JPH05192543A - Method and apparatus for regenerating membrane evaporative concentrator of waste fluid - Google Patents
Method and apparatus for regenerating membrane evaporative concentrator of waste fluidInfo
- Publication number
- JPH05192543A JPH05192543A JP818292A JP818292A JPH05192543A JP H05192543 A JPH05192543 A JP H05192543A JP 818292 A JP818292 A JP 818292A JP 818292 A JP818292 A JP 818292A JP H05192543 A JPH05192543 A JP H05192543A
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- JP
- Japan
- Prior art keywords
- membrane
- waste liquid
- waste fluid
- evaporation
- hydrophobic porous
- 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.)
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- Separation Using Semi-Permeable Membranes (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は廃液処理装置に係り、特
に、宇宙船や原子力発電所などで、界面活性剤が混入す
る水をリサイクルする施設に好適な高性能な廃液処理装
置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a waste liquid treatment device, and more particularly to a high performance waste liquid treatment device suitable for facilities such as spacecraft and nuclear power plants for recycling water mixed with a surfactant.
【０００２】[0002]
【従来の技術】宇宙船や原子力発電所など水をリサイク
ルするため、限られた空間で、廃液から純度の高い水を
得る浄化が必要である。このような浄化方法の一つとし
て、膜蒸留法（膜蒸発濃縮方法）がある。膜蒸発濃縮装
置は、例えば、特公昭50-45461号公報に示される構造が
ある。また、蒸発濃縮器を組み込んだ廃液処理方法とし
ては、例えば、特開昭61−164195号公報に示された方法
がある。2. Description of the Related Art In order to recycle water such as in a spacecraft or a nuclear power plant, it is necessary to purify water from waste liquid in a limited space. As one of such purification methods, there is a membrane distillation method (membrane evaporation concentration method). The membrane evaporative concentrator has, for example, a structure disclosed in Japanese Patent Publication No. 50-45461. Further, as a waste liquid treatment method incorporating an evaporative concentrator, for example, there is a method disclosed in JP-A-61-164195.
【０００３】これらの蒸発濃縮装置は、蒸発面に膜を用
いていることから、蒸発面積を自由にとれ、装置の小型
化が容易である。また、中温度で蒸気を発生できるの
で、腐蝕し難い高分子材料を構造材料として利用でき
る。この点から、膜蒸発濃縮装置は、従来の金属材料で
作られた蒸発缶濃縮器に比べて多くの利点を有する。Since these evaporative concentrators use a film on the evaporating surface, the evaporating area can be freely set and the device can be easily miniaturized. Further, since steam can be generated at an intermediate temperature, a polymeric material that is difficult to corrode can be used as a structural material. From this point, the membrane evaporative concentrator has many advantages over conventional evaporator concentrators made of metallic materials.
【０００４】また、この方法では、数十〜数百μｍの薄
い膜を介して廃液と浄化水が接触するため、廃液の浄化
水へのリークが問題となる。そこで、特開平1−322562
号公報では、リークの問題となる成分をあらかじめ除去
する方法と、リークが拡大する前にアルコールで洗浄し
て再生する方法が提案されている。また、この対策とし
て、特公昭50−3753号公報では、凝縮水側を加圧して、
膜のリーク箇所から廃液が流れでることが防止する方式
が提案されている。Further, in this method, since the waste liquid and the purified water come into contact with each other through a thin film of several tens to several hundreds of μm, leakage of the waste liquid to the purified water poses a problem. Therefore, JP-A-1-322562
In the publication, a method of previously removing a component causing a problem of leakage and a method of cleaning and regenerating with alcohol before the leakage expands are proposed. Further, as a countermeasure against this, in Japanese Patent Publication No. 503753, the condensed water side is pressurized,
A method has been proposed in which the waste liquid is prevented from flowing out from the leak portion of the membrane.
【０００５】[0005]
【発明が解決しようとする課題】特開昭61−164195号公
報では、界面活性剤は微量であってもリークが発生する
ため、あらかじめ除去するためには、装置が大型化して
複雑となる問題点があった。また、リーク時の対策が膜
のアルコール洗浄であるため、発明者らの新たな知見に
よれば、膜の洗浄が十分でない。さらに、アルコールを
使用するために、さらにアルコールの処理装置が新たに
必要となる問題点があった。In Japanese Patent Laid-Open No. 61-164195, even if a small amount of a surfactant is used, a leak occurs. Therefore, in order to remove it in advance, the device becomes large and complicated. There was a point. Further, since the countermeasure against a leak is the cleaning of the film with alcohol, the new findings of the inventors indicate that the cleaning of the film is not sufficient. Further, since alcohol is used, there is a problem that a new alcohol processing device is required.
