JP2001314865A - Method of preparing pure water - Google Patents
Method of preparing pure waterInfo
- Publication number
- JP2001314865A JP2001314865A JP2000136040A JP2000136040A JP2001314865A JP 2001314865 A JP2001314865 A JP 2001314865A JP 2000136040 A JP2000136040 A JP 2000136040A JP 2000136040 A JP2000136040 A JP 2000136040A JP 2001314865 A JP2001314865 A JP 2001314865A
- Authority
- JP
- Japan
- Prior art keywords
- water
- concentration
- electrodeionization
- electrodeionization apparatus
- pure water
- 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
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
-
- 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
- Y02A20/131—Reverse-osmosis
Landscapes
- Water Treatment By Electricity Or Magnetism (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、半導体、液晶、製
薬、食品、電力等の分野の各種産業、民生用、又は研究
設備で利用される脱イオン水を、電気脱イオン装置を用
いて製造する方法に係り、特に純水製造用の電気脱イオ
ン装置でのスケール発生を防止して長期に亘り安定かつ
効率的に純水を製造する方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to the production of deionized water used in various industries in the fields of semiconductors, liquid crystals, pharmaceuticals, foods, electric power, etc., for consumer use, or in research facilities using an electrodeionization apparatus. More particularly, the present invention relates to a method for stably and efficiently producing pure water for a long period of time by preventing generation of scale in an electrodeionization apparatus for producing pure water.
【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１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１
４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１７８２９４３
号、特許第２７５１０９０号、特許第２６９９２５６
号）。なお、図１において、１７は陽極室、１８は陰極
室である。2. Description of the Related Art Conventionally, semiconductor manufacturing plants, liquid crystal manufacturing plants,
In 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, as shown in FIG.
A plurality of anion exchange membranes 13 and cation exchange membranes 1
4 are alternately arranged to form a concentration chamber 15 and a desalination chamber 16 alternately, and an anion exchanger and a cation exchanger composed of an ion exchange resin, an ion exchange fiber or a graft exchanger are mixed in the desalination chamber 16. Alternatively, a multi-layered electrodeionization apparatus is often used (Japanese Patent No. 1782943).
Patent No. 2,751,090, Patent No. 2,699,256
issue). In FIG. 1, reference numeral 17 denotes an anode chamber, and 18 denotes 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】一方で、電気脱イオン装置では、濃縮室に
おいて炭酸カルシウムを主体としたスケールが析出し、
濃縮室が閉塞して連続運転が困難になるというトラブル
が発生している。On the other hand, in the electrodeionization apparatus, a scale mainly composed of calcium carbonate precipitates in the concentration chamber,
There is a problem that the concentrating chamber is closed and continuous operation becomes difficult.
【０００５】従来、一般に、炭酸カルシウム由来のスケ
ール析出の有無の判定には、ランジェリア指数が用いら
れるが、上述のように電気脱イオン装置内では水解離が
生じており、局所的にアルカリ部分が生じていることよ
り、ランジェリア指数をスケール析出の指標とすること
ができなかった。また、ＣＯ２、シリカ、ホウ素等の弱
イオン性物質を除去するために、高電流を流す電気脱イ
オン装置では、微量のＣａ、無機炭酸（以下「ＩＣ」と
呼ぶ。）濃度下でもスケールが発生してしまい、その都
度、ＨＣｌなどの酸洗浄を実施する必要があった。Conventionally, the Lingeria index is generally used to determine the presence or absence of scale precipitation derived from calcium carbonate. However, as described above, water dissociation occurs in the electrodeionization apparatus, and the alkali portion is locally localized. Because of the occurrence of, the Langerian index could not be used as an index of scale precipitation. In addition, in an electrodeionization apparatus in which a high current is applied to remove weakly ionic substances such as CO 2 , silica, and boron, the scale can be reduced even under a small amount of Ca or inorganic carbonic acid (hereinafter referred to as “IC”). In each case, acid cleaning with HCl or the like had to be performed.
【０００６】また、従来においては、炭酸カルシウム発
生の指標が明確になっていないため、電気脱イオン装置
の前処理に過剰な軟化装置や脱ガス装置を設置せざるを
得ない場合もあった。[0006] Conventionally, since the index of calcium carbonate generation has not been clarified, an excessive softening device or degassing device has to be installed in the pretreatment of the electrodeionization device in some cases.
