 will be described in detail. The anion component in the desalting chamber inlet water 10 introduced into the first desalting chamber 71 moves to the anode 3 side by the direct current applied to both electrodes. , Permeate the anion exchange membrane 5 and move into the concentrating chamber 8. Since the cation component cannot pass through the anion exchange membrane 5 arranged on the cathode side, it stays in the first deionization chamber 71. As a result, in the first desalting chamber 71, only the anion component is reduced, so that the pH is increased, and the weak anion component is ionized to be easily removed. From the ion exchange membrane 5 arranged on the cathode side, the second deionization chamber 7
The residual anion component and OH − removed in 2 permeate into the first desalting chamber 71. By the action of this OH − , the anion exchanger filled in the first deionization chamber 71 is regenerated,
The anion component in the desalting compartment inlet water 10 can be removed again.
【００１５】第１の脱塩室７１で上述の脱塩処理をされ
た処理水は、続いて第２の脱塩室７２に導入される。こ
こでも第１の脱塩室７１での脱塩処理と同様に、陰イオ
ン分は陰イオン交換膜５を透過して第１の脱塩室へ移動
し、陽イオン分は処理水中に留まるため、処理水は第２
の脱塩室７２に導入された時点からｐＨが高いまま保持
され、さらに弱陰イオン成分の脱塩効果を高くしてい
る。これにより、第１の脱塩室７１で脱塩しきれなかっ
た、主に弱陰イオン分かなる残存陰イオン分が除去され
る。陰極１側に存在する陰イオン交換膜５からは、主に
ＯＨ-が第２の脱塩室７２に透過してくるため、第２の
脱塩室中の陰イオン交換体は、第１の脱塩室７１中の陰
イオン交換体よりも効率よく再生され、第１の脱塩室で
除去しきれなかった陰イオン成分の除去を効率よく行う
ことができる。第２の脱塩室７２でさらに脱塩処理され
た処理水は、第３の脱塩室７３に導入され、最終的な脱
塩処理が行われる。The treated water that has been desalted as described above in the first desalination chamber 71 is subsequently introduced into the second desalination chamber 72. Here, as in the desalting process in the first desalting chamber 71, the anion component permeates the anion exchange membrane 5 and moves to the first desalting chamber, and the cation component remains in the treated water. , Treated water is second
The pH is kept high from the time of introduction into the desalting chamber 72, and the desalting effect of the weak anion component is further enhanced. As a result, the remaining anion component, which is mainly weak anion component, which could not be desalted in the first desalting chamber 71, is removed. Since OH − mainly permeates into the second deionization chamber 72 from the anion exchange membrane 5 existing on the cathode 1 side, the anion exchanger in the second deionization chamber is the first anion exchanger. It is regenerated more efficiently than the anion exchanger in the desalting chamber 71, and the anion components that could not be completely removed in the first desalting chamber can be efficiently removed. The treated water that has been further desalted in the second desalting chamber 72 is introduced into the third desalting chamber 73, and the final desalting process is performed.
