JPS62204892A - Desalting method - Google Patents
Desalting methodInfo
- Publication number
- JPS62204892A JPS62204892A JP61047298A JP4729886A JPS62204892A JP S62204892 A JPS62204892 A JP S62204892A JP 61047298 A JP61047298 A JP 61047298A JP 4729886 A JP4729886 A JP 4729886A JP S62204892 A JPS62204892 A JP S62204892A
- Authority
- JP
- Japan
- Prior art keywords
- water
- treated
- tower
- exchange resin
- reverse osmosis
- 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.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims abstract description 5
- 238000011033 desalting Methods 0.000 title 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 104
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 62
- 239000012528 membrane Substances 0.000 claims abstract description 50
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 43
- 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 claims abstract description 19
- 239000003729 cation exchange resin Substances 0.000 claims abstract description 18
- 239000003957 anion exchange resin Substances 0.000 claims description 17
- 238000010612 desalination reaction Methods 0.000 claims description 2
- 229910052799 carbon Inorganic materials 0.000 abstract description 25
- 230000002378 acidificating effect Effects 0.000 abstract description 22
- 241000894006 Bacteria Species 0.000 abstract description 21
- 150000002500 ions Chemical class 0.000 abstract description 10
- 238000004062 sedimentation Methods 0.000 abstract description 6
- 239000008234 soft water Substances 0.000 abstract description 6
- 239000004576 sand Substances 0.000 abstract description 4
- 150000001768 cations Chemical class 0.000 abstract description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 8
- 230000007423 decrease Effects 0.000 description 7
- 238000001914 filtration Methods 0.000 description 6
- 239000012466 permeate Substances 0.000 description 6
- 238000006114 decarboxylation reaction Methods 0.000 description 5
- 150000003839 salts Chemical class 0.000 description 5
- 229910021642 ultra pure water Inorganic materials 0.000 description 5
- 239000012498 ultrapure water Substances 0.000 description 5
- 239000000645 desinfectant Substances 0.000 description 4
- -1 Cβ ions Chemical class 0.000 description 3
- 239000004952 Polyamide Substances 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 230000015271 coagulation Effects 0.000 description 3
- 238000005345 coagulation Methods 0.000 description 3
- 239000002131 composite material Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 229910052500 inorganic mineral Inorganic materials 0.000 description 3
- 238000005342 ion exchange Methods 0.000 description 3
- 244000005700 microbiome Species 0.000 description 3
- 239000011707 mineral Substances 0.000 description 3
- 229920002647 polyamide Polymers 0.000 description 3
- 238000009287 sand filtration Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 150000001450 anions Chemical class 0.000 description 2
- 238000009395 breeding Methods 0.000 description 2
- 230000001488 breeding effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 150000007524 organic acids Chemical class 0.000 description 2
- 235000005985 organic acids Nutrition 0.000 description 2
- 229920002492 poly(sulfone) Polymers 0.000 description 2
- 230000001902 propagating effect Effects 0.000 description 2
- 239000004065 semiconductor Substances 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 230000001954 sterilising effect Effects 0.000 description 2
- 238000004659 sterilization and disinfection Methods 0.000 description 2
- 235000012431 wafers Nutrition 0.000 description 2
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- 229920002301 cellulose acetate Polymers 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 239000008119 colloidal silica Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 229910001425 magnesium ion Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000003204 osmotic effect Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000035755 proliferation Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000009291 secondary effect Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000000108 ultra-filtration Methods 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
- Y02A20/131—Reverse-osmosis
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Treatment Of Water By Ion Exchange (AREA)
- Water Treatment By Sorption (AREA)
Abstract
Description
【発明の詳細な説明】
〈産業上の利用分野〉
本発明は、粒状活性炭塔と逆浸透膜装置とイオン交換樹
脂塔を組み合わせて、原水中の全存機炭素（以下Ｔ、Ｏ
，Ｃと言う）を除去するとともに脱塩する場合において
、粒状活性炭塔および逆浸透膜装置に一般細菌が繁殖す
るのを防止する方法に関するものである。Detailed Description of the Invention <Industrial Application Field> The present invention combines a granular activated carbon column, a reverse osmosis membrane device, and an ion exchange resin column to remove total organic carbon (hereinafter referred to as T, O) in raw water.
This invention relates to a method for preventing the growth of common bacteria in a granular activated carbon tower and a reverse osmosis membrane device when removing and desalinating carbon (hereinafter referred to as "C").
〈従来の技術〉
ＬＳＩや超ＬＳＩを生産する電子工業においては、その
中間製品である半導体ウェハーの洗浄にあたり、その製
品の歩留まりを向上するために微粒子数、Ｔ、Ｏ，Ｃ、
イオン等をｐＩ）ｂオーダーまで減少させた、いわゆる
超純水を必要とする。<Prior art> In the electronics industry that produces LSI and VLSI, when cleaning semiconductor wafers, which are intermediate products, the number of particles, T, O, C,
It requires so-called ultrapure water in which ions and the like are reduced to the pI)b order.