【０００７】[0007]
【発明が解決しようとする課題】本発明は、上記従来の
問題点を解決し、電気脱イオン装置を用いて純水を製造
するに当り、炭酸カルシウム発生の指標を明確にするこ
とにより、電気脱イオン装置におけるスケールの発生を
確実に防止して、長期安定運転を可能とする純水の製造
方法を提供することを目的とする。DISCLOSURE OF THE INVENTION The present invention solves the above-mentioned conventional problems and, when producing pure water using an electrodeionization apparatus, clarifies the index of calcium carbonate generation, thereby reducing the electricity consumption. It is an object of the present invention to provide a method for producing pure water that reliably prevents generation of scale in a deionization device and enables long-term stable operation.
【０００８】[0008]
【課題を解決するための手段】本発明の純水の製造方法
は、陽極と陰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を用い、原水を該電気脱
イオン装置の脱塩室に導入し、該脱塩室の流出水を処理
水として取り出す純水の製造方法において、下記式で算
出されるスケール指標数値ＳＩが２００以下となる条件
で該電気脱イオン装置を運転することを特徴とする。According to the method for producing pure water of the present invention, a plurality of anion exchange membranes and cation exchange membranes are alternately arranged between an anode and a cathode to form a concentration chamber and a desalination chamber. Using an electrodeionization apparatus formed alternately, raw water is introduced into a desalination chamber of the electrodeionization apparatus, and a method for producing pure water in which effluent from the deionization chamber is taken out as treated water is represented by the following formula: The electrodeionization apparatus is operated under the condition that the calculated scale index value SI is 200 or less.
【０００９】スケール指標数値ＳＩ＝ＩＣ膜面積負荷量
（ｍｇ−ＣＯ２／ｈｒ・ｄｍ２）×濃縮水Ｃａ濃度（ｍ
ｇ−ＣａＣＯ３／Ｌ） （ただし、ＩＣ膜面積負荷量（ｍｇ−ＣＯ２／ｈｒ・ｄ
ｍ２）は、該電気脱イオン装置のアニオン交換膜面積
（ｄｍ２）当たりのＩＣ負荷量（ｍｇ−ＣＯ２／ｈｒ）
であり、濃縮水Ｃａ濃度は濃縮室流出水のＣａ濃度（Ｃ
ａＣＯ３換算）である。）Scale index value SI = IC membrane area load (mg-CO 2 / hr · dm 2 ) × concentrated water Ca concentration (m
g-CaCO 3 / L) (However, IC membrane area load (mg-CO 2 / hr · d)
m 2 ) is the IC load (mg-CO 2 / hr) per anion exchange membrane area (dm 2 ) of the electrodeionization apparatus.
And the Ca concentration of the concentrated water is the Ca concentration (C
aCO 3 conversion). )
【００１０】本発明者らは、電気脱イオン装置における
スケール発生のメカニズムを明らかにするために、電気
脱イオン装置の供給水に過剰量のＩＣ及びＣａを混在さ
せて、意図的にスケールを発生させた後、装置を解体し
て濃縮室を観察した結果、濃縮室面側のアニオン交換膜
に炭酸カルシウムが付着していることを知見した。In order to clarify the mechanism of scale generation in the electrodeionization apparatus, the present inventors intentionally generate scale by mixing an excessive amount of IC and Ca in the water supplied to the electrodeionization apparatus. After that, the apparatus was disassembled and the concentration chamber was observed. As a result, it was found that calcium carbonate had adhered to the anion exchange membrane on the side of the concentration chamber.
【００１１】この知見から、本発明者らは、スケール発
生のメカニズムを次のように推定した。即ち、図２に示
す如く、アニオン交換膜１３面は局所的にアルカリにな
り、脱塩室１６からアニオン交換膜１３を透過してくる
ＨＣＯ３ −もしくはＣＯ３ ２ −及びＯＨ−はアニオン交
換膜１３付近で濃縮されており、そこへ濃縮室１５内の
水に含まれるＣａがアニオン交換膜１３面へ引き寄せら
れ、これらが反応して炭酸カルシウムのスケール２０が
アニオン交換膜１３面に発生する。Based on this finding, the present inventors estimated the mechanism of scale generation as follows. That is, as shown in FIG. 2, the anion exchange membrane 13 surface becomes locally alkali, HCO coming through the anion exchange membrane 13 from the desalting compartments 16 3 - or CO 3 2 - and OH - anion exchange membrane 13, Ca contained in the water in the concentration chamber 15 is attracted to the surface of the anion exchange membrane 13, which reacts to generate calcium carbonate scale 20 on the surface of the anion exchange membrane 13.