【００１６】第３の脱塩室７３に導入された時点で、処
理水中の陰イオン成分はほとんどなくなっており、極微
量の弱陰イオン成分及び陽イオン成分が除去の対象とな
る。第３の脱塩室７３には、陽イオン交換体と陰イオン
交換体が充填されており、陽イオン分は陽イオン交換体
とイオン交換された後、陰極１側に存在する陽イオン交
換膜６を透過して濃縮室８に移動する。残存する微量の
弱陰イオン成分は、第３の脱塩室７３中の陰イオン交換
体とイオン交換した後、陽極３側にある陰イオン交換膜
５を透過して、第２の脱塩室７２に移動する。第３の脱
塩室では、イオン分の移動の他、水解によって水がＨ+
とＯＨ-に分解されており、これが第３の脱塩室７３中
の陽イオン交換体、陰イオン交換体を再生すると共に、
ＯＨ-は、第１、第２の脱塩室７１、７２内に充填され
た陰イオン交換体の再生にも用いられるため、酸、アル
カリによるイオン交換体の再生作業は必要なく、このよ
うにして、脱塩室入口水１０中のイオン分は、弱陰イオ
ン成分も含めて十分に除去され、連続的に純水１９を得
ることができる。At the time of introduction into the third desalting chamber 73, the anion components in the treated water have almost disappeared, and a very small amount of weak anion components and cation components are targets for removal. The third desalting chamber 73 is filled with a cation exchanger and an anion exchanger, and after the cation component is ion-exchanged with the cation exchanger, a cation exchange membrane existing on the cathode 1 side. It permeates 6 and moves to the concentrating chamber 8. The small amount of the remaining weak anion component is ion-exchanged with the anion exchanger in the third desalting chamber 73, and then permeates the anion exchange membrane 5 on the side of the anode 3 to form the second desalting chamber. Move to 72. In the third desalination chamber, water moves to H +
And OH − , which regenerates the cation exchanger and the anion exchanger in the third desalting chamber 73, and
Since OH − is also used to regenerate the anion exchanger filled in the first and second desalting chambers 71 and 72, it is not necessary to regenerate the ion exchanger with an acid or alkali. Thus, the ion content in the deionization chamber inlet water 10 including the weak anion component is sufficiently removed, and the pure water 19 can be continuously obtained.
【００１７】ここで、陽イオン分は、弱陰イオン分に比
べ遥かに除去し易いため、通常は第３の脱塩室７３だけ
で十分除去することが可能だが、脱塩室入口水１０中に
陽イオン成分が多量に含まれている場合には、本図であ
げている第３の脱塩室に充填するイオン交換体を陽イオ
ンのみとすることで、陽イオンの除去能力を増大した
り、第２の脱塩室７２の陽極側のイオン交換膜を陽イオ
ン交換膜６に変更し、第２の脱塩室７２に充填されてい
るイオン交換体を陽イオン交換体と陰イオン交換体の混
合イオン交換体とすると共に、第３の脱塩室７３中のイ
オン交換体を陽イオン交換体とし、第１の脱塩室７１か
ら流出した処理水を第３の脱塩室７３に導入し、さらに
陰イオン交換体と陽イオン交換体の充填された第２の脱
塩室７２に導入する、という処理方法を行って陽イオン
の除去能力を増大させてもよい。また、本図の第３の脱
塩室７３に加え、さらに第４の脱塩室を設け、第３の脱
塩室７３の出口水をさらに脱塩処理するということも可
能である。Since the cation component is much easier to remove than the weak anion component, it is usually possible to sufficiently remove the cation component only in the third desalting chamber 73, but in the desalting chamber inlet water 10 When a large amount of cation components are contained in the cations, the cation removal capacity is increased by using only cations as the ion exchanger to fill the third desalting chamber shown in this figure. Alternatively, the ion exchange membrane on the anode side of the second desalting chamber 72 is changed to the cation exchange membrane 6, and the ion exchanger filled in the second desalting chamber 72 is exchanged with the cation exchanger for anion exchange. In addition to the body mixed ion exchanger, the ion exchanger in the third desalting chamber 73 is used as a cation exchanger, and the treated water flowing out from the first desalting chamber 71 is supplied to the third desalting chamber 73. It is introduced, and further introduced into the second desalting chamber 72 filled with an anion exchanger and a cation exchanger. It may be increased removal capacity of the cation performs processing method called. Further, in addition to the third desalting chamber 73 in this figure, it is possible to further provide a fourth desalting chamber to further desalinate the outlet water of the third desalting chamber 73.