このような超純水を製造する場合、近年において逆浸透
膜装置が用いられることが多い。When producing such ultrapure water, reverse osmosis membrane devices are often used in recent years.
すなわち−次側処理装置として、原水を凝集沈殿、濾過
などをして原水中の懸濁物質等を除去し、当該原水を逆
浸透膜装置で脱塩し、次いで当該脱塩水をさらに２床３
塔式純水製造装置、混床式ポリシャー、精密濾過器等で
処理し、次いで当該−次側処理純水をさらに二次側処理
装置として混床式ポリシャー、紫外線殺菌装置、超濾過
膜装置あるいは逆浸透膜装置で処理して前記超純水を得
るものである。In other words, as a next-side treatment device, the raw water is subjected to coagulation sedimentation, filtration, etc. to remove suspended substances, etc., the raw water is desalted with a reverse osmosis membrane device, and then the desalted water is further passed through two beds.
It is treated with a tower-type pure water production device, a mixed-bed polisher, a precision filter, etc., and then the next-side treated pure water is further processed as a secondary-side treatment device such as a mixed-bed polisher, an ultraviolet sterilizer, an ultrafiltration membrane device, or the like. The ultrapure water is obtained by processing with a reverse osmosis membrane device.
逆浸透膜装置は逆浸透膜に原水を溶解塩類の浸透圧以上
の加圧下で供給し、塩類の大半を逆浸透膜で阻止して塩
類を減少させた透過水を処理水として得るとともに、塩
類を濃縮した非透過水を排出するものであるが、この処
理中に原水に含まれているＴ、Ｏ，Ｃ等も逆浸透膜で阻
止することができ、前記超純水の製造には好都合である
。A reverse osmosis membrane device supplies raw water to a reverse osmosis membrane under pressure higher than the osmotic pressure of dissolved salts, and the reverse osmosis membrane blocks most of the salts to obtain permeated water with reduced salts as treated water. During this treatment, T, O, C, etc. contained in the raw water can be blocked by the reverse osmosis membrane, which is convenient for producing ultrapure water. It is.
しかしながら前記逆浸透膜装置でＴ、Ｏ，Ｃ等を除去す
ることはできるが、原水中に多量のＴ、０゜Ｃ等が存在
していると逆浸透膜を汚染することとなり、その透過水
量が低下したりして好ましくない。However, although it is possible to remove T, O, C, etc. with the reverse osmosis membrane device, if a large amount of T, 0°C, etc. is present in the raw water, it will contaminate the reverse osmosis membrane, and the amount of permeated water will decrease. This is not desirable as it may cause a decrease in
従って原水中のＴ、Ｏ，Ｃを出来るだけ逆浸透膜装置の
前段で除去するために、粒状活性炭塔が用いられること
が多い。Therefore, in order to remove as much T, O, and C from raw water as possible before the reverse osmosis membrane device, a granular activated carbon column is often used.
すなわち原水を凝集沈殿、濾過などの前処理をした後、
粒状活性炭塔であらかじめ可能なかぎりＴ、Ｏ，Ｃを除
去した後、その処理水を逆浸透膜装置で処理するもので
ある。In other words, after pretreatment of raw water such as coagulation sedimentation and filtration,
After removing as much T, O, and C as possible in advance in a granular activated carbon tower, the treated water is treated in a reverse osmosis membrane device.
しかしながら−次側処理装置に粒状活性炭塔を用いると
以下のような新たな問題が生ずることとなる。However, when a granular activated carbon tower is used as a downstream treatment device, the following new problems arise.
すなわち粒状活性炭塔は水中のＴ、Ｏ，Ｃの除去に関し
ては、十分にその能力を発揮するが、粒状活性炭層は一
般細菌の温床となりやすく、粒状活性炭塔で原水を処理
すると、その処理水のＴ、Ｏ。In other words, the granular activated carbon tower fully demonstrates its ability to remove T, O, and C from water, but the granular activated carbon layer tends to become a breeding ground for general bacteria, and when raw water is treated with the granular activated carbon tower, the treated water T.O.
Ｃは大幅に減少するが、生菌数が大幅に増加するという
欠点がある。さらに後段に設置されている逆浸透膜装置
内にも一般細菌が繁殖し、透過水量が低下したり、また
透過水中に生菌が多量に漏洩してくることとなる。Although C is significantly reduced, the disadvantage is that the number of viable bacteria is significantly increased. Furthermore, general bacteria will grow in the reverse osmosis membrane device installed at the later stage, resulting in a decrease in the amount of permeated water and a large amount of living bacteria leaking into the permeated water.