【００１２】そこで、本発明者らは更に研究を進めてい
き、アニオン交換膜のＩＣ膜面積負荷量と濃縮水のＣａ
濃度を掛け合わせた下記数値（スケール指標数値ＳＩ）
を設定値以下とすればスケールが全く発生しないことを
見出し、本発明を完成させた。Therefore, the present inventors have further studied and found that the area load on the IC membrane of the anion exchange membrane and the Ca concentration of the concentrated water
Multiplied by the following values (scale index value SI)
It was found that no scale was generated when the value was less than the set value, and the present invention was completed.
【００１３】スケール指標数値ＳＩ＝ＩＣ膜面積負荷量
（ｍｇ−ＣＯ２／ｈｒ・ｄｍ２）×濃縮水Ｃａ濃度（ｍ
ｇ−ＣａＣＯ３／Ｌ） （ただし、ＩＣ膜面積負荷量（ｍｇ−ＣＯ２／ｈｒ・ｄ
ｍ２）は、該電気脱イオン装置のアニオン交換膜面積
（ｄｍ２）当たりのＩＣ負荷量（ｍｇ−ＣＯ２／ｈｒ）
であり、濃縮水Ｃａ濃度は濃縮室流出水のＣａＣＯ３換
算のＣａ濃度である。） 電気脱イオン装置のＩＣ負荷量（ｍｇ−ＣＯ２／ｈｒ）
は、電気脱イオン装置の供給水のＩＣ濃度（ｍｇ−ＣＯ
２／Ｌ）に流量（Ｌ／ｈｒ）を掛けることにより求めら
れ、従って、ＩＣ膜面積負荷量（ｍｇ−ＣＯ２／ｈｒ・
ｄｍ２）は、 供給水のＩＣ濃度（ｍｇ−ＣＯ２／Ｌ）×セル当たりの
流量（Ｌ／ｈｒ）÷セル有効アニオン交換膜面積（ｄｍ
２） で算出される。Scale index value SI = IC membrane area load (mg-CO 2 / hr · dm 2 ) × concentrated water Ca concentration (m
g-CaCO 3 / L) (However, IC membrane area load (mg-CO 2 / hr · d)
m 2 ) is the IC load (mg-CO 2 / hr) per anion exchange membrane area (dm 2 ) of the electrodeionization apparatus.
And the Ca concentration of the concentrated water is the Ca concentration in terms of CaCO 3 in the effluent of the concentration chamber. ) IC load of the electrodeionization device (mg-CO 2 / hr)
Is the IC concentration of the feed water of the electrodeionization device (mg-CO
2 / L) multiplied by the flow rate (L / hr). Therefore, the IC membrane area load (mg-CO 2 / hr ·
dm 2 ) is the IC concentration of the feed water (mg-CO 2 / L) × the flow rate per cell (L / hr) ÷ the cell effective anion exchange membrane area (dm
2 ) It is calculated by.
【００１４】このように電気脱イオン装置のスケール発
生因子の指標としてのスケール指標数値ＳＩを規定値以
下にすることにより、電気脱イオン装置の濃縮室内での
炭酸カルシウムスケールの析出を確実に防止することが
でき、該電気脱イオン装置を長期間に亘って安定に運転
することが可能となる。By setting the scale index value SI as an index of the scale generation factor of the electrodeionization apparatus to a specified value or less, the precipitation of calcium carbonate scale in the concentration chamber of the electrodeionization apparatus is reliably prevented. The electrodeionization apparatus can be operated stably for a long period of time.
【００１５】ところで、電気脱イオン装置では前述のよ
うに供給水のイオンを排出させるのに必要な理論電流値
以上の電流を流して、脱塩室内で水解離を生じさせて、
イオン交換体を連続的に再生している。従って、電流を
流すほどアニオン交換膜面のｐＨはアルカリ性になり、
炭酸カルシウムは析出し易くなる。そのため、許容ＳＩ
値は電流値によって変化する。By the way, in the electrodeionization apparatus, as described above, a current larger than a theoretical current value required for discharging ions of the supplied water is caused to flow to cause water dissociation in the deionization chamber.