【０００６】一方、特公昭50−3753号公報では、発明者
らの実験により、十分なリーク対策が得られないという
問題点があることがわかった。On the other hand, Japanese Examined Patent Publication No. 50-3753 has revealed from the experiments by the inventors that there is a problem that sufficient measures against leak cannot be obtained.
【０００７】本発明は、新たな知見により、膜の洗浄方
法、およびその装置を提供することにある。[0007] The present invention is to provide a method for cleaning a film and an apparatus therefor based on a new finding.
【０００８】[0008]
【課題を解決するための手段】上記目的を達成するため
に、可溶性の有機物を含む廃液を、蒸発面に疎水性多孔
質膜を設けた膜蒸発濃縮器によって処理し、清浄な凝縮
水を得る処理方法において、前記疎水性多孔質膜を設け
た前記膜蒸発濃縮器の前記凝縮水側の水圧を廃液側の水
圧よりも高く維持し、前記凝縮水の生成量の低下を検出
して、前記疎水性多孔質膜を有機物を分解する物質で洗
浄し、前記疎水性多孔質膜を乾燥することによって疎水
性膜を再生するようにした。In order to achieve the above object, a waste liquid containing a soluble organic substance is treated by a membrane evaporation concentrator having a hydrophobic porous membrane on the evaporation surface to obtain clean condensed water. In the treatment method, the water pressure on the condensed water side of the membrane evaporation concentrator provided with the hydrophobic porous film is maintained higher than the water pressure on the waste liquid side, and a decrease in the amount of the condensed water generated is detected, and The hydrophobic porous membrane was washed with a substance that decomposes organic substances, and the hydrophobic porous membrane was dried to regenerate the hydrophobic membrane.
【０００９】[0009]
【作用】本発明は、界面活性剤などの膜の有機汚染物を
薬品を用いて分解，除去して再生するものである。ただ
し、膜蒸発濃縮器では、液体が膜を透過してはならない
ため、再生操作によって、リークにつながる膜面の疎水
性の喪失があってはならない。これは、ろ過などで用い
る膜と異なる点で、ろ過で用いる膜では液体を気体を透
過させるため、膜の細孔の構造が変化しない限り、細孔
の表面の化学的な状態が変化しても問題とはならない。According to the present invention, the organic contaminants of the film such as the surface active agent are decomposed and removed by using chemicals to be regenerated. However, in membrane evaporative concentrators, the liquid must not permeate through the membrane, so the regeneration operation must not result in loss of hydrophobicity of the membrane surface leading to leakage. This is different from the membrane used for filtration, etc., because the membrane used for filtration allows liquid to permeate gas, so unless the structure of the pores of the membrane changes, the chemical state of the surface of the pores changes. Does not matter.
【００１０】したがって、膜蒸発濃縮器では、膜の有機
汚染物の除去に当たって、膜面の疎水性を損なうこと無
いような薬品，操作法を見出す必要がある。本発明は、
このような観点からなされたものである。Therefore, in the membrane evaporative concentrator, it is necessary to find a chemical and an operating method for removing the organic contaminants of the membrane, which do not impair the hydrophobicity of the membrane surface. The present invention is
This is the point of view.
【００１１】[0011]
【実施例】以下、本発明の至った基礎検討の結果と、本
発明の好適な実施例について図面を用いて詳細に述べ
る。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS The results of the basic study of the present invention and the preferred embodiments of the present invention will be described below in detail with reference to the drawings.
【００１２】まず、基礎検討の結果について述べる。図
２にリーク特性と膜蒸発濃縮器の原理を示す。膜蒸発濃
縮器は、疎水性多孔質膜を挟んで廃液を流通する蒸発室
及び冷却水を流通する冷却室とにより構成されている。
膜は、ポリテトラフルオロエチレン（ＰＴＦＥ），ポリ
エチレン，ポリプロピレンなどの疎水性の材質による多
孔質膜である。この膜の細孔径は０.０５ 〜数μｍ、気
孔率は５０〜８５％、厚さ２０〜２００μｍのものが用
いられる。疎水性多孔質膜は、気体は透過するが、液は
透過しない性質を持つ。したがって、蒸発室の廃液の温
度は、４０〜９９℃で、冷却室に比べて高く保つ、この
ため、廃液の蒸発が起こり、発生した蒸気は疎水性多孔
質膜内を拡散して冷却室で凝縮する。このようにして、
凝縮水が得られる。リークは、この膜内の細孔に液体の
流路ができ、この流路を通り原液が冷却水側に漏れ出す
現象である。First, the result of the basic examination will be described. Fig. 2 shows the leak characteristics and the principle of the membrane evaporation concentrator. The membrane evaporative concentrator is composed of an evaporation chamber in which a waste liquid flows and a cooling chamber in which cooling water flows, with a hydrophobic porous film interposed therebetween.