前述した半導体ウェハーの洗浄用の超純水においては生
菌の存在も製品の歩留まりを低下させる原因となるので
、前記した生菌数の増加は好ましいものではない。In the ultrapure water for cleaning semiconductor wafers described above, the presence of viable bacteria also causes a decrease in the yield of products, so the increase in the number of viable bacteria is not desirable.
なお一般細菌が繁殖した粒状活性炭塔および逆浸透膜装
置を定期的に熱水あるいは各種の殺菌剤で洗浄して殺菌
処理することも考えられるが、操作が繁雑となり、また
熱水を使用する場合は粒状活性炭塔、逆浸透膜装置、配
管等を耐熱性のものとする必要があり、設備費が増加し
、また殺菌剤を用いる場合は処理コストが増加するとい
う問題の他に、粒状活性炭塔においてはＴ、Ｏ，Ｃ吸着
量を低下させたり、また逆浸透膜装置においては使用す
る逆浸透膜に制約を受けたり、そして当該殺菌剤が通水
中に漏洩する等の問題があって好ましくない。It is also possible to sterilize the granular activated carbon tower and reverse osmosis membrane equipment where general bacteria have grown by periodically cleaning them with hot water or various disinfectants, but this would be complicated to operate, and if hot water is used, In addition to the problem that the granular activated carbon tower, reverse osmosis membrane equipment, piping, etc. must be made heat-resistant, which increases equipment costs, and if a disinfectant is used, the processing cost increases. It is undesirable because it reduces the adsorption amount of T, O, and C in the case of a reverse osmosis membrane device, and there are restrictions on the reverse osmosis membrane used in a reverse osmosis membrane device, and there are problems such as the disinfectant leaking during water flow. .
〈発明が解決しようとする問題点〉
本発明は原水を粒状活性炭塔で濾過し、次いで当該濾過
水を逆浸透膜装置で処理し、次しくでイオン交換装置で
処理する際における前述の欠点を解決し、熱水あるいは
殺菌剤を全く使用することなく、かつ定期的な殺菌処理
等を行うことなく、かつ低コストで粒状活性炭塔および
逆浸透膜装置における一般細菌の繁殖を防止することを
目的とするものである。<Problems to be Solved by the Invention> The present invention solves the above-mentioned drawbacks when raw water is filtered through a granular activated carbon tower, the filtered water is then treated with a reverse osmosis membrane device, and then treated with an ion exchange device. The purpose is to solve the problem and prevent the growth of general bacteria in granular activated carbon towers and reverse osmosis membrane equipment at low cost without using any hot water or disinfectants, without periodic sterilization, etc. That is.
く問題点を解決するための手段〉
微生物の生育はその環境ｐＨによって影響を受け、それ
ぞれの微生物にはその生育好適ｐＨ帯がある。Means for Solving Problems> The growth of microorganisms is affected by the pH of the environment, and each microorganism has its preferred pH range for growth.
たとえば一般細菌は中性から弱アルカリ性（ｐＨ７〜８
）に、酵母と黴は弱酸性（ｐＨ６〜７）に最適ｐＨ帯が
あると言われている。For example, common bacteria are neutral to slightly alkaline (pH 7 to 8).
), yeast and mold are said to have an optimal pH range in a slightly acidic range (pH 6-7).
また最適ｐＨ帯から酸性側あるいはアルカリ性側に移る
に従って微生物の生育は次第に抑制され、追には死滅す
るとも言われている。It is also said that the growth of microorganisms is gradually suppressed and eventually becomes extinct as the pH moves from the optimum pH range to the acidic or alkaline side.
従って通常の一般細菌はｐＨが低くなればなる程、その
生育が抑制されるようになる。Therefore, the lower the pH, the more the growth of ordinary bacteria is inhibited.
本発明はこの点に鑑みてなされたもので、Ｈ形カチオン
交換樹脂塔の処理水が通常ｐＨ３前後の酸性であること
から、原水をまずＨ形カチオン交換樹脂塔で処理し、当
該酸性の処理水を粒状活性炭濾過塔に通水することによ
り、Ｔ、Ｏ，Ｃを除去するとともに、粒状活性炭塔にお
ける一般細菌の繁殖を効果的に防止し、次いで当該濾過
水を逆浸透膜装置で処理して残留Ｔ、Ｏ，Ｃを除去する
とともに大部分の脱塩を行い、次いでその透過水をＯＨ
形アニオン交換樹脂の混床塔で処理することを特徴とす
る脱塩方法に関するものである。The present invention was made in view of this point, and since the treated water of the H type cation exchange resin tower is usually acidic with a pH of around 3, the raw water is first treated in the H type cation exchange resin tower, and the acidic treatment is carried out by first treating the raw water in the H type cation exchange resin tower. By passing water through a granular activated carbon filtration tower, T, O, and C are removed, and the proliferation of general bacteria in the granular activated carbon tower is effectively prevented, and then the filtered water is treated with a reverse osmosis membrane device. The remaining T, O, and C are removed and most of the salt is desalted, and the permeated water is then treated with OH
The present invention relates to a desalination method characterized by treatment in a mixed bed column of type anion exchange resin.