The ion exchanger is continuously regenerated. Therefore, the more the current flows, the more alkaline the pH of the anion exchange membrane surface becomes,
Calcium carbonate tends to precipitate. Therefore, the allowable SI
The value changes depending on the current value.
【００１６】通常、処理水比抵抗値１０ＭΩ・ｃｍ程度
を達成すればよい電気脱イオン装置で、９０％以上の高
シリカ除去率が要求されない場合、又は２０％を超える
電流効率で運転するような場合には、ＳＩ値が２００以
下になるようにすればよく、好ましくは１５０以下であ
る。特に、経済的な考慮からは、必要以上の脱ガス装置
や軟化装置による処理を避けるために、ＳＩ値を８０〜
２００とするのが望ましい。Usually, an electrodeionization apparatus which only needs to achieve a treated water specific resistance value of about 10 MΩ · cm is used, when a high silica removal rate of 90% or more is not required, or when it is operated at a current efficiency exceeding 20%. In such a case, the SI value may be set to 200 or less, preferably 150 or less. In particular, from economic considerations, in order to avoid unnecessary treatment with a degassing device or a softening device, an SI value of 80 to 80 is used.
It is desirable to be 200.
【００１７】一方、電気脱イオン装置がシリカ除去率９
０％以上を要求される場合、即ち電流効率を２０％以下
で運転する場合は、ＳＩ値は１２０以下、特に８０以下
で運転することが好ましい。経済的にはＳＩ値を５０〜
１２０で運転するのが望ましい。On the other hand, the electrodeionization apparatus has a silica removal rate of 9%.
When 0% or more is required, that is, when operating at a current efficiency of 20% or less, it is preferable to operate with an SI value of 120 or less, particularly 80 or less. Economically, SI value should be 50 ~
It is desirable to drive at 120.
【００１８】また、濃縮室にイオン交換体を充填した電
気脱イオン装置の場合には、アニオン交換膜を透過した
ＯＨ−イオンが濃縮室内を移動し易くなるため、スケー
ル層が分散する効果がある。この場合、ＳＩ値は電流値
を増加させても８０以上で運転が可能であり、８０〜２
００で運転を行うことができる。この場合の特に好まし
いＳＩ値は８０〜１５０であるが、経済的な考慮を除け
ば８０以下であっても良い。[0018] In the case of electrodeionization apparatus filled with ion exchanger in the concentrating compartment, OH passed through the anion exchange membrane - the ion tends to move the concentrated compartment, the effect of the scale layer is dispersed . In this case, the operation can be performed at an SI value of 80 or more even when the current value is increased.
The operation can be performed at 00. The particularly preferred SI value in this case is 80 to 150, but may be 80 or less except for economic considerations.
【００１９】本発明において、ＳＩ値を規定値以下にま
で低下させるためには、次のような方法がある。即ち、
濃縮水のＣａ濃度を低下させるためには、水回収率を下
げたり、濃縮室に軟化装置等のＣａ除去装置を設けてＣ
ａを除去する方法がある。また、ＩＣ膜面積負荷量を低
下させるためには、電気脱イオン装置の処理水量を低下
させたり、電気脱イオン装置の上流側に脱ガス装置を設
けてＩＣを除去する方法がある。更に、電気脱イオン装
置の電流値を制御することによってもＩＣ膜面積負荷量
を低下させることができる。In the present invention, there are the following methods for lowering the SI value to a specified value or less. That is,
In order to reduce the Ca concentration of the concentrated water, the water recovery rate may be reduced, or a Ca removal device such as a softening device may be provided in the concentration chamber to reduce the C concentration.
There is a method of removing a. In order to reduce the IC membrane area load, there are methods of reducing the amount of treated water in the electrodeionization apparatus and providing a degassing apparatus upstream of the electrodeionization apparatus to remove the IC. Furthermore, the IC membrane area load can be reduced by controlling the current value of the electrodeionization device.
