JPS60175504A - Method for washing membrane separation apparatus - Google Patents
Method for washing membrane separation apparatusInfo
- Publication number
- JPS60175504A JPS60175504A JP3206084A JP3206084A JPS60175504A JP S60175504 A JPS60175504 A JP S60175504A JP 3206084 A JP3206084 A JP 3206084A JP 3206084 A JP3206084 A JP 3206084A JP S60175504 A JPS60175504 A JP S60175504A
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- JP
- Japan
- Prior art keywords
- membrane
- water
- solution
- aqueous
- membrane separation
- 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)
Abstract
Description
【発明の詳細な説明】
〔軸間の利用分野」
本発明は膜分離装置の洗浄方法に係り、特に膜分離装置
に装着された嗅の膜面に析出又は付着した汚染ｑＩＢを
簡単かつ確実に剥離除去することができる膜分離装置の
洗浄方法に関する。[Detailed description of the invention] [Field of application between shafts] The present invention relates to a method for cleaning a membrane separation device, and in particular, a method for easily and reliably removing contaminated qIB deposited or attached to the olfactory membrane surface attached to a membrane separation device. The present invention relates to a cleaning method for a membrane separation device that can be peeled and removed.
〔従来１ネ術」
近年、廃水処理、海水の淡水化、純水の製造等各種の水
処坤分野において、逆浸透（ＲＯ）候。[Conventional technique 1] In recent years, reverse osmosis (RO) has been used in various water treatment fields such as wastewater treatment, seawater desalination, and pure water production.
限外ｐ過（ＯＦ）膜又はｆｉｌ ｆｆｉ 濾過膜等の選
択透過膜な内蔵した膜分Ｗａ装置が広く用ｉられて−る
・この膜分離装置は、膜で区画された２つの室の一万（
原液供給室）に処理すべき原液を加圧“上で導入し、他
方の室（処理順１から処理水な取り出すように徊成され
ている。Membrane separation devices with built-in selectively permeable membranes such as ultraviolet filtration (OF) membranes or fil ffi filtration membranes are widely used.・This membrane separation device consists of two chambers separated by membranes. Ten thousand (
The stock solution to be treated is introduced under pressure into the stock solution supply chamber (stock solution supply chamber), and the treated water is taken out from the other chamber (processing order 1).
膜分離装置に装着される膜はエレメントの形状により、
平板型膜、管型模、渦番型模、中空糸型膜、襞型嗅、に
大別され、その材質としてｒ［、−６Ｋ、 酢ｔｉｔセ
ルロース、ポリスルホン。The membrane installed in the membrane separator depends on the shape of the element.
It is roughly divided into flat plate membrane, tube type membrane, vortex type membrane, hollow fiber type membrane, and fold type membrane, and its materials include r[, -6K, vinegar tit cellulose, and polysulfone.
ポリエナレン、ポリプロピレン、ポリアクリロニトリル
、ポリアミド、ポリ塩化ビニル、ボ゛リビニルアルコー
ル、ポリイミド、ポリ酢殴ビニル等が用いられている。Polyenalene, polypropylene, polyacrylonitrile, polyamide, polyvinyl chloride, polyvinyl alcohol, polyimide, polyvinyl acetate, and the like are used.
膜分離装置ｖ長時間運転することにより、原液中に含Ｍ
される檎々の無機ｑａ負又は有機物置あるいはヌライム
等が膜面に付着し、汚染（ファウリングンさせる。しか
して、膜汚染により。Membrane separation equipment v By operating for a long time, the M content in the stock solution increases.
Inorganic QA negative or organic substances such as nulimes, etc., adhere to the membrane surface and cause contamination (fouling).As a result, membrane contamination occurs.
■ 膜面が閉基し、透過水量が低）する（採水量低下）
、
■ 膜分離装置出入口の差圧が増加し、膜エレメントに
対する吻埋的貝句な増す（差圧増加）。■ Membrane surface is closed and permeated water volume is low (lower water collection volume)
, ■ The differential pressure at the entrance and exit of the membrane separation device increases, and the pressure difference against the membrane element increases (differential pressure increase).
■ 一定量の透過水を得るためには、原水ポンプ圧を嶋
める必費がでてくる（゛成力消費増加）、
■ 処理水の水質低重、
■ 汚れによる映寿命の短幅。■ In order to obtain a certain amount of permeated water, it becomes necessary to increase the raw water pump pressure (increase in raw power consumption), ■ the quality of the treated water is low, and ■ the film life is shortened due to contamination.