The membrane is a porous membrane made of a hydrophobic material such as polytetrafluoroethylene (PTFE), polyethylene and polypropylene. This membrane has a pore size of 0.05 to several μm, a porosity of 50 to 85%, and a thickness of 20 to 200 μm. The hydrophobic porous membrane has a property that gas is permeable but liquid is not permeable. Therefore, the temperature of the waste liquid in the evaporation chamber is kept at 40 to 99 ° C., which is higher than that in the cooling chamber. Therefore, the evaporation of the waste liquid occurs, and the generated vapor diffuses in the hydrophobic porous film and is generated in the cooling chamber. To condense. In this way
Condensed water is obtained. Leakage is a phenomenon in which a liquid flow path is formed in pores in the film, and the stock solution leaks to the cooling water side through the flow path.
【００１３】次に、有機物を含む廃液のリーク特性につ
いて説明する。ここでは、疎水性を失わせる効果が最も
大きい界面活性剤を例にとる。図２に一般的な洗剤で使
用されている界面活性剤であるＤＢＳ（ドデシル・ベン
ゼン・スルホン酸塩）を含む廃液のリーク特性の一例を
示す。原液側を冷却水側に比べて圧力を高めた場合（原
液加圧）、膜内に液体の流路ができると原液がリークす
る冷却水の導電率が上昇する。蒸発速度は、本来の蒸発
量にリーク量が加わるため、リークの進行に伴い、見掛
け上、上昇する。一方、特公昭50−3753号公報に従い、
冷却水側を加圧すると、冷却水の導電率の上昇は少なく
できるが、蒸発速度は見掛け上、低下して最終的に０と
なる。これは、膜内に液体の流路ができると、冷却水が
原液に流入するためである。また、後述するが、冷却水
側加圧でリークした膜を、特開平1−322562 号公報の方
法で膜を洗浄したが、短時間（３０min 以下）で蒸発速
度が０となった。したがって、従来技術を適用しても十
分な効果が得られないことがわかった。Next, the leak characteristics of the waste liquid containing organic substances will be described. Here, a surfactant having the greatest effect of losing hydrophobicity is taken as an example. FIG. 2 shows an example of leak characteristics of a waste liquid containing DBS (dodecyl benzene sulfonate) which is a surfactant used in general detergents. When the pressure on the stock solution side is higher than that on the cooling water side (stock solution pressurization), the conductivity of the cooling water leaking from the stock solution increases when a liquid flow path is formed in the membrane. Since the amount of leak is added to the original amount of evaporation, the evaporation rate apparently increases as the leak progresses. On the other hand, according to Japanese Patent Publication No. 50-3753,
When the cooling water side is pressurized, the increase in the conductivity of the cooling water can be reduced, but the evaporation rate apparently decreases and finally becomes zero. This is because when a liquid flow path is formed in the film, cooling water flows into the stock solution. Further, as will be described later, the film leaked by pressurization on the cooling water side was washed by the method of JP-A-1-322562, but the evaporation rate became 0 in a short time (30 min or less). Therefore, it was found that even if the conventional technique is applied, a sufficient effect cannot be obtained.
【００１４】そこで、イオンとなるＤＢＳがなぜ洗浄で
きないのか、その理由を検討した。その結果、塩の共存
以下の３点がわかった。Then, the reason why the DBS which becomes an ion cannot be cleaned was examined. As a result, the following three points were found: coexistence of salt.
【００１５】（１）ＤＢＳ溶液にＮａＣｌ溶液を添加し
てみた、その結果、白色の沈澱物が生成することわかっ
た。(1) When a NaCl solution was added to the DBS solution, it was found that a white precipitate was formed as a result.
【００１６】（２）図３にＤＢＳ単独の場合と、塩であ
るＮａＣｌが共存した場合の蒸発速度の変化を示す。蒸
発速度は、ＤＢＳ単独の場合には、ほとんど低下しない
が、塩が共存すると急激に低下して０となる。(2) FIG. 3 shows changes in the evaporation rate when DBS is used alone and when NaCl, which is a salt, coexists. The evaporation rate hardly decreases when DBS is used alone, but it rapidly decreases to 0 when salt coexists.