【００１８】脱塩室群７０を、片側にバイポーラ膜を配
置した脱塩室を使用して構成する場合は、陰イオン交換
膜とバイポーラ膜で形成された脱塩室内部には陰イオン
交換体を、バイポーラ膜と陽イオン交換膜で形成された
脱塩室内部には陽イオン交換体を充填すると脱塩効率が
高い。バイポーラ膜の特性から、バイポーラ膜にて低電
圧で効率的に水解によるＨ+、ＯＨ-が発生し、Ｈ+は陽
イオン交換体を、ＯＨ-は陰イオン交換体を再生させ、
脱塩室群入口水１８中のイオン分を除去することが可能
となる。水解を効率的に発生させられるため、バイポー
ラ膜を用いた場合は、さらに運転電圧が低減することが
期待できる。また、電気再生式脱塩装置においては、従
来、脱塩室の数の±１の濃縮室が必要であったのが、上
述のように、複数枚のイオン交換膜で分割された脱塩室
を用いて電気再生式脱塩装置を形成することにより、濃
縮室の室数を減らすことが可能になり、その分運転電圧
を軽減することも可能となる。When the desalting chamber group 70 is constructed by using a desalting chamber having a bipolar membrane arranged on one side, an anion exchanger is provided inside the desalting chamber formed by the anion exchange membrane and the bipolar membrane. The desalination efficiency is high when the inside of the desalination chamber formed by the bipolar membrane and the cation exchange membrane is filled with a cation exchanger. Due to the characteristics of the bipolar membrane, H + and OH − are efficiently generated by hydrolyzing at a low voltage in the bipolar membrane, H + regenerates a cation exchanger and OH − regenerates an anion exchanger,
It is possible to remove the ion component in the desalination chamber group inlet water 18. Since the hydrolyzation can be efficiently generated, it is expected that the operating voltage will be further reduced when the bipolar membrane is used. Further, in the electric regeneration type desalination apparatus, conventionally, a concentration chamber having a number of desalination chambers of ± 1 was required, but as described above, the desalination chamber divided by a plurality of ion exchange membranes is used. By forming an electric regeneration type desalination apparatus using the above, it is possible to reduce the number of concentration chambers, and it is also possible to reduce the operating voltage accordingly.
【００１９】[0019]
【実施例】以下、本発明を実施例により具体的に説明す
る。
実施例１
この実施例では、本発明の効果を比較例との対比の元で
説明する。試験設備は、図２に示す試験装置のフロー図
の通りであり、、脱塩室入口水１０、濃縮室入口水１、
陰極室入口水１４、陽極室入口水１６として、藤沢市水
を活性炭濾過器、保安フィルタ、逆浸透膜装置で前処理
したものを使用し、その水質は、比抵抗０．２５ＭΩ・
ｃｍであった。本実施例では、図２に示す試験装置中の
電気再生式脱塩装置に、図１に示す構成の電気再生式脱
塩装置を用い、脱塩室入口水１０の流量を１００Ｌ／
ｈ、脱塩室群入口水１８の流量を１５０Ｌ／ｈ、濃縮室
入口水１２の流量を５０Ｌ／ｈ、陰極室入口水１４の流
量及び陽極室入口水１６の流量をそれぞれ１０Ｌ／ｈと
して、０．４Ａの直流電流を陰極１と陽極３に印可して
運転を行った。EXAMPLES The present invention will be specifically described below with reference to examples. Example 1 In this example, the effect of the present invention will be described in comparison with a comparative example. The test equipment is as shown in the flow chart of the test apparatus shown in FIG. 2, and the demineralizing chamber inlet water 10, the concentrating chamber inlet water 1,
As the cathode chamber inlet water 14 and the anode chamber inlet water 16, Fujisawa city water pretreated with an activated carbon filter, a safety filter and a reverse osmosis membrane device is used, and the water quality thereof is a specific resistance of 0.25 MΩ.
It was cm. In the present embodiment, the electric regenerative desalination apparatus having the configuration shown in FIG. 1 is used as the electric regenerative desalination apparatus in the test apparatus shown in FIG.
h, the flow rate of the deionization chamber group inlet water 18 is 150 L / h, the flow rate of the concentration chamber inlet water 12 is 50 L / h, the flow rate of the cathode chamber inlet water 14 and the flow rate of the anode chamber inlet water 16 are 10 L / h, respectively. A direct current of 0.4 A was applied to the cathode 1 and the anode 3, and the operation was performed.