【００２０】本発明の方法は、原水（供給水）のＩＣ濃
度及び濃縮水のＣａ濃度をモニタリングし、自動演算装
置等を用いてスケール指標数値ＳＩを算出し、このＩＣ
値が所定値以下となるように、下記〜の１又は２以
上を制御することが好ましく、これにより、電気脱イオ
ン装置の自動運転を行って、長期に亘りスケールの析出
を防止して安定に純水を製造することが可能となる。According to the method of the present invention, the IC concentration of raw water (supply water) and the Ca concentration of concentrated water are monitored, and a scale index value SI is calculated using an automatic arithmetic unit or the like.
It is preferable to control 1 or 2 or more of the following so that the value is equal to or less than a predetermined value, whereby the automatic operation of the electrodeionization device is performed, and the precipitation of scale is prevented over a long period of time to stably perform the operation. It becomes possible to produce pure water.
【００２１】 電気脱イオン装置の水回収率 濃縮室流入水のＣａ除去装置を設けた場合の該Ｃａ
除去装置のＣａ除去量 電気脱イオン装置の処理水量 電気脱イオン装置の電流値Water recovery rate of the electrodeionization device The Ca in the case where a Ca removal device for the inflow water of the concentration chamber is provided
The amount of Ca removed by the removal device The amount of water treated by the electrodeionization device The current value of the electrodeionization device
【００２２】[0022]
【発明の実施の形態】以下に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.
【００２３】本発明の純水の製造方法は、前述のスケー
ル指標数値ＳＩ値が規定値以下となるように処理を行う
こと以外は、常法に従って純水の製造を行うことができ
る。According to the method for producing pure water of the present invention, pure water can be produced according to a conventional method, except that the treatment is carried out so that the above-mentioned scale index value SI value is not more than a specified value.
【００２４】従って、原水（この水は、通常、活性炭塔
及び逆浸透膜分離装置で順次前処理される。）の一部を
電気脱イオン装置の濃縮室に供給し、残部を脱塩室に供
給して脱イオン処理し、脱塩室の流出水を処理水（生産
水）として取り出せば良い。なお、通常の場合、濃縮室
の流出水は一部が系外に排出され、残部は濃縮室の供給
側へ循環される。Therefore, part of the raw water (this water is usually pretreated in an activated carbon tower and a reverse osmosis membrane separator in sequence) is supplied to the concentration chamber of the electrodeionization apparatus, and the remainder is supplied to the desalination chamber. It may be supplied and deionized, and the effluent from the desalination chamber may be taken out as treated water (produced water). In a normal case, a part of the effluent from the concentration chamber is discharged out of the system, and the remaining part is circulated to the supply side of the concentration chamber.
【００２５】なお、濃縮室の流出水の循環は、水回収率
の向上のために行われるが、この循環水量は上記スケー
ル指標数値ＳＩ値が本発明の規定値以下であれば良く、
特に制限はないが、通常、濃縮室の流出水の５０〜９５
％程度とし、電気脱イオン装置の水回収率は０．５〜
０．９５程度の条件で運転を実施するのが好ましい。The effluent from the concentrating chamber is circulated to improve the water recovery rate. The amount of circulated water may be any value as long as the above-mentioned scale index value SI value is equal to or less than the specified value of the present invention.
Although there is no particular limitation, usually 50 to 95 effluents of the concentration chamber are used.
%, And the water recovery rate of the electrodeionization device is 0.5 ~
It is preferable to operate under conditions of about 0.95.
【００２６】本発明において用いる電気脱イオン装置
は、複数のアニオン交換膜及びカチオン交換膜を交互に
配列して濃縮室と脱塩室とを交互に形成した一般的なも
のであり、脱塩室にアニオン交換樹脂とカチオン交換樹
脂との混合樹脂が充填されたものであっても、充填され
ていないものであっても良いが、処理水（生産水）の水
質の向上の面からは、脱塩室にアニオン交換樹脂とカチ
オン交換樹脂の混合樹脂が充填されているものが好まし
い。The electrodeionization apparatus used in the present invention is a general one in which a plurality of anion exchange membranes and cation exchange membranes are alternately arranged to form a concentration chamber and a desalination chamber alternately. May or may not be filled with a mixed resin of an anion exchange resin and a cation exchange resin. However, from the viewpoint of improving the quality of treated water (production water), It is preferable that the salt chamber is filled with a mixed resin of an anion exchange resin and a cation exchange resin.