【００１７】（３）疎水性多孔質膜をＤＢＳ溶液に浸漬
して振とうし、膜へのＤＢＳの吸着量を測定した結果、
塩の共存によって、吸着量が約２倍に増加することがわ
かった。(3) The hydrophobic porous membrane was immersed in a DBS solution and shaken to measure the amount of DBS adsorbed on the membrane.
It was found that the coexistence of salt increased the amount of adsorption approximately twice.
【００１８】以上の結果から、ＤＢＳがリークを発生さ
せる機構は、次のようなものであることがわかった。図
４にその機構を示す。ここでは、ＤＢＳ単独の場合とNa
Clが共存する場合について示す。界面活性剤であるＤＢ
Ｓは疎水基と親水基とを持ち、ＤＢＳ単独の場合は、Ｄ
ＢＳは疎水基で、疎水性の膜面に向けて吸着する。一
方、塩が共存する場合には、ＤＢＳの疎水基同士が配向
して、ＤＢＳ分子が集まって粒子（ミセル）を形成し、
この粒子が膜の表面や細孔内に吸着や沈着する。このよ
うに、ＤＢＳが粒子を形成するため、膜面に吸着や沈着
し易くなり、リークし易くなる。また、粒子を形成する
ためは再溶解し難くなる。From the above results, it was found that the mechanism by which DBS causes a leak is as follows. The mechanism is shown in FIG. Here, the case of DBS alone and Na
The case where Cl coexists is shown. DB that is a surfactant
S has a hydrophobic group and a hydrophilic group, and in the case of DBS alone, D
BS is a hydrophobic group and adsorbs toward the hydrophobic membrane surface. On the other hand, when a salt coexists, the hydrophobic groups of DBS are aligned with each other, and DBS molecules gather to form particles (micelles).
These particles are adsorbed or deposited on the surface of the membrane or in the pores. In this way, since DBS forms particles, it tends to be adsorbed or deposited on the film surface and leak easily. In addition, since particles are formed, redissolution becomes difficult.
【００１９】そこで、膜の洗浄方法を比較検討した。表
１に洗浄方法と洗浄効果の評価結果を示す。Therefore, the methods of cleaning the membrane were compared and examined. Table 1 shows the cleaning method and the evaluation results of the cleaning effect.
【００２０】[0020]
【表１】 [Table 1]
【００２１】その結果、温Ｈ2Ｏ2液による洗浄が最も効
果的であることがわかる。As a result, it can be seen that cleaning with the warm H 2 O 2 solution is most effective.
【００２２】以上の基礎検討結果に基づき、これを実施
するの効果的な一実施例を図面を用いて詳細に述べる。Based on the above basic examination results, an effective embodiment for carrying out this will be described in detail with reference to the drawings.
【００２３】〈実施例１〉本発明の好適な実施例の処理
装置の系統図を図１に示す。ここでは、原子力発電所で
発生する廃液の濃縮に適用した場合の例、すなわち、２
〜３％の硫酸ナトリウムを含む廃液を約２０ｗｔ％まで
濃縮する。図１の処理装置は、膜蒸発濃縮器１，廃液の
循環系２，２Ａ、冷却水の循環系３，３Ａより構成され
ている。再生のために、再生系５，５Ａ，５Ｂ，膜の乾
燥のための送風系６が設けられている。この蒸発濃縮器
１は、凝縮水が冷却水中に直接取り込まれるものであ
る。廃液の循環系２，２Ａには、廃液タンク７，加熱器
２１，循環ポンプ２２，バルブ３０，３５，差圧計２６
（一端）が設けられている。冷却水の循環系３，３Ａに
は、冷却水タンク８，冷却器２３，循環ポンプ２４，バ
ルブ３１，３６，差圧計２６（一端）が設けられてい
る。差圧計２６の出力は制御器２７に、制御器２７の出
力はバルブ３０，３１に電気的に接続されている。再生
系５，５Ａ，５Ｂには、再生用の薬液タンク９，送液ポ
ンプ２５，バルブ３２，３３，３７が設けられており、
送風系６には、バルブ３４，送風機１０が設けられてい
る。膜蒸発濃縮器１は、疎水性多孔質膜１１を挟んで廃
液を流通する蒸発室１２及び冷却水を流通する冷却室１
３とにより構成されている。膜１１は、ポリテトラフル
オロエチレン（ＰＴＦＥ），ポリエチレン，ポリプロピ
レンなどの疎水性の多孔質膜（厚さ２０〜２００μｍ）
である。<Embodiment 1> A system diagram of a processing apparatus according to a preferred embodiment of the present invention is shown in FIG. Here, an example when applied to the concentration of waste liquid generated in a nuclear power plant, that is, 2
Concentrate the effluent containing ~ 3% sodium sulfate to about 20 wt%. The processing apparatus shown in FIG. 1 includes a film evaporation concentrator 1, a waste liquid circulation system 2 and 2A, and a cooling water circulation system 3 and 3A. For regeneration, regeneration systems 5, 5A and 5B, and a ventilation system 6 for drying the film are provided. In this evaporative concentrator 1, condensed water is directly taken into cooling water. A waste liquid tank 7, a heater 21, a circulation pump 22, valves 30, 35, and a differential pressure gauge 26 are provided in the waste liquid circulation systems 2 and 2A.