【００２０】電気再生式脱塩装置は、電極面積６４０ｃ
ｍ2、脱塩室は１０室でそのうちの６室を２つの脱塩室
群７０に用い、脱塩室群７０のうち、第１の脱塩室７
１、第２の脱塩室７２は、両側を陰イオン交換膜５で形
成し、内部に陰イオン交換体を、第３の脱塩室７３及び
脱塩室７は、陰イオン交換膜５と陽イオン交換膜６で形
成し、陰イオン交換体と陽イオン交換体を充填した構成
とした。濃縮室８は５室とし、両端に陰極室２と陽極室
４を設けた。また、濃縮室８の内部には、陰イオン交換
体と陽イオン交換体を、陰極室２の内部には、陽イオン
交換体と導電性をもたないスペーサを、陽極室４の内部
には、陰イオン交換体と導電性を持たないスペーサを充
填した。上記条件で運転した結果、脱塩室群７０からは
比抵抗１７．７ＭΩ・ｃｍ、炭酸、シリカの除去率が共
に９９％程度の脱塩室群出口純水１９が、脱塩室７から
は比抵抗１４．２ＭΩ・ｃｍ、炭酸除去率９４％、シリ
カ除去率８８％程度の脱塩室出口純水１１が連続して得
られた。The electric regeneration type desalination apparatus has an electrode area of 640c.
m 2 , 10 desalting chambers, 6 of which are used for two desalting chamber groups 70, and the first desalting chamber 7 of the desalting chamber group 70
The first and second desalting chambers 72 are formed with anion exchange membranes 5 on both sides, and an anion exchanger is provided inside, and the third desalting chambers 73 and 7 are anion exchange membranes 5 and It was formed of a cation exchange membrane 6 and was filled with an anion exchanger and a cation exchanger. The concentration chamber 8 was made into 5 chambers, and the cathode chamber 2 and the anode chamber 4 were provided at both ends. Further, an anion exchanger and a cation exchanger are provided inside the concentrating chamber 8, a spacer having no conductivity with the cation exchanger is provided inside the cathode chamber 2, and a spacer having no conductivity is provided inside the anode chamber 4. , Filled with an anion exchanger and a spacer having no conductivity. As a result of operating under the above conditions, the deionization chamber group outlet pure water 19 having a specific resistance of 17.7 MΩ · cm and a removal rate of carbonic acid and silica of about 99% from the deionization chamber group 70 is discharged from the desalination chamber group 7. Pure water 11 having a specific resistance of 14.2 MΩ · cm, a carbon dioxide removal rate of 94% and a silica removal rate of about 88% was continuously obtained from the desalting chamber.
【００２１】比抵抗が高い純水と、それほど高くなくて
もかまわない純水の２種類を使用するような場合は、本
発明においては、複数の脱塩室を濃縮室を介さないで形
成した脱塩室群７０と、両側に濃縮室８を配置した脱塩
室７の各部屋数、通水流量を変化させることで、１台の
電気再生式脱塩装置で、２種類の目的にあった比抵抗の
純水を得ることが可能となる。濃縮室８の部屋数が、下
記の比較例１の９室に対して５室に減少しているため、
運転電圧は１８０V程度と比較例１に比べ低かった。ま
た、脱塩室出口純水１１と脱塩室群出口純水１９の両者
を混合して用いる場合にも、混合された純水の水質は、
１６．０ＭΩ・ｃｍで、炭酸除去率は約９７％、シリカ
除去率は約９５％と比較例１に対して高い比抵抗の純水
が得られた。In the case of using two kinds of pure water having a high specific resistance and pure water which does not need to be so high, in the present invention, a plurality of desalting chambers are formed without interposing a concentration chamber. By changing the number of each of the desalination chamber group 70 and the desalination chambers 7 having the concentration chambers 8 on both sides and the flow rate of water, one electric regenerative desalination device has two purposes. It is possible to obtain pure water having a high specific resistance. Since the number of the concentrating chambers 8 has been reduced to 5 compared to 9 in Comparative Example 1 below,
The operating voltage was about 180 V, which was lower than that of Comparative Example 1. Also, when both the deionization chamber outlet pure water 11 and the deionization chamber group outlet pure water 19 are used as a mixture, the quality of the mixed pure water is
With 16.0 MΩ · cm, the carbon dioxide removal rate was about 97% and the silica removal rate was about 95%, and pure water having a higher specific resistance than that of Comparative Example 1 was obtained.
