JP2001198577A - Electric deionizing device - Google Patents
Electric deionizing deviceInfo
- Publication number
- JP2001198577A JP2001198577A JP2000011989A JP2000011989A JP2001198577A JP 2001198577 A JP2001198577 A JP 2001198577A JP 2000011989 A JP2000011989 A JP 2000011989A JP 2000011989 A JP2000011989 A JP 2000011989A JP 2001198577 A JP2001198577 A JP 2001198577A
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- Prior art keywords
- chamber
- water
- membrane
- electrodeionization apparatus
- electrodeionization
- Prior art date
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- 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、陰極と陽極との間
に、複数のアニオン交換膜とカチオン交換膜とを交互に
配列して濃縮室と脱塩室とを交互に形成してなる電気脱
イオン装置に係り、特に、濃縮室の構成を改良すること
により、濃縮室内でのスケールの発生を防止した電気脱
イオン装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an electric device comprising a plurality of anion exchange membranes and a plurality of cation exchange membranes arranged alternately between a cathode and an anode to alternately form a concentration chamber and a desalination chamber. The present invention relates to a deionization apparatus, and more particularly, to an electrodeionization apparatus in which the generation of scale in a concentration chamber is prevented by improving the configuration of a concentration chamber.
【０００２】[0002]
【従来の技術】従来、半導体製造工場、液晶製造工場、
製薬工業、食品工業、電力工業等の各種の産業又は民生
用ないし研究施設等において使用される脱イオン水の製
造には、図３（ａ）に示す如く、電極（陽極１１，陰極
１２）の間に複数のアニオン交換膜１３及びカチオン交
換膜１４を交互に配列して濃縮室１５と脱塩室１６とを
交互に形成し、脱塩室１６にイオン交換樹脂、イオン交
換繊維もしくはグラフト交換体等からなるアニオン交換
体及びカチオン交換体を混合もしくは複層状に充填した
電気脱イオン装置が多用されている（特許第１７８２９
４３号、特許第２７５１０９０号、特許第２６９９２５
６号）。なお、図３（ａ）において、１７は陽極室、１
８は陰極室である。2. Description of the Related Art Conventionally, semiconductor manufacturing plants, liquid crystal manufacturing plants,
As shown in FIG. 3 (a), the production of deionized water used in various industries such as the pharmaceutical industry, the food industry, the electric power industry, etc., or for consumer or research facilities, requires the use of electrodes (anode 11, cathode 12). A plurality of anion exchange membranes 13 and cation exchange membranes 14 are alternately arranged therebetween to form a concentration chamber 15 and a desalination chamber 16 alternately, and an ion exchange resin, an ion exchange fiber or a graft exchanger in the desalination chamber 16. An electrodeionization apparatus in which an anion exchanger and a cation exchanger made of a mixture or the like are mixed or filled in a multi-layered form is frequently used (Japanese Patent No. 17829).
No. 43, Japanese Patent No. 2751090, Japanese Patent No. 269925
No. 6). In FIG. 3A, reference numeral 17 denotes an anode chamber;
8 is a cathode chamber.
【０００３】電気脱イオン装置は、水解離によってＨ＋
イオンとＯＨ−イオンを生成させ、脱塩室内に充填され
ているイオン交換体を連続して再生することによって、
効率的な脱塩処理が可能であり、従来から広く用いられ
てきたイオン交換樹脂装置のような薬品を用いた再生処
理を必要とせず、完全な連続採水が可能で、高純度の水
が得られるという優れた効果を発揮する。[0003] The electrodeionization apparatus uses water to dissociate H +
Ions and OH - to produce ions, by continuously reproducing ion exchanger filled in the desalting compartment,
Efficient desalination treatment is possible, and complete continuous water sampling is possible without the need for regeneration treatment using chemicals such as ion exchange resin equipment that has been widely used in the past. It has an excellent effect of being obtained.
【０００４】しかしながら、浄水場等で河川水、地下水
等を除濁、脱塩素、軟化処理した水道水を電気脱イオン
装置の被処理水として直接用いた場合、 濃縮室内でのスケール発生 ＣＯ２負荷増大による処理水導電率の悪化 が起こることから、従来において、水道水を直接電気脱
イオン装置の被処理水として通水することは行われてい
ない。However, river water in water purification plants and the like, turbidity dividing the groundwater, when used directly dechlorinated, the softening treatment was tap water as water to be treated electrodeionization apparatus, scale formation CO 2 loading in the concentration chamber Conventionally, tap water is not directly passed as the water to be treated in the electrodeionization apparatus because the conductivity of the treated water is deteriorated due to the increase.