(One end) is provided. The cooling water circulation system 3, 3A is provided with a cooling water tank 8, a cooler 23, a circulation pump 24, valves 31, 36, and a differential pressure gauge 26 (one end). The output of the differential pressure gauge 26 is electrically connected to the controller 27, and the output of the controller 27 is electrically connected to the valves 30 and 31. Regeneration systems 5, 5A, 5B are provided with a chemical tank 9 for regeneration, a liquid feed pump 25, valves 32, 33, 37,
The blower system 6 is provided with a valve 34 and a blower 10. The membrane evaporative concentrator 1 includes an evaporation chamber 12 for circulating waste liquid and a cooling chamber 1 for circulating cooling water with a hydrophobic porous membrane 11 interposed therebetween.
3 and 3. The membrane 11 is a hydrophobic porous membrane (thickness 20 to 200 μm) such as polytetrafluoroethylene (PTFE), polyethylene or polypropylene.
Is.
【００２４】次に、処理装置を用いて本発明の廃液の処
理方法について説明する。まず、タンク７内に廃液貯蔵
タンク（図示せず）から廃液が受け入れられる。次い
で、タンク８内の冷却水は、冷却器２３によって所定の
温度に冷却され、ポンプ２４によりバルブ３６及び循環
系３を通り、膜蒸発濃縮器１の冷却室１３に供給され、
バルブ３１，循環系３Ａを通り、循環される。タンク７
内の廃液は、加熱器２１によって所定の温度に加熱さ
れ、ポンプ２２によりバルブ３５及び循環系２を通り、
膜蒸発濃縮器１の蒸発室１２に供給され、バルブ３０，
循環系２Ａを通り、循環される（この時バルブ３２，３
３，３７は閉）。このとき、バルブ３０，３１は、差圧
計２６の値により制御器２７を介して冷却室１３の圧力
と、冷却室１３の圧力が蒸発室１２のそれより高くなる
ように設定される。Next, a method for treating waste liquid according to the present invention using a treatment apparatus will be described. First, the waste liquid is received in the tank 7 from a waste liquid storage tank (not shown). Next, the cooling water in the tank 8 is cooled to a predetermined temperature by the cooler 23, and is supplied to the cooling chamber 13 of the membrane evaporation concentrator 1 through the valve 36 and the circulation system 3 by the pump 24.
It is circulated through the valve 31 and the circulation system 3A. Tank 7
The waste liquid inside is heated to a predetermined temperature by the heater 21, passes through the valve 35 and the circulation system 2 by the pump 22,
The film is supplied to the evaporation chamber 12 of the film evaporation concentrator 1, and the valve 30,
It is circulated through the circulation system 2A (at this time, the valves 32, 3
3, 37 closed). At this time, the valves 30 and 31 are set so that the pressure of the cooling chamber 13 and the pressure of the cooling chamber 13 become higher than that of the evaporation chamber 12 via the controller 27 according to the value of the differential pressure gauge 26.