【００２２】比較例１
比較例として、図３に示す構成の電気再生式脱塩装置を
用い、脱塩室入口水１０の流量を２５０Ｌ／ｈ、濃縮室
入口水１２の流量を９０Ｌ／ｈ、陰極室入口水１４の流
量及び陽極室入口水１６の流量をそれぞれ１０Ｌ／ｈと
して、０．４Ａの直流電流を陰極１と陽極３に印可して
運転を行った。電気再生式脱塩装置は、電極面積６４０
ｃｍ2、脱塩室は１０室、濃縮室は９室とし、両端に陰
極室と陽極室を設け、脱塩室、濃縮室内部には陰イオン
交換体と陽イオン交換体を、陰極室には陽イオン交換体
を、陽極室には陰イオン交換体を充填してある。上記条
件で運転した結果、比抵抗１４．４ＭΩ・ｃｍ程度の純
水１１が連続して製造された。この運転において、運転
電圧は２１０Ｖ、炭酸除去率９５％、シリカ除去率８８
％であった。Comparative Example 1 As a comparative example, an electric regenerative desalination apparatus having the structure shown in FIG. 3 was used, the flow rate of the inlet water 10 of the desalting chamber was 250 L / h, and the flow rate of the inlet water 12 of the concentration chamber was 90 L / h. The flow rate of the cathode chamber inlet water 14 and the anode chamber inlet water 16 was set to 10 L / h, and a DC current of 0.4 A was applied to the cathode 1 and the anode 3 for operation. The electric regeneration type desalination device has an electrode area of 640
cm 2 , demineralization chamber is 10 chambers, concentrating chamber is 9 chambers, cathode and anode chambers are provided at both ends, and anion exchanger and cation exchanger are provided in the desalting chamber and concentrating chamber as cathode chambers. Is filled with a cation exchanger and the anode chamber is filled with an anion exchanger. As a result of operating under the above conditions, pure water 11 having a specific resistance of about 14.4 MΩ · cm was continuously produced. In this operation, the operating voltage was 210 V, the carbon dioxide removal rate was 95%, and the silica removal rate was 88.
%Met.
【００２３】[0023]
【発明の効果】本発明の電気再生式脱塩装置によれば、
上述したように、被処理水中の弱陰イオン成分を除去す
る能力を高め比抵抗の高い純水を得ることができると共
に、水質の異なる２種類の純水を外部に供給することが
可能となる。According to the electric regeneration type desalination apparatus of the present invention,
As described above, it is possible to enhance the ability to remove the weak anion component in the water to be treated and obtain pure water with high specific resistance, and to supply two kinds of pure water having different water qualities to the outside. .
【図１】本発明の電気再生式脱塩装置の一例を示す概略
構成図。FIG. 1 is a schematic configuration diagram showing an example of an electric regeneration type desalination apparatus of the present invention.
【図２】実施例に用いた試験装置のフロー図。FIG. 2 is a flowchart of the test apparatus used in the examples.
【図３】従来の電気再生式脱塩装置の一例を示す概略構
成図。FIG. 3 is a schematic configuration diagram showing an example of a conventional electric regenerative desalination apparatus.