【０００５】上記，の問題点のうち、のＣＯ２負
荷の増大については、比較的安価な脱炭酸装置を電気脱
イオン装置の前処理装置として用いることにより解決で
きる。しかし、のスケールを防止するためには更に軟
化装置等を設置して水中の硬度成分を完全に除去するこ
とが必要となるが、軟化装置を用いた場合にはその再生
が必要となり、再生不要の電気脱イオン装置を用いるこ
とによる利点が失われてしまう。[0005] The above, of the problems, for the increase of the CO 2 loading can be solved by using a relatively inexpensive decarbonation apparatus as a pretreatment apparatus electrodeionization apparatus. However, it is necessary to further install a softening device and the like to completely remove the hardness component in the water in order to prevent the scale of the water, but when the softening device is used, the regeneration is necessary, and the regeneration is unnecessary. The advantage of using the electrodeionization device of the above is lost.
【０００６】このような問題点を解決するために、従来
から電気脱イオン装置の前処理装置として、硬度成分及
びＣＯ２濃度を低減させるために、一般的に逆浸透膜装
置（ＲＯ膜装置）を設置する方法が用いられている。In order to solve such problems, a reverse osmosis membrane apparatus (RO membrane apparatus) is generally used as a pretreatment apparatus for an electrodeionization apparatus in order to reduce the hardness component and the CO 2 concentration. Is used.
【０００７】なお、特公平７−５７３０８号公報には、
処理水量及び処理水質の向上のために、脱塩室内にバイ
ポーラ膜を設けることが記載されているが、スケール防
止についての検討はなされていない。In Japanese Patent Publication No. 7-57308,
It is described that a bipolar membrane is provided in a desalination chamber in order to improve the amount of treated water and the quality of treated water, but no study has been made on prevention of scale.
【０００８】[0008]
【発明が解決しようとする課題】しかしながら、ＲＯ膜
装置は１〜２ＭＰａという高圧で運転することから、高
価な設備が必要となり、運転費用も上昇する。そして、
このことが電気脱イオン装置が広く一般産業ないし民生
用の脱イオン水の製造装置として普及していくために解
決すべき課題となっていた。However, since the RO membrane apparatus operates at a high pressure of 1 to 2 MPa, expensive equipment is required, and the operating cost increases. And
This has been a problem to be solved in order for the electrodeionization device to be widely used as a device for producing deionized water for general industry or consumer use.
【０００９】しかも、電気脱イオン装置の前処理装置と
してＲＯ膜装置を用いた場合でも、ＲＯ膜からわずかに
リークしてくるカルシウムによって、電気脱イオン装置
の濃縮室内で炭酸カルシウムスケールが発生するため、
長期間安定運転を行うことはできないという問題もあっ
た。In addition, even when an RO membrane device is used as a pretreatment device for the electrodeionization device, calcium leaks from the RO film to generate calcium carbonate scale in the concentration chamber of the electrodeionization device. ,
There was also a problem that stable operation could not be performed for a long time.
【００１０】本発明は上記従来の問題点を解決し、被処
理水中に硬度成分が含まれていても、スケールを発生さ
せることなく、長期間安定に運転することができる電気
脱イオン装置を提供することを目的とする。The present invention solves the above-mentioned conventional problems, and provides an electrodeionization apparatus that can be operated stably for a long period of time without generating scale even if a hardness component is contained in the water to be treated. The purpose is to do.
【００１１】[0011]
【課題を解決するための手段】本発明の電気脱イオン装
置は陰極と陽極との間に、複数のアニオン交換膜とカチ
オン交換膜とを交互に配列して濃縮室と脱塩室とを交互
に形成してなる電気脱イオン装置において、該濃縮室に
バイポーラ膜を設けて、該濃縮室内を陰極側と陽極側と
に区画したことを特徴とする。In the electrodeionization apparatus of the present invention, a plurality of anion exchange membranes and cation exchange membranes are alternately arranged between a cathode and an anode so that a concentration chamber and a desalination chamber are alternately arranged. Wherein a bipolar membrane is provided in the enrichment chamber, and the enrichment chamber is divided into a cathode side and an anode side.