【００２５】蒸発室１２の廃液の温度が高いため、廃液
の蒸発が起こり、発生した蒸気は疎水性多孔質膜内を拡
散して冷却室１３で凝縮する。このため、廃液中の界面
活性剤が膜表面で濃縮され、膜内に界面活性剤の粒子が
沈着して、膜が親水化され、廃液が膜内に侵入する。最
終的には、膜の反対側の冷却室１３に達して、液の流れ
る流路ができる。この場合、冷却室１３の圧力が蒸発室
１２のそれより高いため、冷却水が廃液内に流入する。
先に述べたように、この流入量は、膜の親水化の進行に
伴い増加し、蒸発速度が低下する。この低下量が所定の
値以下になった時点で再生操作を行う。再生操作では、
まず、ポンプ２２，２４を停止し、バルブ３０，３１，
３５，３６を閉め蒸発濃縮操作を停止する。次いで、バ
ルブ３２，３３，３７を開き、送液ポンプ２５により、
薬液タンク９のＨ2Ｏ2などの薬液を膜蒸発濃縮器１の冷
却室１３に送り、バルブ３３を介してライン５Ａを通り
薬液タンク９に戻る。また、膜１１を透過した薬液はラ
イン５Ｂを通り、薬液タンク９に戻る。所定時間、薬液
を流した後、送水ポンプ２５を止めて薬液の通水を終了
する。次いで、バルブ３４を開け、送風機１０を運転
し、膜１１の細孔内に残った薬液を乾燥によって除去す
る。Since the temperature of the waste liquid in the evaporation chamber 12 is high, the waste liquid is evaporated, and the generated vapor diffuses in the hydrophobic porous film and is condensed in the cooling chamber 13. For this reason, the surfactant in the waste liquid is concentrated on the surface of the film, the particles of the surfactant are deposited in the film, the film is made hydrophilic, and the waste liquid enters the film. Finally, the cooling chamber 13 on the opposite side of the membrane is reached to form a flow path for the liquid. In this case, since the pressure of the cooling chamber 13 is higher than that of the evaporation chamber 12, the cooling water flows into the waste liquid.
As described above, this inflow rate increases as the membrane becomes hydrophilic, and the evaporation rate decreases. When the amount of decrease falls below a predetermined value, the regeneration operation is performed. In playback operation,
First, the pumps 22, 24 are stopped, and the valves 30, 31,
35 and 36 are closed to stop the evaporative concentration operation. Next, the valves 32, 33, 37 are opened, and the liquid feed pump 25
The chemical solution such as H 2 O 2 in the chemical solution tank 9 is sent to the cooling chamber 13 of the membrane evaporation concentrator 1, and returns to the chemical solution tank 9 through the line 5A via the valve 33. Further, the chemical liquid that has passed through the membrane 11 passes through the line 5B and returns to the chemical liquid tank 9. After flowing the chemical solution for a predetermined time, the water feed pump 25 is stopped to stop the flow of the chemical solution. Next, the valve 34 is opened, the blower 10 is operated, and the chemical liquid remaining in the pores of the membrane 11 is removed by drying.
【００２６】このようにして、再生した膜の蒸発特性
を、従来の水洗浄と比較して、図５に示す。この図から
わかるように、本発明によるＨ2Ｏ2は、未使用の新しい
膜と同様の性能を示し、本発明がリーク防止に著しい効
果がある。また、本発明の再生の繰り返し特性を見た。
図６にその特性を示す。３回の繰り返し操作によって
も、同様の蒸発特性を示し、本発明の効果が確認でき
た。The evaporation characteristics of the film thus regenerated is shown in FIG. 5 in comparison with the conventional water washing. As can be seen from this figure, H 2 O 2 according to the present invention exhibits the same performance as that of a new film that has not been used, and the present invention has a remarkable effect in preventing leakage. Further, the repetitive reproduction characteristics of the present invention were observed.
The characteristic is shown in FIG. The same evaporation characteristics were exhibited even after repeating three times, and the effect of the present invention was confirmed.
【００２７】以上の結果、実施例では廃液成分、特に界
面活性剤などの有機物による膜の汚染の除去に有効であ
り、これら有機成分を含む廃液の蒸発濃縮が可能とな
る。As a result of the above, in the examples, it is effective for removing the contamination of the membrane by the waste liquid components, particularly the organic substances such as the surfactant, and the waste liquid containing these organic components can be evaporated and concentrated.
【００２８】〈実施例２〉上記実施例では、疎水性多孔
質膜１１として平板状の膜１枚を使用した例を示した
が、これを積層した膜，環状の膜，中空糸膜，スパイラ
ル膜でも同様の効果を奏する。また、上記実施例では、
廃液からの蒸発を冷却水中に直接凝縮さたが、特公昭50
−3753号公報にあるように、３室構造とし、凝縮水のみ
を直接取り出す方式にも適用できる。<Example 2> In the above example, an example in which one plate-shaped membrane was used as the hydrophobic porous membrane 11 was shown. A laminated membrane, an annular membrane, a hollow fiber membrane, and a spiral membrane are shown. The same effect is obtained with the film. Further, in the above embodiment,
The evaporation from the waste liquid was condensed directly into the cooling water, but
As disclosed in Japanese Patent No. 3753/1975, a three-chamber structure is adopted, and it is also possible to apply a method of directly taking out only condensed water.