く作用〉
図面は本発明の実施態様の一例を示すフローの説明図で
あるが、原水−１をまず凝集沈殿装置２および砂濾過塔
３で処理し、原水中に含有している懸濁物質、コロイド
シリカ、Ｔ、Ｏ，Ｃの一部等を除去する。Action> The drawing is an explanatory diagram of a flow showing an example of an embodiment of the present invention. Raw water-1 is first treated with a coagulation-sedimentation device 2 and a sand filter tower 3 to remove suspended substances contained in the raw water. , colloidal silica, and some of T, O, and C are removed.
なお原水１の水質によっては凝集沈殿装置２を省略して
も差し支えなく、あるいは砂濾過塔３の入口水に凝集剤
等を添加するマイクロフロック濾過を行ってもよい。Note that depending on the quality of the raw water 1, the coagulation-sedimentation device 2 may be omitted, or microfloc filtration may be performed in which a coagulant or the like is added to the inlet water of the sand filtration tower 3.
次いで当該砂濾過塔３の処理水をＨ形カチオシ交換樹脂
塔４で処理する。当該カチオン交換樹脂塔４は、Ｈ膨強
酸性カチオン交換樹脂単独あるいはＨ形弱酸性カチオン
交換樹脂とＨ膨強酸性カチオン交換樹脂を複層床に充填
したもので、ここで水中のカチオンをＨイオンにイオン
交換する。従ってその処理水は水中に含まれるＣβイオ
ン、ＳＯ，イオン等の鉱酸イオンに相当する鉱酸が生成
されるとともに、水中に含まれているＨＣＯ３イオンは
遊離炭酸となり、そのｐＨは通常３前後の酸性を呈する
。Next, the treated water from the sand filter tower 3 is treated in the H-type cation exchange resin tower 4. The cation exchange resin column 4 is a multi-layer bed packed with an H-swollen acidic cation exchange resin alone or an H-type weakly acidic cation exchange resin and an H-swollen strong acidic cation exchange resin, in which cations in water are converted into H ions. ion exchange. Therefore, in the treated water, mineral acids corresponding to mineral acid ions such as Cβ ions, SO, ions, etc. contained in the water are generated, and HCO3 ions contained in the water become free carbonic acid, and the pH thereof is usually around 3. exhibits acidic properties.
次いで当該酸性軟水を脱炭酸塔５で処理する。Next, the acidic soft water is treated in a decarboxylation tower 5.
当該脱炭酸塔５はラシヒリング等の充填層の上部から酸
性軟水を流下するとともに、充填層の下部から空気、窒
素等の気体を流入するもの、あるいは脱炭酸塔５内を減
圧して溶解気体を排除する、いわゆる真空脱気装置であ
り、このような気液接触あるいは減圧処理により、酸性
軟水中の遊離炭酸を除去する。The decarboxylation tower 5 is one in which acidic soft water flows down from the upper part of a packed bed such as a Raschig ring, and gases such as air and nitrogen are introduced from the bottom of the packed bed, or the inside of the decarboxylation tower 5 is depressurized to remove dissolved gas. This is a so-called vacuum deaerator that removes free carbonic acid from acidic soft water through such gas-liquid contact or reduced pressure treatment.
なお原水中に含まれるＨＣＯ３イオンの量がそれ程多く
ない場合は、当該脱炭酸塔５の設置を省略しても差し支
えない。Note that if the amount of HCO3 ions contained in the raw water is not so large, the installation of the decarbonation tower 5 may be omitted.
本発明は次いで脱炭酸塔５からの脱炭酸水を粒状活性炭
塔６に通水し、脱炭酸水中に含まれているＴ、Ｏ，Ｃの
大半をここで吸着除去する。In the present invention, the decarbonated water from the decarbonation tower 5 is then passed through the granular activated carbon tower 6, where most of the T, O, and C contained in the decarbonated water are adsorbed and removed.
当該粒状活性炭塔６は粒状活性炭を充填したものである
が、本発明においては当該充填層に常にｐＨ３前後の酸
性水が接触するので、当該充填層に一般細菌が繁殖する
のを効果的に防止することができる。The granular activated carbon tower 6 is filled with granular activated carbon, and in the present invention, acidic water with a pH of around 3 is always in contact with the packed bed, so it is effective to prevent general bacteria from breeding in the packed bed. can do.