【００１２】本発明の電気脱イオン装置におけるスケー
ル防止機構を説明するに先立ち、まず、従来の電気脱イ
オン装置において、スケールが発生するメカニズムを図
３（ｂ）を参照して説明する。Prior to describing the scale preventing mechanism in the electrodeionization apparatus of the present invention, first, the mechanism of generation of scale in the conventional electrodeionization apparatus will be described with reference to FIG.
【００１３】電気脱イオン装置のスケール発生因子とし
て最も問題となるのが炭酸カルシウムである。電気脱イ
オン装置では、濃縮室の供給水として一般的に被処理水
が分岐して用いられる。この濃縮室内においては、カチ
オン交換膜１４側の脱塩室からカルシウムイオン（Ｃａ
２＋）がイオン交換されて透過し、電気的作用によって
アニオン交換膜１３の表面に近づいてくる。一方、アニ
オン交換膜１３側の脱塩室からは炭酸水素イオン（ＨＣ
Ｏ３ −）が透過し、濃縮室内ではカルシウムイオンと炭
酸イオンによって炭酸カルシウム（ＣａＣＯ３）が形成
される。Calcium carbonate is the most problematic as a scale generating factor in an electrodeionization apparatus. In an electrodeionization apparatus, generally, water to be treated is branched and used as supply water for a concentration chamber. In the concentration chamber, calcium ions (Ca) are supplied from the desalination chamber on the side of the cation exchange membrane 14.
2+ ) are ion-exchanged and permeate, and approach the surface of the anion exchange membrane 13 by an electric action. On the other hand, from the desalting chamber on the side of the anion exchange membrane 13, bicarbonate ions (HC
O 3 − ) permeates, and calcium carbonate (CaCO 3 ) is formed by calcium ions and carbonate ions in the concentration chamber.
【００１４】一般に、炭酸カルシウムの飽和条件は下記
式で表される。 ｌｏｇ［Ｃａ２＋］＋ｌｏｇ［ＨＣＯ３ −］＋ｐＨｓ＝
ｌｏｇ（Ｋｓ／Ｋ２） Ｋｓ：炭酸カルシウムの溶解度積 Ｋ２：炭酸の第２解離定数 ｐＨｓ：炭酸カルシウムの飽和ｐＨ 実際の水溶液中のｐＨと炭酸カルシウムの飽和ｐＨ（ｐ
Ｈｓ）との差はランジェリア指数（ＬＳＩ）と呼ばれ、 ＬＳＩ＝ｐＨ−ｐＨｓ＞０ となると炭酸カルシウムが析出することになる。In general, the condition of saturation of calcium carbonate is expressed by the following equation. log [Ca 2+ ] + log [HCO 3 − ] + pHs =
log (Ks / K 2) Ks : solubility product K 2 calcium carbonate: second dissociation constant pHs carbonate: saturation pH of pH and calcium carbonate saturation pH during the actual aqueous solution of calcium carbonate (p
The difference from Hs) is called the Langerian index (LSI). If LSI = pH−pHs> 0, calcium carbonate will precipitate.
【００１５】電気脱イオン装置の濃縮室内にもアニオン
交換膜１３側から脱塩室内の水解離で発生したＯＨ−イ
オンが透過してくるため、局所的にアルカリ性となって
いる。そのため、アニオン交換膜１３の表面でのＬＳＩ
は正（＞０）となることから、この濃縮室内のアニオン
交換膜１３の近傍、炭酸カルシウムスケールが析出する
ことになる。[0015] OH generated from the concentrated anion exchange membrane 13 side to the indoor water dissociation desalting compartment of an electrodeionization device - the ion comes transmitted, and has a locally alkaline. Therefore, the LSI on the surface of the anion exchange membrane 13
Is positive (> 0), so that calcium carbonate scale is deposited near the anion exchange membrane 13 in the concentration chamber.
【００１６】このような濃縮室内での炭酸カルシウムス
ケールの発生を防止するために、本発明者らは種々研究
を重ねた結果、濃縮室内をバイポーラ膜で区画すること
によってこの問題が解決できることを見出した。The present inventors have conducted various studies in order to prevent the generation of calcium carbonate scale in such a concentration chamber, and as a result, they have found that this problem can be solved by partitioning the concentration chamber with a bipolar membrane. Was.