【００２７】また、濃縮室にこのようなイオン交換体を
充填した場合には、スケール指標数値ＳＩ値が高い範囲
であってもスケール発生の問題なく、運転することがで
きる。この場合濃縮室に充填するイオン交換体として
は、特に限定はしないが、粒子状のイオン交換樹脂が好
ましい。When the concentration chamber is filled with such an ion exchanger, even if the scale index value SI is in a high range, the operation can be performed without a problem of scale generation. In this case, the ion exchanger filled in the concentration chamber is not particularly limited, but a particulate ion exchange resin is preferable.
【００２８】[0028]
【実施例】以下に実施例及び比較例を挙げて本発明の効
果をより具体的に説明する。The effects of the present invention will be more specifically described below with reference to examples and comparative examples.
【００２９】なお、以下の実施例及び比較例で用いた試
験装置は、下記の装置を図３に示すように配置したもの
であり、更に電気脱イオン装置の供給水ＩＣ及びＣａ濃
度を調整するために薬注装置４を設置した。The test apparatus used in the following examples and comparative examples is one in which the following apparatuses are arranged as shown in FIG. 3, and further adjusts the feed water IC and the Ca concentration of the electrodeionization apparatus. Injection device 4 was installed for this purpose.
【００３０】 活性炭装置１：栗田工業（株）製「クリコールＫＷ１０−３０」 逆浸透膜装置２：栗田工業（株）製「膜エースＫＮ２００」 電気脱イオン装置３：栗田工業（株）製「ピュアエースＰＡ−２００」 処理量：１００Ｌ／ｈｒ 上記電気脱イオン装置には、下記の電気脱イオンスタッ
クを製作して設置した。 （電気脱イオンスタック）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、図１に示す構成の電気脱イオンスタックを組
み立てた。Activated carbon device 1: "Crycol KW10-30" manufactured by Kurita Kogyo Co., Ltd. Reverse osmosis membrane device 2: "Membrane Ace KN200" manufactured by Kurita Kogyo Co., Ltd. Electrodeionization device 3: "Pure" manufactured by Kurita Kogyo Co., Ltd. ACE PA-200 "Processing amount: 100 L / hr The following electrodeionization stack was manufactured and installed in the above electrodeionization apparatus. (Electrodeionization Stack) 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 an electrodeionization stack having the structure shown in FIG.
【００３１】アニオン交換膜：（株）トクヤマ製「ネオ
セプタＡＨＡ」 カチオン交換膜：（株）トクヤマ製「ネオセプタＣＭ
Ｂ」 陰イオン交換樹脂：三菱化学（株）製「ＳＡ１０Ａ」 陽イオン交換樹脂：三菱化学（株）製「ＳＫ１Ｂ」 陽、陰イオン交換樹脂体積混合比率：４対６ （陰、陽イオン交換樹脂は超純水で十分に洗浄したもの
を用いた。） セル１枚当たりのアニオン、カチオン交換膜の膜面積は
５ｄｍ２であり、セル枚数は１０枚とした。Anion exchange membrane: "Neoceptor AHA" manufactured by Tokuyama Corporation Cation exchange membrane: "Neoceptor CM" manufactured by Tokuyama Corporation
B "Anion exchange resin:" SA10A "manufactured by Mitsubishi Chemical Corporation Cation exchange resin:" SK1B "manufactured by Mitsubishi Chemical Corporation Volume mixing ratio of cation and anion exchange resin: 4 to 6 (anion and cation exchange resin Used was sufficiently washed with ultrapure water.) The membrane area of the anion / cation exchange membrane per cell was 5 dm 2 , and the number of cells was 10.
【００３２】また、測定器としては以下のものを用い
た。The following measuring instruments were used.
【００３３】供給水のＩＣ測定……ＳＩＶＥＲＳ ＩＮ
ＳＴＲＵＭＥＮＴＳ社製「ＴＯＣ８１０（ＩＣ測定モー
ド）」 濃縮水のＣａ測定……ＨＡＣＨ社製「ＡＰＡ６０００
５１００２型」[0033] IC measurement of feed water ... SIVERS IN
"TOC810 (IC measurement mode)" manufactured by STRUMENTS Inc. Ca measurement of concentrated water ... "APA6000" manufactured by HACH
51002 type "
【００３４】実施例１ 電気脱イオン装置の運転条件を表１に示す通り種々変
え、このときのスケール指標数値ＳＩ値とスケール発生
の有無との関係を調べ、結果を表１に示した。Example 1 The operation conditions of the electrodeionization apparatus were variously changed as shown in Table 1. At this time, the relationship between the scale index value SI value and the presence or absence of scale generation was examined. The results are shown in Table 1.