【符号の説明】
１：陰極、２：陰極室、３：陽極、４：陽極室、５：陰
イオン交換膜、６：陽イオン交換膜、７：脱塩室、８：
濃縮室、９：イオン交換体、１０：脱塩室入口水、１
１：純水、１２：濃縮室入口水、１３：濃縮室出口水、
１４：陰極室入口水、１５：陰極室出口水、１６：陽極
室入口水、１７：陽極室出口水、１８：脱塩室群入口
水、１９：純水、７１：脱塩室群を構成する第１の脱塩
室、７２：脱塩室群を構成する第２の脱塩室、７３：脱
塩室群を構成する第３の脱塩室[Explanation of Codes] 1: Cathode, 2: Cathode chamber, 3: Anode, 4: Anode chamber, 5: Anion exchange membrane, 6: Cation exchange membrane, 7: Deionization chamber, 8:
Concentration chamber, 9: ion exchanger, 10: water in the desalting chamber, 1
1: Pure water, 12: Concentration chamber inlet water, 13: Concentration chamber outlet water,
14: cathode chamber inlet water, 15: cathode chamber outlet water, 16: anode chamber inlet water, 17: anode chamber outlet water, 18: desalination chamber group inlet water, 19: pure water, 71: desalination chamber group First desalination chamber, 72: second desalination chamber that constitutes the desalination chamber group, 73: third desalination chamber that constitutes the desalination chamber group
───────────────────────────────────────────────────── フロントページの続き Ｆターム(参考） 4D006 GA17 HA43 HA44 HA47 JA30A JA30C JA44A JA58A MA03 MA13 MA14 MA15 PA01 PB06 4D061 DA03 DB13 EA09 EB04 EB13 EB17 FA08 ─────────────────────────────────────────────────── ─── Continued front page F-term (reference) 4D006 GA17 HA43 HA44 HA47 JA30A JA30C JA44A JA58A MA03 MA13 MA14 MA15 PA01 PB06 4D061 DA03 DB13 EA09 EB04 EB13 EB17 FA08
Claims (5)
極室とを有し、該両極室間に、陽極側に陽イオン交換
膜、陰極側に陰イオン交換膜を配置して構成される濃縮
室と、次の（ａ）〜（ｅ）の脱塩室、（ａ）陰極側に陽
イオン交換膜、陽極側に陰イオン交換膜を配置し、内部
にイオン交換体を充填した脱塩室、（ｂ）両側に陽イオ
ン交換膜を配置し、内部にイオン交換体を充填した脱塩
室、（ｃ）両側に陰イオン交換膜を配置し、内部にイオ
ン交換体を充填した脱塩室、（ｄ）陰極側に陽イオン交
換膜、陽極側にバイポーラ膜を配置し、内部にイオン交
換体を充填した脱塩室、（ｅ）陰極側にバイポーラ膜、
陽極側に陰イオン交換膜を配置し、内部にイオン交換体
を充填した脱塩室、のいずれか１種類以上の脱塩室とを
配置して構成される電気再生式脱塩装置であって、前記
脱塩室として、両側に濃縮室を配置した前記いずれかの
脱塩室と、間に濃縮室を介さずに前記いずれか１種類以
上の脱塩室を複数隣接して配置した脱塩室群とを、それ
ぞれ１以上有することを特徴とする電気再生式脱塩装
置。1. A cathode chamber having a cathode and an anode chamber having an anode, wherein a cation exchange membrane is disposed on the anode side and an anion exchange membrane is disposed on the cathode side between the cathode chambers. Concentration chamber and desalting chamber of the following (a) to (e), (a) a cation exchange membrane on the cathode side, an anion exchange membrane on the anode side, and a desalting chamber filled with an ion exchanger Chamber, (b) deionization chamber with cation exchange membranes on both sides and inside filled with ion exchangers, (c) deionization chamber with anion exchange membranes on both sides and inside filled with ion exchangers Chamber, (d) a cation exchange membrane on the cathode side, a bipolar membrane on the anode side, and a desalting chamber filled with an ion exchanger inside, (e) a bipolar membrane on the cathode side,
An electric regenerative desalination device comprising an anion exchange membrane disposed on the anode side and a desalination chamber filled with an ion exchanger, and at least one desalination chamber disposed therein. As the desalting chamber, any one of the desalting chambers having concentrating chambers arranged on both sides and a desalting chamber in which a plurality of the one or more desalting chambers are arranged adjacent to each other without a concentrating chamber therebetween An electric regenerative desalination apparatus, characterized in that it has one or more chamber groups.