【００１７】バイポーラ膜とは陽イオン交換膜と陰イオ
ン交換膜とが貼り合わさった構造とされた複合膜の一種
である。バイポーラ膜は、水の電気分解に用いる隔膜と
して、或いは、酸とアルカリの中和生成物である塩の水
溶液から酸とアルカリを再生する際の分離膜等として従
来より広く使用されている公知のイオン交換膜であり、
種々の製造方法が提案されている。The bipolar membrane is a type of composite membrane having a structure in which a cation exchange membrane and an anion exchange membrane are bonded. The bipolar membrane is a known membrane that has been widely used as a separator used for electrolysis of water or as a separation membrane for regenerating acid and alkali from an aqueous solution of a salt that is a neutralization product of acid and alkali. An ion exchange membrane,
Various manufacturing methods have been proposed.
【００１８】本発明においては、このようなバイポーラ
膜を電気脱イオン装置の陽極側にバイポーラ膜のアニオ
ン交換膜面が、陰極側にバイポーラ膜のカチオン交換膜
面が位置するように濃縮室内に設置する。なお、バイポ
ーラ膜内では理論水電解電圧（０．８３Ｖ）以上の電圧
を印加することによって、水解離が発生するので電流は
流れる。このため、バイポーラ膜を濃縮室内に設置する
ことで電気脱イオン装置の脱イオン性能が損なわれるこ
とはない。In the present invention, such a bipolar membrane is placed in the concentration chamber such that the anion exchange membrane surface of the bipolar membrane is located on the anode side of the electrodeionization device and the cation exchange membrane surface of the bipolar membrane is located on the cathode side. I do. In addition, when a voltage higher than the theoretical water electrolysis voltage (0.83 V) is applied in the bipolar membrane, water dissociation occurs, so that current flows. Therefore, the deionization performance of the electrodeionization apparatus is not impaired by installing the bipolar membrane in the concentration chamber.
【００１９】本発明に従って、図１（ｂ）に示す如く、
濃縮室内にバイポーラ膜２０を配置すると、アニオン交
換膜１３側の脱塩室から濃縮室内に透過してきた炭酸水
素イオンと、カチオン交換膜１４側から透過してきたカ
ルシウムイオンとは、それぞれバイポーラ膜２０のカチ
オン交換膜２０Ａとアニオン交換膜２０Ｂにより遮断さ
れるため、濃縮室内で炭酸カルシウムを形成することは
ない。このため、濃縮室内での炭酸カルシウムスケール
の発生は防止される。According to the present invention, as shown in FIG.
When the bipolar membrane 20 is disposed in the enrichment chamber, the bicarbonate ions permeating into the enrichment chamber from the desalting chamber on the anion exchange membrane 13 side and the calcium ions permeating from the cation exchange membrane 14 side respectively Since it is shut off by the cation exchange membrane 20A and the anion exchange membrane 20B, calcium carbonate is not formed in the concentration chamber. Therefore, generation of calcium carbonate scale in the concentration chamber is prevented.
【００２０】しかし、濃縮室内にバイポーラ膜を配置し
た場合であっても、水道水のようにカルシウム濃度の高
い水を処理する場合には、スケールが発生する恐れがあ
るため、この場合には、脱塩室から得られる脱イオン水
の一部を濃縮室に導入して、濃縮室循環水を脱イオン水
で希釈してカルシウム濃度を低減することが好ましい。However, even when a bipolar membrane is disposed in the concentration chamber, scale may be generated when treating water having a high calcium concentration such as tap water. It is preferable that a part of the deionized water obtained from the demineralization chamber is introduced into the concentration chamber, and the circulating water of the concentration chamber is diluted with deionized water to reduce the calcium concentration.
【００２１】本発明の電気脱イオン装置を用いることに
より、従来、用いられてきたＲＯ膜装置による前処理を
行うことなく、安定した脱イオン処理が可能となる。By using the electrodeionization apparatus of the present invention, a stable deionization processing can be performed without performing a pretreatment using a conventionally used RO membrane apparatus.
【００２２】[0022]
【発明の実施の形態】以下に図面を参照して本発明の実
施の形態を詳細に説明する。Embodiments of the present invention will be described below in detail with reference to the drawings.
【００２３】図１は本発明の電気脱イオン装置の実施の
形態を示す構成図、図２は同系統図である。図１におい
て、図３に示す部材と同一機能を奏する部材には同一符
号を付してある。FIG. 1 is a block diagram showing an embodiment of an electrodeionization apparatus of the present invention, and FIG. 2 is a system diagram. 1, members having the same functions as the members shown in FIG. 3 are denoted by the same reference numerals.