【００３５】なお、Ｎｏ．５においては、電気脱イオン
装置の濃縮室にイオン交換体として脱塩室と同じイオン
交換樹脂を同じ比率で充填した。No. In No. 5, the same ion exchange resin as that of the deionization chamber was filled in the same ratio as the ion exchanger in the concentration chamber of the electrodeionization apparatus.
【００３６】[0036]
【表１】 [Table 1]
【００３７】表１より明らかなように、本発明の規定値
を超えるＳＩ値で運転した場合にはスケールの発生が認
められるが、本発明の規定値以下のＳＩ値で運転した場
合には、スケールの発生は認められなかった。As is clear from Table 1, when an SI value exceeding the specified value of the present invention is operated, scale is observed. However, when operating at an SI value equal to or less than the specified value of the present invention, scale is generated. No scale development was observed.
【００３８】なお、シリカ除去率９０％以上の条件にお
いては、ＳＩ値は１２０以下にする必要があるが、濃縮
室にイオン交換体を充填することにより、ＳＩ値１３０
以上でもスケールの発生は防止された。It is to be noted that under the condition of a silica removal rate of 90% or more, the SI value needs to be 120 or less.
Thus, generation of scale was prevented.
【００３９】[0039]
【発明の効果】以上詳述した通り、本発明の純水の製造
方法によれば、過剰な前処理手段や付加設備を必要とす
ることなく、電気脱イオン装置の濃縮室におけるスケー
ルの発生を確実に防止して、長期に亘り安定かつ効率的
な純水の製造を行うことができる。As described above in detail, according to the method for producing pure water of the present invention, generation of scale in the concentration chamber of the electrodeionization apparatus can be achieved without requiring excessive pretreatment means or additional equipment. Prevention can be reliably performed, and stable and efficient production of pure water can be performed over a long period of time.
【図１】電気脱イオン装置の一般的な構成を示す模式的
な断面図である。FIG. 1 is a schematic sectional view showing a general configuration of an electrodeionization apparatus.
【図２】電気脱イオン装置におけるイオンの移動状況を
説明する模式図である。FIG. 2 is a schematic diagram illustrating the movement of ions in the electrodeionization apparatus.
【図３】実施例で用いた試験装置を示す系統図である。FIG. 3 is a system diagram showing a test apparatus used in an example.
１ 活性炭装置 ２ 逆浸透膜装置 ３ 電気脱イオン装置 ４ 薬注装置 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 DESCRIPTION OF SYMBOLS 1 Activated carbon apparatus 2 Reverse osmosis membrane apparatus 3 Electrodeionization apparatus 4 Chemical injection apparatus 10 Ion exchanger 11 Anode 12 Cathode 13 Anion exchange membrane 14 Cation exchange membrane 15 Concentration room 16 Demineralization room 17 Anode room 18 Cathode room
───────────────────────────────────────────────────── フロントページの続き Ｆターム(参考） 4D006 GA03 GA17 HA47 JA30A JA43A JA44A KA02 KA72 KB11 KB12 KD19 PB06 PB23 PB27 PB28 4D061 DA03 DB13 EA09 EB13 FA06 FA09 ──────────────────────────────────────────────────続 き Continued on the front page F term (reference) 4D006 GA03 GA17 HA47 JA30A JA43A JA44A KA02 KA72 KB11 KB12 KD19 PB06 PB23 PB27 PB28 4D061 DA03 DB13 EA09 EB13 FA06 FA09
Claims (4)
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を用い、原水
を該電気脱イオン装置の脱塩室に導入し、該脱塩室の流
出水を処理水として取り出す純水の製造方法において、
下記式で算出されるスケール指標数値ＳＩが２００以下
となる条件で該電気脱イオン装置を運転することを特徴
とする純水の製造方法。 スケール指標数値ＳＩ＝ＩＣ膜面積負荷量（ｍｇ−ＣＯ
２／ｈｒ・ｄｍ２）×濃縮水Ｃａ濃度（ｍｇ−ＣａＣＯ
３／Ｌ） （ただし、ＩＣ膜面積負荷量（ｍｇ−ＣＯ２／ｈｒ・ｄ
ｍ２）は、該電気脱イオン装置のアニオン交換膜面積
（ｄｍ２）当たりの無機炭酸負荷量（ｍｇ−ＣＯ２／ｈ
ｒ）であり、濃縮水Ｃａ濃度は濃縮室流出水のＣａ濃度
（ＣａＣＯ３換算）である。）1. An electrodeionization apparatus comprising a plurality of anion exchange membranes and cation exchange membranes arranged alternately between an anode and a cathode to alternately form a concentration chamber and a desalination chamber. Is introduced into a desalination chamber of the electrodeionization apparatus, and a method for producing pure water in which effluent from the desalination chamber is taken out as treated water,
A method for producing pure water, wherein the electrodeionization apparatus is operated under the condition that a scale index value SI calculated by the following equation is 200 or less. Scale index value SI = IC film area load (mg-CO
2 / hr · dm 2 ) × concentrated water Ca concentration (mg-CaCO 2 )
3 / L) (However, the IC membrane area load (mg-CO 2 / hr · d)
m 2 ) is the inorganic carbon dioxide load (mg-CO 2 / h) per anion exchange membrane area (dm 2 ) of the electrodeionization apparatus.