また一般に水中に含まれる有機物の内、親水性有機酸類
は系のｐＨが酸性になると溶解度が減少するので、その
結果として水に対する親和力が減少し、活性炭によりよ
く吸着すると言われており、従って本発明においてはこ
れらの親水性有機酸類に起因するＴ、Ｏ，Ｃの除去効果
を向上させることができる。Furthermore, among the organic substances generally contained in water, the solubility of hydrophilic organic acids decreases when the pH of the system becomes acidic.As a result, their affinity for water decreases, and it is said that they are better adsorbed by activated carbon. In the present invention, the effect of removing T, O, and C caused by these hydrophilic organic acids can be improved.
このような処理により水中のＴ、Ｏ，Ｃの大部分を除去
した粒状活性炭塔６の処理水を次いで逆浸透膜装置７で
処理し、大部分のイオンを除去した透過水８を得るとと
もにイオンを濃縮した非透過水９を得、非透過水９はブ
ローする。なお場合によっては非透過水９の一部を回収
して原水に混合しても差し支えない。The treated water from the granular activated carbon tower 6, from which most of the T, O, and C in the water have been removed through such treatment, is then treated with a reverse osmosis membrane device 7 to obtain permeated water 8 from which most of the ions have been removed, as well as ions. A non-permeate water 9 is obtained by concentrating the non-permeate water 9, and the non-permeate water 9 is blown. In some cases, a part of the non-permeated water 9 may be recovered and mixed with the raw water.
本発明においては逆浸透膜装置７の供給水が酸性なので
、逆浸透膜装置７においても一般細菌が繁殖するのを効
果的に防止することができる。In the present invention, since the water supplied to the reverse osmosis membrane device 7 is acidic, it is possible to effectively prevent general bacteria from propagating in the reverse osmosis membrane device 7 as well.
逆浸透膜装置７の透過水８を次いでＯＨ形アニオン交換
樹脂塔１０に通水し、残留する鉱酸イオン、シリカ、遊
離炭酸等のアニオン成分を除去し、脱塩水を得る。当該
ＯＨ形アニオン交換樹脂塔は、ＯＨ形強塩基性アニオン
交換樹脂単独あるいはＯＨ形弱塩基性アニオン交換樹脂
とＯＨ形強塩基性アニオン交換樹脂を複層床に充填した
ものである。The permeated water 8 from the reverse osmosis membrane device 7 is then passed through an OH type anion exchange resin column 10 to remove residual anion components such as mineral acid ions, silica, and free carbonic acid to obtain demineralized water. The OH type anion exchange resin column is a multilayer bed packed with an OH type strong basic anion exchange resin alone or an OH type weakly basic anion exchange resin and an OH type strong basic anion exchange resin.
なおＯＨ形アニオン交換樹脂塔ＩＯにかえてこの部分を
Ｈ膨強酸性カチオン交換樹脂とＯＨ形強塩基性アニオン
交換樹脂の混床塔としても差し支えない。要は逆浸透膜
装置７の後段で透過水８中に残留する鉱酸イオン、シリ
カ、遊離炭酸等のアニオン成分を除去することができる
イオン交換塔を用いればよい。Note that instead of the OH type anion exchange resin column IO, this portion may be used as a mixed bed column of an H-swelled acidic cation exchange resin and an OH type strong basic anion exchange resin. In short, an ion exchange column capable of removing anion components such as mineral acid ions, silica, and free carbonate remaining in the permeated water 8 after the reverse osmosis membrane device 7 may be used.
ＯＨ形アニオン交換樹脂塔１０の処理水を次いで温床式
ポリシャー１１、精密濾過塔１２等で処理し、当該−次
側処理純水１３を二次側処理装置に供給する。The treated water from the OH type anion exchange resin column 10 is then treated in a hotbed polisher 11, a precision filtration column 12, etc., and the downstream treated pure water 13 is supplied to a secondary treatment device.
本発明の逆浸透膜装置７に使用する逆浸透膜としては、
酢酸セルローズ系膜、ポリアミド系膜およびポリアミド
系とポリスルホン系の複合膜等を用いることができるが
、Ｔ、Ｏ，Ｃの除去能力の優れている前記の複合膜を用
いることが望ましい。The reverse osmosis membrane used in the reverse osmosis membrane device 7 of the present invention includes:
Although cellulose acetate membranes, polyamide membranes, composite membranes of polyamide and polysulfone membranes, etc. can be used, it is preferable to use the aforementioned composite membranes, which have excellent T, O, and C removal abilities.