【００２４】本発明の電気脱イオン装置は、濃縮室１５
内にバイポーラ膜２０を設けて、濃縮室１５内を陰極側
と陽極側とに区画したこと以外は図３に示す従来の電気
脱イオン装置と同様の構成とされている。The electrodeionization apparatus according to the present invention comprises a concentration chamber 15
The structure is the same as that of the conventional electrodeionization apparatus shown in FIG. 3 except that a bipolar membrane 20 is provided therein and the inside of the concentration chamber 15 is partitioned into a cathode side and an anode side.
【００２５】前述の如く、このバイポーラ膜２０は、陽
極１１側にバイポーラ膜２０のアニオン交換膜２０Ｂ側
が、陰極１２側にバイポーラ膜２０のカチオン交換膜２
０Ａ側が位置するように濃縮室１５内に設置する。As described above, the bipolar membrane 20 has the anion exchange membrane 20B of the bipolar membrane 20 on the anode 11 side and the cation exchange membrane 2 of the bipolar membrane 20 on the cathode 12 side.
It is installed in the concentration chamber 15 so that the 0A side is located.
【００２６】これにより、図１（ｂ）に示す如く、アニ
オン交換膜１３側の脱塩室から透過してきた炭酸水素イ
オンと、カチオン交換膜１４側から透過してきたカルシ
ウムイオンとは、それぞれバイポーラ膜２０のカチオン
交換膜２０Ａとアニオン交換膜２０Ｂにより遮断される
ため、これらが反応することによる炭酸カルシウムのス
ケールの発生は防止される。Thus, as shown in FIG. 1B, the bicarbonate ions permeating from the desalting chamber on the side of the anion exchange membrane 13 and the calcium ions permeating from the side of the cation exchange membrane 14 are each a bipolar membrane. Since the cation exchange membrane 20A and the anion exchange membrane 20B of 20 are cut off, scale reaction of calcium carbonate due to their reaction is prevented.
【００２７】なお、本発明で用いるバイポーラ膜として
は、陰イオン交換層と陽イオン交換層とを有し、水電解
効率が高いものであれば良く、特に制限はない。The bipolar membrane used in the present invention is not particularly limited as long as it has an anion exchange layer and a cation exchange layer and has high water electrolysis efficiency.
【００２８】本発明の電気脱イオン装置は、濃縮室にこ
のようなバイポーラ膜を用いること以外は、従来の電気
脱イオン装置と同様の構成とされ、脱塩室１６内には、
イオン交換繊維もしくはグラフト交換体等からなるアニ
オン交換体及びカチオン交換体を混合もしくは複層状に
充填されていることが、得られる脱イオン水の向上の面
で好ましい。このようなイオン交換体は、濃縮室や電極
室に充填しても良い。The electrodeionization apparatus of the present invention has the same configuration as the conventional electrodeionization apparatus except that such a bipolar membrane is used in the concentration chamber.
It is preferable that anion exchangers and cation exchangers composed of ion exchange fibers or graft exchangers are mixed or filled in a multi-layer form from the viewpoint of improving the obtained deionized water. Such an ion exchanger may be filled in a concentration chamber or an electrode chamber.
【００２９】本発明の電気脱イオン装置では、上述の如
く、濃縮室にバイポーラ膜を設けることで、濃縮室内で
の炭酸カルシウムスケールを有効に防止することができ
るが、この場合においても、水道水のようにカルシウム
濃度の高い水を処理する場合には、スケールが発生する
恐れがある。従って、この場合には、図２に示す如く、
脱塩室３２から得られる脱イオン水の一部を濃縮室３３
に導入して、濃縮室３３の循環水を脱イオン水で希釈し
てカルシウム濃度を低減することが好ましい。同様に電
極室３１内の水についても、脱イオン水を用いることが
好ましい。In the electrodeionization apparatus of the present invention, calcium carbonate scale in the concentration chamber can be effectively prevented by providing a bipolar membrane in the concentration chamber, as described above. When water having a high calcium concentration is treated as described above, scale may be generated. Therefore, in this case, as shown in FIG.
Part of the deionized water obtained from the desalting chamber 32 is concentrated
It is preferable to reduce the calcium concentration by diluting the circulating water in the concentration chamber 33 with deionized water. Similarly, for the water in the electrode chamber 31, it is preferable to use deionized water.
【００３０】また、濃縮室に導入する被処理水のみ軟化
処理するようにしても良く、この場合には、軟化装置が
必要となるが、全ての被処理水を軟化処理する場合に比
べてその処理コストは大幅に低減される。Further, only the water to be treated to be introduced into the concentration chamber may be softened. In this case, a softening device is required. Processing costs are greatly reduced.