静様々な障害が生起し、膜分１１ｉｌｌ装置の愼餌ぞ低
下させる。Various disturbances occur and reduce the capacity of the membrane 11ill device.
従って、膜分離装置の愼岨回俵のために、恢米、ば、ア
ルカリ、酸化剤、還元剤、キレート剤、酵素等の薬品で
膜を洗浄することにより、膜付着物をａＭ１剥襟させ除
去する方法が、−敗に採用されてｉる。Therefore, in order to recycle the membrane separation equipment, the membrane is cleaned with chemicals such as rice, alkali, oxidizing agents, reducing agents, chelating agents, and enzymes to remove the membrane deposits. The method of removal is adopted in a negative manner.
しかしながら、渦＠型膜エレメント等ｒｌｔｉＩＬ常の
ｌｌｃ＃方法では差圧回復効果が小名い場合か多い。差
圧が十分４ＣＪ！！Ｉ復６れなｉと、再運転の際の差圧
上昇が急激に生じる、透過水ｆ確保のために装置の運転
圧力な上ける必歎が生じる。また、膜エレメントが変形
する等の問題が生起することとなる。（このような玩象
框、膜付着物がスライム貞主体である場合にＩＩ′ｉ特
に顕著である）。これは、勧善型では、その構造上、か
なりの跣流を与えなφと膜付Ｎ物の味去が十分に行なえ
ないためであると考えられている。このため、気体発生
＃ｃｔにより、況浄時に気泡１に混入させる方法も検討
されているが、設備、操作が仮雑となり、有効な方法と
は舊えなめ。However, in the rltiIL and usual llc# methods such as vortex@ type membrane elements, the differential pressure recovery effect is often insignificant. The differential pressure is 4CJ! ! When restarting the system, a sudden rise in differential pressure occurs, and it becomes necessary to increase the operating pressure of the device in order to secure permeate water. Further, problems such as deformation of the membrane element will occur. (II'i is particularly noticeable when such fictitious objects and membrane deposits are mainly slime). This is thought to be because the Kanzen type cannot sufficiently remove the taste of the φ and membrane-attached N substances due to its structure, which does not cause a considerable amount of cross-flow. For this reason, a method of mixing gas into the bubbles 1 during cleaning using gas generation #ct has been considered, but the equipment and operations would be complicated and it would not be an effective method.
その池、汚染した逆良透換を過取化水素浴歇で洗浄しつ
つ、さらに圧力変動を加えることにより付着物を隙去す
る方法（特公昭５５−３７２８８号）も提案されている
が、短時間とはいえ、モジ為−ル内の圧力％：急激によ
′ｉ−嘔せると１便が支持体から剥れたり、装置全体に
振ｍ’ｈ：与える幀釆模の劣化や装置の脆弱化な招いた
り、計装上４ｉｌ鑵になりｆｃ９する寺の問題がるり、
必ずしも満足すべき方法とＩＩｉ言えない。A method has also been proposed (Japanese Patent Publication No. 55-37288) in which the polluted reverse permeation of the pond is washed with a hydrogen peroxide bath and the deposits are removed by applying pressure fluctuations. Even if the pressure inside the module is short-lived, sudden vomiting may cause the stool to peel off from the support or shake the entire device, causing deterioration of the container and damaging the device. This may lead to the weakening of the FC9, or the problem of the FC9 due to the 4il failure on the instrumentation.
This cannot necessarily be said to be a satisfactory method.
〔発明の目的」
本発明は上記実情に鑑みてな妊れたものであり、その１
的とするところは、膜分離装置の膜に析出、付着した汚
染り卵質ｔ、極めて幼果的に沈＃除去することができる
、膜分離装置の此伊方法を提供することにある。[Object of the invention] The present invention was conceived in view of the above-mentioned circumstances.
The aim is to provide a method for a membrane separator that can remove contaminants and egg matter deposited and adhered to the membrane of the membrane separator in a very immature manner.
この目的な達成するために１本発明省は膜の洗浄方法に
つ＠鋭意検討を重ねた精米、抗浄剤により洸＃を実施し
て帳面の汚染物な剥れ易くした仮、この使用ｔｋ、ｆｐ
剤を分解して気泡を発生させるｇＪ員を踊加し、気泡に
より暎而の汚染物ｆｔｌ７Ｊ制的に剥離させる方法が、
扉【す剤乞Ｍ幼かつ簡単に利用でき、渦巻型膜分離装置
の洗浄にも極めて幼果的であることを見い出し、本発明
に到達した。In order to achieve this objective, the Ministry of the Invention has carefully studied the method of cleaning the membrane and carried out cleaning using an anti-detergent agent to make it easier for contaminants to peel off from the book. , fp
There is a method in which a material that decomposes the agent and generates air bubbles is added, and the air bubbles are used to selectively remove the contaminants.