〈効果〉
以上説明したごとく、本発明は原水を先にＨ形カチオン
交換樹脂塔で処理して酸性水を得、当該酸性水を粒状活
性炭塔および逆浸透膜装置で処理し、その透過水をＯＨ
形アニオン交換樹脂塔もしくは混床塔で処理するので、
粒状活性炭塔、逆浸透膜装置には常に酸性水を接触させ
ることができ、両者に一般細菌を繁殖させることがなく
、効果的に原水中のＴ、Ｏ，Ｃを除去できるとともに、
脱塩することができる。<Effects> As explained above, in the present invention, raw water is first treated in an H-type cation exchange resin column to obtain acidic water, then the acidic water is treated in a granular activated carbon column and a reverse osmosis membrane device, and the permeated water is OH
Because it is processed in a type anion exchange resin tower or a mixed bed tower,
Acidic water can be constantly brought into contact with the granular activated carbon tower and reverse osmosis membrane device, preventing general bacteria from propagating in both, effectively removing T, O, and C from raw water.
Can be desalinated.
また本発明は、殺菌するための余分な操作をすることな
く、かつ殺直剤を全く使用しないので、低コストでＴ、
Ｏ，Ｃが除去された脱塩水を供給できる。In addition, the present invention does not require any extra operations for sterilization and does not use any directicides, so T.
Demineralized water from which O and C have been removed can be supplied.
また本発明では逆浸透膜装置の前段で原水中のカルシウ
ムイオン、マグネシウムイオンなどの硬度成分をＨ形カ
チオン交換樹脂塔で除去できるので、かかる硬度成分の
濃縮による逆浸透膜面におけるスケールの発生がなく、
従って透過水回収率全可能なかぎり高めることができ、
更にＯＨ形アニオン交換樹脂塔もしくは混床塔の前段に
逆浸透膜装置を設置してここで大部分の塩類をあらかじ
め除去するので、使用すべきアニオン交換樹脂量を大幅
に減少せしめることができるという副次的効果も奏する
。Furthermore, in the present invention, hardness components such as calcium ions and magnesium ions in the raw water can be removed by an H-type cation exchange resin tower before the reverse osmosis membrane device, so that the formation of scale on the reverse osmosis membrane surface due to the concentration of such hardness components is prevented. Without,
Therefore, the permeate recovery rate can be increased as much as possible,
Additionally, a reverse osmosis membrane device is installed before the OH-type anion exchange resin tower or mixed bed tower, and most of the salts are removed here in advance, making it possible to significantly reduce the amount of anion exchange resin that needs to be used. It also has secondary effects.
以下に本発明の効果をより明確とするために実施例を説
明する。Examples will be described below to make the effects of the present invention more clear.
実施例
本発明の実施例として、図面に示したフローに従って、
砂濾過塔の処理水をＦＩ形カチオン交換樹脂塔および脱
炭酸塔で処理した。Example As an example of the present invention, according to the flow shown in the drawings,
The treated water from the sand filter tower was treated with an FI type cation exchange resin tower and a decarboxylation tower.
その結果ｐＨ２，７〜２．９の酸性軟水が得られた。As a result, acidic soft water with a pH of 2.7 to 2.9 was obtained.
この酸性軟水を充填層高２ｍの粒状活性炭塔にＬＶ１５
ｍ／Ｈの条件で通水し、その濾過水を逆浸透膜としてポ
リアミド系とポリスルホン系の複合膜である日東電工（
４１製ＮＴＲ−７１９７を装着した逆浸透膜装置で処理
し、その透過水をＯＨ形アニオン交換樹脂塔で処理した
。This acidic soft water is transferred to a granular activated carbon tower with a packed bed height of 2m at LV15.
Nitto Denko (Nitto Denko), which is a composite membrane of polyamide and polysulfone, passes water under the conditions of m/H and uses the filtered water as a reverse osmosis membrane.
It was treated with a reverse osmosis membrane device equipped with NTR-7197 manufactured by No. 41, and the permeated water was treated with an OH type anion exchange resin column.
Ｈ形カチオン交換樹脂塔およびアニオン交換樹脂塔につ
いては、必要に応じ常法の再生操作を処理中に随時実施
したが、全処理時間として３，０００時間処理を行った
。Regarding the H-type cation exchange resin tower and anion exchange resin tower, regeneration operations using conventional methods were carried out as needed during the treatment, and the treatment was carried out for a total treatment time of 3,000 hours.
その結果、粒状活性炭塔の処理水のＴ、Ｏ，Ｃは０．０
５■ａｓＣ／１となり、また当該処理水に生菌は全く漏
洩しなかった。As a result, T, O, and C of the treated water from the granular activated carbon tower were 0.0.
5■asC/1, and no living bacteria leaked into the treated water.