【００３１】[0031]
【実施例】以下に比較例及び実施例を挙げて本発明をよ
り具体的に説明する。The present invention will be described more specifically with reference to comparative examples and examples.
【００３２】なお、以下の比較例及び実施例で用いた試
験装置は、下記の装置を活性炭装置、電気脱イオン装置
の順で直列に配置したものである。 活性炭装置 ：栗田工業（株）製「クリコールＫＷ
１０−３０」 電気脱イオン装置：栗田工業（株）製「ピュアエースＰ
Ａ−２００」 処理水量１００Ｌ／ｈｒThe test apparatus used in the following comparative examples and examples was such that the following apparatuses were arranged in series in the order of an activated carbon apparatus and an electrodeionization apparatus. Activated carbon equipment: Kurita Kogyo Co., Ltd. “Crycol KW
10-30 "Electrodeionizer: Kurita Kogyo Co., Ltd." Pure Ace P "
A-200 "Processed water volume 100 L / hr
【００３３】比較例１ 電気脱イオン装置のイオン交換膜及び脱塩室に充填する
イオン交換樹脂として次のものを用い、市水を被処理水
として表１に示す条件で通水を行い、得られた処理水の
導電率、及び濃縮室流量を２５Ｌ／ｈｒで通水したとき
の濃縮室の差圧の経時変化を調べ、結果を表１に示し
た。なお、濃縮室循環水の補給水及び電極室水として
は、被処理水を用いた。 アニオン交換膜： 旭化成工業（株）「アシプレックス
Ａ５０１ＳＢ」 カチオン交換膜： 旭化成工業（株）「アシプレックス
Ｋ５０１ＳＢ」 イオン交換樹脂： アニオン交換樹脂；三菱化学（株）
製「ＳＡ１０Ａ」とカチオン交換樹脂；三菱化学（株）
製「ＳＫ１Ｂ」とを体積混合比率６：４で混合したも
の。Comparative Example 1 The following was used as the ion exchange resin to be filled in the ion exchange membrane and the desalting chamber of the electrodeionization apparatus, and city water was passed under the conditions shown in Table 1 as the water to be treated. The conductivity of the treated water thus obtained and the change over time in the differential pressure of the concentrating chamber when the flow rate of the concentrating chamber was 25 L / hr were examined. The results are shown in Table 1. The water to be treated was used as the replenishing water and the electrode chamber water for the circulating water in the concentration chamber. Anion exchange membrane: “Aciplex A501SB” Asahi Kasei Kogyo Co., Ltd. Cation exchange membrane: “Aciplex K501SB” Asahi Kasei Kogyo Co., Ltd. Ion exchange resin: Anion exchange resin; Mitsubishi Chemical Corporation
"SA10A" and cation exchange resin; Mitsubishi Chemical Corporation
Manufactured by “SK1B” manufactured at a volume mixing ratio of 6: 4.
【００３４】実施例１ 比較例１で用いた電気脱イオン装置の濃縮室にバイポー
ラ膜を設けて図１に示す電気脱イオン装置を組み立て、
この電気脱イオン装置を用いたこと以外は同様にして、
表１に示す通水条件で試験を行い、結果を表１に示し
た。Example 1 A bipolar membrane was provided in the concentration chamber of the electrodeionization apparatus used in Comparative Example 1 to assemble the electrodeionization apparatus shown in FIG.
Except for using this electrodeionization device,
The test was performed under the water flow conditions shown in Table 1, and the results are shown in Table 1.
【００３５】なお、バイポーラ膜としては特許第２５２
４０１２号の実施例１に示された方法、すなわち徳山ソ
ーダ製カチオン交換膜（ＣＭＢ）を塩化第一鉄水溶液に
２５℃で１時間浸漬した後、イオン交換水で十分に洗浄
して、風乾した後、ポリマー被膜法によりカチオン交換
膜表面に４級塩基化したアミノ基を含むポリマーを塗布
して製作したものを用いた。The bipolar film is disclosed in Japanese Patent No. 252
No. 4012, Example 1, that is, a cation exchange membrane (CMB) manufactured by Tokuyama Soda was immersed in an aqueous ferrous chloride solution at 25 ° C. for 1 hour, washed sufficiently with ion-exchanged water, and air-dried. Thereafter, a polymer prepared by applying a polymer containing a quaternary basified amino group to the surface of the cation exchange membrane by a polymer coating method was used.