【００２９】〈実施例３〉上記実施例では、薬液として
Ｈ2Ｏ2を用いたが、有機物分解する次亜塩素酸ナトリウ
ムなどの他の薬品や、オゾンを溶解した水などを用いて
も同様の効果を奏する。Example 3 In the above example, H 2 O 2 was used as the chemical solution, but the same applies when other chemicals such as sodium hypochlorite that decomposes organic substances or water in which ozone is dissolved are used. Produce the effect of.
【００３０】〈実施例４〉上記実施例では、リークが発
生した後、再生操作を行ったが、薬品を連続的に注入し
ても良い。ただし、薬品の使用量が増加する。<Embodiment 4> In the above embodiment, the regeneration operation is performed after the leak occurs, but the chemical may be continuously injected. However, the amount of chemicals used increases.
【００３１】〈実施例５〉上記実施例では、差圧，圧力
の調節をバルブによって行なったが、循環流量の調節な
どによっても行なっても同様の効果を奏する。この場合
でも、差圧計と圧力計が必要である。<Embodiment 5> In the above embodiment, the differential pressure and pressure are adjusted by the valve, but the same effect can be obtained by adjusting the circulation flow rate. Even in this case, a differential pressure gauge and a pressure gauge are required.
【００３２】[0032]
【発明の効果】本発明の再生方法により、高純度の処理
水が得られる。EFFECT OF THE INVENTION By the regeneration method of the present invention, highly purified treated water can be obtained.
【図１】本発明による実施例の系統図。FIG. 1 is a system diagram of an embodiment according to the present invention.
【図２】ＤＢＳ含有液でのリーク特性図。FIG. 2 is a leak characteristic diagram of a DBS-containing liquid.
【図３】ＤＢＳ含有液での蒸発特性図。FIG. 3 is an evaporation characteristic diagram of a DBS-containing liquid.
【図４】ＤＢＳの塩析機構特性図。FIG. 4 is a characteristic diagram of salting-out mechanism of DBS.
【図５】本発明によるＤＢＳ付着膜の洗浄効果の説明
図。FIG. 5 is an explanatory view of the cleaning effect of the DBS adhesion film according to the present invention.
【図６】本発明によるＤＢＳ含有廃液での蒸発再生特性
図。FIG. 6 is a characteristic diagram of evaporative regeneration of a DBS-containing waste liquid according to the present invention.
１…蒸発濃縮器、９…薬液タンク、１０…送風機、１１
…疎水性多孔質膜、１２…蒸発室、１３…冷却室、２６
…差圧計、２１…制御器。1 ... Evaporative Concentrator, 9 ... Chemical Solution Tank, 10 ... Blower, 11
... hydrophobic porous membrane, 12 ... evaporation chamber, 13 ... cooling chamber, 26
… Differential pressure gauge, 21… Controller.
───────────────────────────────────────────────────── フロントページの続き (72)発明者 沢 俊雄 茨城県日立市森山町1168番地 株式会社日 立製作所エネルギー研究所内 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Toshio Sawa 1168 Moriyama-cho, Hitachi-shi, Ibaraki Prefecture Hiritsu Seisakusho Energy Research Institute
Claims (2)
水性多孔質膜を設けた膜蒸発濃縮器によって処理し、清
浄な凝縮水を得る処理方法において、前記疎水性多孔質
膜を設けた前記膜蒸発濃縮器の前記凝縮水側の水圧を廃
液側の水圧よりも高く維持し、前記凝縮水の生成量の低
下を検出して、前記疎水性多孔質膜を有機物を分解する
物質で洗浄し、前記疎水性多孔質膜を乾燥することによ
って疎水性膜を再生することを特徴とする廃液の膜蒸発
濃縮器の再生法。1. A treatment method for obtaining clean condensed water by treating a waste liquid containing a soluble organic substance with a membrane evaporation concentrator having a hydrophobic porous membrane on its evaporation surface, wherein the hydrophobic porous membrane is provided. In addition, the water pressure on the condensed water side of the membrane evaporative concentrator is maintained higher than the water pressure on the waste liquid side, a decrease in the amount of condensed water produced is detected, and the hydrophobic porous membrane is a substance that decomposes organic substances. A method for regenerating a waste liquid membrane evaporator / concentrator, which comprises regenerating the hydrophobic membrane by washing and drying the hydrophobic porous membrane.