更に逆浸透膜装置の透過水のＴ、Ｏ，Ｃは０．０２５■
ａｓＣ／ｌとなり、また当該透過水中にも生菌は全く漏
洩せず、また透過水量が低下することもなかった。なお
砂濾過水のＴ、Ｏ，Ｃは１．０■ａｓＣ／１である。Furthermore, the T, O, and C of the permeated water from the reverse osmosis membrane device are 0.025■
asC/l, no viable bacteria leaked into the permeated water, and the amount of permeated water did not decrease. Note that T, O, and C of the sand-filtered water are 1.0 asC/1.
一方比較のために同様の砂濾過塔の処理水を本発明に用
いたと同じ粒状活性炭塔で同条件で処理し、次いで当該
濾過水を同じ逆浸透膜装置で３，０００時間処理したと
ころ、粒状活性炭塔の処理水のＴ。On the other hand, for comparison, treated water from a similar sand filtration tower was treated under the same conditions in the same granular activated carbon tower used in the present invention, and then the filtered water was treated for 3,000 hours in the same reverse osmosis membrane device. T of treated water from activated carbon tower.
Ｏ，Ｃは０．２ｍｇ ａｓ Ｃ／ １となり、また当８
亥処理水の生菌数は運転初期６〜１５個／ｍβ、運転中
期９５〜１８５個／ｍβ、３，０００時間後２３０〜３
１０個／ ｍ ｌであり、処理水中に流出した生菌数は
かなり増加した。O, C is 0.2 mg as C/1, and this 8
The number of viable bacteria in the boar treated water was 6-15 cells/mβ at the beginning of operation, 95-185 cells/mβ during the middle period of operation, and 230-3 after 3,000 hours.
10 cells/ml, and the number of viable bacteria that leaked into the treated water increased considerably.
また逆浸透膜装置の透過水のＴ、Ｏ，Ｃはｏ、１■ａｓ
Ｃ７Ｎであり、また透過水の生菌数は運転３゜０００時
間後で２０〜３２個／ ｍ Ａであった。更に逆浸透膜
装置の透過水量は運転初期と比較して４０％も低下した
。In addition, T, O, and C of the permeated water of the reverse osmosis membrane device are o, 1■ as
C7N, and the number of viable bacteria in the permeated water was 20 to 32 cells/mA after 3,000 hours of operation. Furthermore, the amount of water permeated through the reverse osmosis membrane device decreased by 40% compared to the initial period of operation.
図面は本発明の実施態様の一例を示すフローの説明図で
ある。
■・・・原水 ２・・・凝集沈殿装置３・・
・砂濾過塔
４・・・Ｈ形カチオン交換樹脂塔
５・・・脱炭酸塔 ６・・・粒状活性炭塔７・・
・逆浸透膜装置 ８・・・透過水９・・・非透過水
１０・・・ＯＨ形アニオン交換樹脂塔
ゝ１１・・・温床式ポリシャー
１２・・・精密濾過塔
１３・・・−次側処理純水The drawing is an explanatory diagram of a flow showing an example of an embodiment of the present invention. ■...Raw water 2...Coagulation sedimentation device 3...
・Sand filtration tower 4... H type cation exchange resin tower 5... Decarboxylation tower 6... Granular activated carbon tower 7...
・Reverse osmosis membrane device 8...Permeate water 9...Non-permeate water 10...OH type anion exchange resin tower
11...Hotbed polisher 12...Precision filtration tower 13...-next side treated pure water
Claims (1)
理水を粒状活性炭塔で処理し、次いでその濾過水を逆浸
透膜装置で処理し、次いでその透過水をＯＨ形アニオン
交換樹脂塔もしくはＨ形カチオン交換樹脂とＯＨ形アニ
オン交換樹脂の混床塔で処理することを特徴とする脱塩
方法Raw water is treated in an H type cation exchange resin column, then the treated water is treated in a granular activated carbon column, the filtered water is then treated in a reverse osmosis membrane device, and then the permeated water is treated in an OH type anion exchange resin column or H A desalination method characterized by treatment in a mixed bed tower of a type cation exchange resin and an OH type anion exchange resin.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61047298A JPS62204892A (en) | 1986-03-06 | 1986-03-06 | Desalting method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61047298A JPS62204892A (en) | 1986-03-06 | 1986-03-06 | Desalting method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS62204892A true JPS62204892A (en) | 1987-09-09 |
Family
ID=12771375
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61047298A Pending JPS62204892A (en) | 1986-03-06 | 1986-03-06 | Desalting method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS62204892A (en) |
Cited By (16)
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|---|---|---|---|---|
| WO1998006483A1 (en) * | 1996-08-12 | 1998-02-19 | Debasish Mukhopadhyay | Method and apparatus for high efficiency reverse osmosis operation |
| US5925255A (en) * | 1997-03-01 | 1999-07-20 | Mukhopadhyay; Debasish | Method and apparatus for high efficiency reverse osmosis operation |
| US6306197B1 (en) | 2000-04-19 | 2001-10-23 | Seh America, Inc. | Isopropyl alcohol scrubbing system |