【００３６】実施例２ 実施例１において、図２に示す如く、被処理水の代りに
脱塩室から得られた脱イオン水の一部（２０％）を濃縮
室循環水の補給水及び電極室水として送給したこと以外
は、同様にして、表１に示す通水条件で試験を行い、結
果を表１に示した。EXAMPLE 2 In Example 1, as shown in FIG. 2, a part (20%) of deionized water obtained from a desalting chamber was replaced with replenishing water and electrode A test was performed in the same manner under the water-passing conditions shown in Table 1 except that the water was supplied as room water, and the results are shown in Table 1.
【００３７】[0037]
【表１】 [Table 1]
【００３８】表１より明らかなように、比較例１の電気
脱イオン装置では１週間で濃縮室側の差圧が上昇してし
まい、運転不能となったが、実施例１、２の電気脱イオ
ン装置では、３ヶ月間安定して運転することができた。
特に実施例２の電気脱イオン装置では、脱イオン水を濃
縮水として循環したことにより、差圧の上昇は殆ど起こ
らなかった。As is clear from Table 1, the operation of the electrodeionization apparatus of Comparative Examples 1 and 2 became inoperable because the differential pressure on the side of the enrichment chamber increased in one week, but the operation of Examples 1 and 2 The ion device was able to operate stably for three months.
In particular, in the electrodeionization apparatus of Example 2, since the deionized water was circulated as the concentrated water, the pressure difference hardly increased.
【００３９】[0039]
【発明の効果】以上詳述した通り、本発明の電気脱イオ
ン装置によれば、水道水のように硬度成分を含む水を処
理する場合においても、濃縮室内での炭酸カルシウムス
ケールの発生を有効に防止することができ、長期間に亘
って安定した運転を継続できる。このため、本発明の電
気脱イオン装置によれば、従来、前処理装置として必要
とされていたＲＯ膜装置を省くことができ、設備コス
ト、処理コストの低減を図ることができる。As described above in detail, according to the electrodeionization apparatus of the present invention, even when water containing a hard component such as tap water is treated, the generation of calcium carbonate scale in the concentration chamber is effective. And stable operation can be continued for a long period of time. For this reason, according to the electrodeionization apparatus of the present invention, the RO membrane apparatus conventionally required as a pretreatment apparatus can be omitted, and equipment costs and processing costs can be reduced.
【図１】本発明の電気脱イオン装置の実施の形態を示す
模式的な断面図である。FIG. 1 is a schematic sectional view showing an embodiment of an electrodeionization apparatus of the present invention.
【図２】本発明の電気脱イオン装置の実施の形態を示す
系統図である。FIG. 2 is a system diagram showing an embodiment of the electrodeionization apparatus of the present invention.
【図３】従来の電気脱イオン装置を示す模式的な断面図
である。FIG. 3 is a schematic sectional view showing a conventional electrodeionization apparatus.
【符号の説明】 １０ イオン交換体 １１ 陽極 １２ 陰極 １３ アニオン交換膜 １４ カチオン交換膜 １５ 濃縮室 １６ 脱塩室 １７ 陽極室 １８ 陰極室 ２０ バイポーラ膜 ２０Ａ カチオン交換膜 ２０Ｂ アニオン交換膜DESCRIPTION OF SYMBOLS 10 Ion exchanger 11 Anode 12 Cathode 13 Anion exchange membrane 14 Cation exchange membrane 15 Concentration chamber 16 Desalination chamber 17 Anode chamber 18 Cathode chamber 20 Bipolar membrane 20A Cation exchange membrane 20B Anion exchange membrane
───────────────────────────────────────────────────── フロントページの続き Ｆターム(参考） 4D006 GA17 HA44 HA47 JA30A JA43A JA70A KA31 KB11 KD19 MA13 MA14 MA15 MC78X PA01 PB05 PB06 PB27 PB28 PC02 4D061 DA02 DA03 DB05 DB13 EA02 EA09 EB01 EB04 EB13 EB19 EB22 FA06 ──────────────────────────────────────────────────続 き Continued on the front page F term (reference) 4D006 GA17 HA44 HA47 JA30A JA43A JA70A KA31 KB11 KD19 MA13 MA14 MA15 MC78X PA01 PB05 PB06 PB27 PB28 PC02 4D061 DA02 DA03 DB05 DB13 EA02 EA09 EB01 EB04 EB13 EB19 EB13 FA
Claims (4)
換膜とカチオン交換膜とを交互に配列して濃縮室と脱塩
室とを交互に形成してなる電気脱イオン装置において、
該濃縮室にバイポーラ膜を設けて、該濃縮室内を陰極側
と陽極側とに区画したことを特徴とする電気脱イオン装
置。An electrodeionization apparatus comprising a plurality of anion exchange membranes and a cation exchange membrane arranged alternately between a cathode and an anode to form a concentration chamber and a desalination chamber alternately.