水性多孔質膜を設けた膜蒸発濃縮器によって処理し、清
浄な凝縮水を得る処理装置において、少なくとも、前記
疎水性多孔質膜を設けた前記膜蒸発濃縮器の凝縮水側の
水圧を廃液側の水圧よりも高く維持する手段、前記凝縮
水の生成量の低下を検出する手段、前記疎水性多孔質膜
を洗浄する有機物を分解する物質を供給する手段、前記
疎水性多孔質膜を乾燥する手段とからなることを特徴と
する廃液の膜蒸発濃縮装置。2. A treatment device for obtaining clean condensed water by treating a waste liquid containing a soluble organic substance with a membrane evaporative concentrator having a hydrophobic porous membrane on the evaporation surface, at least the hydrophobic porous membrane. Means for maintaining the water pressure on the condensed water side of the membrane evaporative concentrator provided higher than the water pressure on the waste liquid side, means for detecting a decrease in the production amount of the condensed water, and an organic substance for cleaning the hydrophobic porous membrane. An apparatus for evaporating and concentrating a waste liquid film, comprising a means for supplying a substance to be decomposed and a means for drying the hydrophobic porous membrane.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP818292A JPH05192543A (en) | 1992-01-21 | 1992-01-21 | Method and apparatus for regenerating membrane evaporative concentrator of waste fluid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP818292A JPH05192543A (en) | 1992-01-21 | 1992-01-21 | Method and apparatus for regenerating membrane evaporative concentrator of waste fluid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH05192543A true JPH05192543A (en) | 1993-08-03 |
Family
ID=11686170
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP818292A Pending JPH05192543A (en) | 1992-01-21 | 1992-01-21 | Method and apparatus for regenerating membrane evaporative concentrator of waste fluid |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH05192543A (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101388475B1 (en) * | 2011-12-23 | 2014-04-23 | 한국건설기술연구원 | Device for Desalination using De-wetting |
| JP2014188468A (en) * | 2013-03-27 | 2014-10-06 | Mitsubishi Heavy Ind Ltd | Water treatment system for space applications |
| WO2016016301A1 (en) * | 2014-07-29 | 2016-02-04 | Water Technologies Gmbh (In Gründung) | Method for the regeneration of a membrane wall in a distillation device |
| JP2016087545A (en) * | 2014-11-04 | 2016-05-23 | 栗田工業株式会社 | Method for cleaning film distillation apparatus |
| CN108636121A (en) * | 2018-06-19 | 2018-10-12 | 南京航空航天大学 | A kind of membrane distillation coupling MVR concentration strong corrosive solution systems and method |
| KR101991790B1 (en) * | 2018-01-25 | 2019-06-21 | 국민대학교산학협력단 | Apparatus and method for cleaning membrane of membrane distillation module using temperature reversal |
| WO2020158049A1 (en) * | 2019-02-01 | 2020-08-06 | 住友電気工業株式会社 | Method for cleaning hydrophobic porous membrane used in membrane distillation module |
| KR20200093740A (en) * | 2019-01-28 | 2020-08-06 | 고려대학교 산학협력단 | Wastewater treatment system using an electrochemical oxidation and a membrane distillation process and wastewater treatment method using the same |
-
1992
- 1992-01-21 JP JP818292A patent/JPH05192543A/en active Pending
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101388475B1 (en) * | 2011-12-23 | 2014-04-23 | 한국건설기술연구원 | Device for Desalination using De-wetting |
| JP2014188468A (en) * | 2013-03-27 | 2014-10-06 | Mitsubishi Heavy Ind Ltd | Water treatment system for space applications |
| WO2016016301A1 (en) * | 2014-07-29 | 2016-02-04 | Water Technologies Gmbh (In Gründung) | Method for the regeneration of a membrane wall in a distillation device |
| CN106659944A (en) * | 2014-07-29 | 2017-05-10 | 梅杰布拉沃有限公司 | Method for the regeneration of a membrane wall in a distillation device |
| US10029211B2 (en) | 2014-07-29 | 2018-07-24 | Major Bravo Limited | Method for the regeneration of a membrane wall in a distillation device |
| JP2016087545A (en) * | 2014-11-04 | 2016-05-23 | 栗田工業株式会社 | Method for cleaning film distillation apparatus |
| KR101991790B1 (en) * | 2018-01-25 | 2019-06-21 | 국민대학교산학협력단 | Apparatus and method for cleaning membrane of membrane distillation module using temperature reversal |
| CN108636121A (en) * | 2018-06-19 | 2018-10-12 | 南京航空航天大学 | A kind of membrane distillation coupling MVR concentration strong corrosive solution systems and method |
| KR20200093740A (en) * | 2019-01-28 | 2020-08-06 | 고려대학교 산학협력단 | Wastewater treatment system using an electrochemical oxidation and a membrane distillation process and wastewater treatment method using the same |
| WO2020158049A1 (en) * | 2019-02-01 | 2020-08-06 | 住友電気工業株式会社 | Method for cleaning hydrophobic porous membrane used in membrane distillation module |
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