| US6325983B1 (en) | 2000-04-19 | 2001-12-04 | Seh America, Inc. | Nox scrubbing system and method |
| US6398965B1 (en) | 1998-03-31 | 2002-06-04 | United States Filter Corporation | Water treatment system and process |
| US6537456B2 (en) | 1996-08-12 | 2003-03-25 | Debasish Mukhopadhyay | Method and apparatus for high efficiency reverse osmosis operation |
| JP2005351881A (en) * | 2004-05-13 | 2005-12-22 | National Institute Of Advanced Industrial & Technology | Coexistent anion treatment device and method |
| US7186344B2 (en) * | 2002-04-17 | 2007-03-06 | Water Visions International, Inc. | Membrane based fluid treatment systems |
| US7320756B2 (en) * | 2001-05-05 | 2008-01-22 | Debasish Mukhopadhyay | Method and apparatus for treatment of feedwaters by membrane separation under acidic conditions |
| JP2008272693A (en) * | 2007-05-01 | 2008-11-13 | Cosmo Health Kk | Water purifier |
| US8617398B2 (en) | 1996-08-12 | 2013-12-31 | Debasish Mukhopadhyay | Method for high efficiency reverse osmosis operation |
| US8758720B2 (en) | 1996-08-12 | 2014-06-24 | Debasish Mukhopadhyay | High purity water produced by reverse osmosis |
| CN104692557A (en) * | 2014-12-22 | 2015-06-10 | 内蒙古久科康瑞环保科技有限公司 | Chemical pretreatment method and device thereof for treating high-salinity wastewater |
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-
1986
- 1986-03-06 JP JP61047298A patent/JPS62204892A/en active Pending
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| US8617398B2 (en) | 1996-08-12 | 2013-12-31 | Debasish Mukhopadhyay | Method for high efficiency reverse osmosis operation |
| WO1998006483A1 (en) * | 1996-08-12 | 1998-02-19 | Debasish Mukhopadhyay | Method and apparatus for high efficiency reverse osmosis operation |
| US8758720B2 (en) | 1996-08-12 | 2014-06-24 | Debasish Mukhopadhyay | High purity water produced by reverse osmosis |
| US8641905B2 (en) | 1996-08-12 | 2014-02-04 | Debasish Mukhopadhyay | Method for high efficiency reverse osmosis operation |
| US6537456B2 (en) | 1996-08-12 | 2003-03-25 | Debasish Mukhopadhyay | Method and apparatus for high efficiency reverse osmosis operation |
| US9428412B2 (en) | 1996-08-12 | 2016-08-30 | Debasish Mukhopadhyay | Method for high efficiency reverse osmosis operation |
| US9073763B2 (en) | 1996-08-12 | 2015-07-07 | Debasish Mukhopadhyay | Method for high efficiency reverse osmosis operation |
| US5925255A (en) * | 1997-03-01 | 1999-07-20 | Mukhopadhyay; Debasish | Method and apparatus for high efficiency reverse osmosis operation |
| US6398965B1 (en) | 1998-03-31 | 2002-06-04 | United States Filter Corporation | Water treatment system and process |
| US6306197B1 (en) | 2000-04-19 | 2001-10-23 | Seh America, Inc. | Isopropyl alcohol scrubbing system |
| US6325983B1 (en) | 2000-04-19 | 2001-12-04 | Seh America, Inc. | Nox scrubbing system and method |
| US7320756B2 (en) * | 2001-05-05 | 2008-01-22 | Debasish Mukhopadhyay | Method and apparatus for treatment of feedwaters by membrane separation under acidic conditions |
| US7186344B2 (en) * | 2002-04-17 | 2007-03-06 | Water Visions International, Inc. | Membrane based fluid treatment systems |
| JP2005351881A (en) * | 2004-05-13 | 2005-12-22 | National Institute Of Advanced Industrial & Technology | Coexistent anion treatment device and method |
| JP2008272693A (en) * | 2007-05-01 | 2008-11-13 | Cosmo Health Kk | Water purifier |
| CN104692557A (en) * | 2014-12-22 | 2015-06-10 | 内蒙古久科康瑞环保科技有限公司 | Chemical pretreatment method and device thereof for treating high-salinity wastewater |
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| WO2020195217A1 (en) * | 2019-03-26 | 2020-10-01 | 栗田工業株式会社 | Method and device for treating water containing calcium and organic matter |
| JP2020157223A (en) * | 2019-03-26 | 2020-10-01 | 栗田工業株式会社 | Method and device of treating water that contains organic matter and calcium |
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