A bipolar membrane is provided in the concentration chamber, and the concentration chamber is partitioned into a cathode side and an anode side.
アニオン交換層面が陽極側に、カチオン交換層面が陰極
側に位置するように設けられていることを特徴とする電
気脱イオン装置。2. The bipolar film according to claim 1, wherein
An electrodeionization device characterized in that an anion exchange layer surface is provided on an anode side and a cation exchange layer surface is provided on a cathode side.
イオン交換体を充填したことを特徴とする電気脱イオン
装置。3. The electrodeionization apparatus according to claim 1, wherein the deionization chamber is filled with an ion exchanger.
て、該脱塩室の流出水の一部を該濃縮室の流入側へ供給
する流路を設けたことを特徴とする電気脱イオン装置。4. The electrodeionization apparatus according to claim 1, further comprising a flow path for supplying a part of the effluent of the desalting chamber to the inflow side of the enrichment chamber. apparatus.
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| JP2000011989A JP4403621B2 (en) | 2000-01-20 | 2000-01-20 | Electrodeionization equipment |
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|---|---|---|---|
| JP2000011989A JP4403621B2 (en) | 2000-01-20 | 2000-01-20 | Electrodeionization equipment |
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Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003094064A (en) * | 2001-09-27 | 2003-04-02 | Kurita Water Ind Ltd | Electric deionization equipment |
| JP2005296878A (en) * | 2004-04-15 | 2005-10-27 | Hitachi Maxell Ltd | Electrolytic ion water preparation apparatus |
| CN100345615C (en) * | 2005-09-12 | 2007-10-31 | 张贵清 | Electric deionisation method and apparatus for producing superpure water using bipolar membrane |
| WO2008016055A1 (en) * | 2006-08-02 | 2008-02-07 | Kurita Water Industries Ltd. | Electrodeionizer |
| WO2008016054A1 (en) * | 2006-07-31 | 2008-02-07 | Kurita Water Industries Ltd. | Electric deionization apparatus |
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| JP2014509694A (en) * | 2011-03-29 | 2014-04-21 | インドゥストリエ・デ・ノラ・ソチエタ・ペル・アツィオーニ | Cell for depolarization electrodialysis of salt solution |
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| JP2003094064A (en) * | 2001-09-27 | 2003-04-02 | Kurita Water Ind Ltd | Electric deionization equipment |
| JP2005296878A (en) * | 2004-04-15 | 2005-10-27 | Hitachi Maxell Ltd | Electrolytic ion water preparation apparatus |
| CN100345615C (en) * | 2005-09-12 | 2007-10-31 | 张贵清 | Electric deionisation method and apparatus for producing superpure water using bipolar membrane |
| WO2008016054A1 (en) * | 2006-07-31 | 2008-02-07 | Kurita Water Industries Ltd. | Electric deionization apparatus |
| US8628653B2 (en) | 2006-08-02 | 2014-01-14 | Kurita Water Industries Ltd. | Electrodeionization apparatus |
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| CN101541686B (en) * | 2006-08-02 | 2012-11-07 | 栗田工业株式会社 | Electrodeionizer |
| JP2008068198A (en) * | 2006-09-14 | 2008-03-27 | Kurita Water Ind Ltd | Electrodeionization apparatus |
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| JP2011139980A (en) * | 2010-01-06 | 2011-07-21 | Japan Organo Co Ltd | Electric deionized water producing apparatus and method of producing deionized water |
| JP2012125738A (en) * | 2010-12-17 | 2012-07-05 | Kurita Water Ind Ltd | Pure water production apparatus |
| JP2014509694A (en) * | 2011-03-29 | 2014-04-21 | インドゥストリエ・デ・ノラ・ソチエタ・ペル・アツィオーニ | Cell for depolarization electrodialysis of salt solution |
| JP2012239966A (en) * | 2011-05-18 | 2012-12-10 | Japan Organo Co Ltd | Electric deionized water producing apparatus |
| CN102838240A (en) * | 2012-09-28 | 2012-12-26 | 武汉大学 | Method and system for recovering waste water generated in carbocisteine production |
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