r), and the Ca concentration of the concentrated water is the Ca concentration (CaCO 3 conversion) of the effluent of the concentration chamber. )
値ＳＩが１２０以下で、シリカ除去率が９０％以上とな
る条件で該電気脱イオン装置を運転することを特徴とす
る純水の製造方法。2. The method for producing pure water according to claim 1, wherein the electrodeionization apparatus is operated under the condition that the scale index value SI is 120 or less and the silica removal rate is 90% or more.
の濃縮室内にイオン交換体が充填されており、前記スケ
ール指標数値ＳＩが８０〜２００となる条件で該電気脱
イオン装置を運転することを特徴とする純水の製造方
法。3. The electrodeionization apparatus according to claim 1, wherein the concentration chamber of the electrodeionization apparatus is filled with an ion exchanger, and the scale index value SI is 80 to 200. A method for producing pure water.
て、原水の無機炭酸濃度及び濃縮水のＣａ濃度を測定
し、スケール指標数値ＳＩが所定値以下となるように、
下記〜の１又は２以上を制御することを特徴とする
純水の製造方法。 電気脱イオン装置の水回収率 濃縮室流入水のＣａ除去装置を設けた場合の該Ｃａ
除去装置のＣａ除去量 電気脱イオン装置の処理水量 電気脱イオン装置の電流値4. The method according to claim 1, wherein the inorganic carbon concentration of the raw water and the Ca concentration of the concentrated water are measured, and the scale index value SI is equal to or less than a predetermined value.
A method for producing pure water, comprising controlling one or more of the following: Water recovery rate of electrodeionization equipment
The amount of Ca removed by the removal device The amount of water treated by the electrodeionization device The current value of the electrodeionization device
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|---|---|---|---|
| JP2000136040A JP3620406B2 (en) | 2000-05-09 | 2000-05-09 | Pure water production method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000136040A JP3620406B2 (en) | 2000-05-09 | 2000-05-09 | Pure water production method |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003326267A (en) * | 2002-05-09 | 2003-11-18 | Kurita Water Ind Ltd | Operation method for electric deionizer |
| JP2003326266A (en) * | 2002-05-08 | 2003-11-18 | Kurita Water Ind Ltd | Method and apparatus for producing pure water, and scale monitor |
| JP2011041940A (en) * | 2009-08-20 | 2011-03-03 | Samsung Electronics Co Ltd | Capacitive deionization device |
-
2000
- 2000-05-09 JP JP2000136040A patent/JP3620406B2/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003326266A (en) * | 2002-05-08 | 2003-11-18 | Kurita Water Ind Ltd | Method and apparatus for producing pure water, and scale monitor |
| JP2003326267A (en) * | 2002-05-09 | 2003-11-18 | Kurita Water Ind Ltd | Operation method for electric deionizer |
| JP2011041940A (en) * | 2009-08-20 | 2011-03-03 | Samsung Electronics Co Ltd | Capacitive deionization device |
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| Publication number | Publication date |
|---|---|
| JP3620406B2 (en) | 2005-02-16 |
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