室群は、前記脱塩室群を構成する第１の脱塩室に導入さ
れた被処理水が、第１の脱塩室から前記脱塩室群を構成
する最終の脱塩室まで、順次直列で通水して脱塩処理さ
れるように接続されていることを特徴とする請求項１に
記載の電気再生式脱塩装置。2. In the desalination chamber group arranged without the concentration chamber, the treated water introduced into the first desalination chamber constituting the desalination chamber group is the first desalination chamber. 2. The electric regenerative deionization according to claim 1, wherein water is sequentially passed in series from the chamber to the final desalination chamber constituting the desalination chamber group so as to be desalted. Salt equipment.
交換体は、陰イオン交換体、陽イオン交換体、又は陰イ
オン交換体と陽イオン交換体の両方のイオン交換体であ
り、前記（ｂ）の脱塩室に充填されるイオン交換体は、
陽イオン交換体であり、前記（ｃ）の脱塩室に充填され
るイオン交換体は、陰イオン交換体であり、前記（ｄ）
の脱塩室に充填されるイオン交換体は、陽イオン交換体
であり、前記（ｅ）の脱塩室に充填されるイオン交換体
は、陰イオン交換体であることを特徴とする請求項１又
は２に記載の電気再生式脱塩装置。3. The ion exchanger packed in the desalting chamber of (a) is an anion exchanger, a cation exchanger, or both an anion exchanger and a cation exchanger. The ion exchanger filled in the desalting chamber of (b) above is
The ion exchanger, which is a cation exchanger and is filled in the desalting chamber in (c) above, is an anion exchanger, and is (d) above.
The ion exchanger packed in the desalting chamber in (e) is a cation exchanger, and the ion exchanger packed in the desalting chamber in (e) is an anion exchanger. The electric regenerative desalination apparatus according to 1 or 2.
合法によりイオン交換基が導入されたイオン交換繊維か
らなるイオン交換体であることを特徴とする請求項１、
２又は３記載の電気再生式脱塩装置。4. The ion exchanger is an ion exchanger composed of ion exchange fibers having ion exchange groups introduced by a radiation graft polymerization method.
The electric regeneration type desalination apparatus according to 2 or 3.
体は、不織布又は織布、及び網目状のスペーサであるこ
とを特徴とする請求項４記載の電気再生式脱塩装置。5. The electric regenerative desalination apparatus according to claim 4, wherein the ion exchanger made of the ion exchange fiber is a non-woven fabric or a woven fabric, and a mesh spacer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2002136604A JP3729348B2 (en) | 2002-05-13 | 2002-05-13 | Electric regenerative desalination equipment |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2002136604A JP3729348B2 (en) | 2002-05-13 | 2002-05-13 | Electric regenerative desalination equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2003326271A true JP2003326271A (en) | 2003-11-18 |
| JP3729348B2 JP3729348B2 (en) | 2005-12-21 |
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ID=29698574
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2002136604A Expired - Fee Related JP3729348B2 (en) | 2002-05-13 | 2002-05-13 | Electric regenerative desalination equipment |
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| Country | Link |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2011000575A (en) * | 2009-06-22 | 2011-01-06 | Japan Organo Co Ltd | Apparatus and method for electrically making deionized water |
| JP2012040560A (en) * | 2011-10-24 | 2012-03-01 | Japan Organo Co Ltd | Water treatment system and water treatment method |
| WO2012108310A1 (en) * | 2011-02-08 | 2012-08-16 | オルガノ株式会社 | Electric device for producing deionized water |
| JP2013039510A (en) * | 2011-08-12 | 2013-02-28 | Japan Organo Co Ltd | Electric deionized water production apparatus |
-
2002
- 2002-05-13 JP JP2002136604A patent/JP3729348B2/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2011000575A (en) * | 2009-06-22 | 2011-01-06 | Japan Organo Co Ltd | Apparatus and method for electrically making deionized water |
| WO2012108310A1 (en) * | 2011-02-08 | 2012-08-16 | オルガノ株式会社 | Electric device for producing deionized water |
| JP2013039510A (en) * | 2011-08-12 | 2013-02-28 | Japan Organo Co Ltd | Electric deionized water production apparatus |
| JP2012040560A (en) * | 2011-10-24 | 2012-03-01 | Japan Organo Co Ltd | Water treatment system and water treatment method |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3729348B2 (en) | 2005-12-21 |
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