We have discovered that the door is simple and easy to use, and that it is extremely effective for cleaning spiral membrane separation devices, and have arrived at the present invention.
即ち、本発明は
膜分謙ｔｃｆＩＬに過酸化水系含有液を供給し、仄ｉで
カタラーセ含有液を供給することを特徴とする膜分離装
置の洗浄方法、
を費旨とするものでるる。That is, the present invention is directed to a method for cleaning a membrane separation device, characterized in that a peroxide-based liquid is supplied to a membrane separator (tcfIL), and a catalase-containing liquid is supplied at a second time.
以下に本発明につき詳細に説明する。The present invention will be explained in detail below.
不発明の洗浄方法に２いてＩＩｉ、まず膜分離装置に過
酸化水素含有液を供給する。過ば化水素含有液としテｕ
［２０！ａ ＆ ０．０１〜１０ ｊＩＬｆｉ １６
．好ましくは０．０５〜３重量−の水溶液が好適である
。In the uninvented cleaning method 2, first, a hydrogen peroxide-containing liquid is supplied to the membrane separator. Hydrogen perbide containing liquid
[20! a & 0.01~10 jILfi 16
．． Preferably, a 0.05 to 3 weight aqueous solution is suitable.
この溶液のｐＲｒｔ５〜９の軛拙が好ましい。A pRrt of 5 to 9 for this solution is preferred.
過鈑化水素含４Ｔ液の通液な行なうには、洗浄慴に過戚
化水′ＪＡ含有液を供給し、まずポンプにより過酸化水
素含有液を況＃壇と膜分離装置に循環通液し、久φで装
置内で幌と過酸化水系含有液とを静置接触させる。過酸
化水素含有液の通液条件としては、圧力通常運転圧以ト
、水意は通常運転水皿の５０〜２００％、 備狽汲触時
間Ｆｉ１５〜１２０分とするのが好ましい。また、静置
接触時間は１〜３０時間、好ましくは６〜２４時間が好
複し９゜
静１１を接触仮、再反過敲化水素含Ｍ畝を通敵循壌する
。この際に、過酸化水素含弔液に過酸化水素分屏智貝で
あるカタラーゼを献加する。カメラーゼの礒加−ｍμ、
カタラーゼ＃［が０．１〜５１’９／１．好１ Ｌ （
Ｈ０，５〜１．５Ｗ／Ｊ！ トナｂ ｊ ウにするのが
好ましい。迫ｇ、儂壌条件として口、前述の初期の通液
循環の際の圧力、水皿と同程度で良く、儂猿接劇時間ｒ
Ｊ１５〜６０分が好ましい。To pass the 4T solution containing hydrogen peroxide, first supply the solution containing superoxide water'JA to the washing tank, first circulate the hydrogen peroxide containing solution through the chamber and the membrane separation device using a pump, and then The hood and the peroxide-based liquid are allowed to come into contact with each other in the apparatus with a long diameter. The conditions for passing the hydrogen peroxide-containing liquid are preferably such that the pressure is below the normal operating pressure, the water level is 50 to 200% of the normal operating water tray, and the contact time Fi is 15 to 120 minutes. Further, the standing contact time is preferably 1 to 30 hours, preferably 6 to 24 hours, and the mixture is kept at 9° for a period of time of 11 hours, and the mixture is circulated through the hydrogen-containing M ridge. At this time, catalase, which is a hydrogen peroxide-containing shell, is added to the hydrogen peroxide-containing mortuary solution. Addition of camerase-mμ,
Catalase # [is 0.1-51'9/1. Good 1 L (
H0.5~1.5W/J! It is preferable to set the value to b j . The pressure during the initial liquid circulation as described above should be about the same as that of the water dish, and the monkey contact time r.
J15 to 60 minutes is preferable.
沈沖１ズ、模透過水寺の消は水で水フラッシングを行な
い、装置内を十分に水成６奢して終了する。水フラッシ
ング条件としては、圧力は辿冨運転圧以）、水型は通に
運転水址の１００〜２００チ、フラッシング時間に５〜
３０分が好適で必る。When the process is completed, the water is flushed with water and the inside of the device is sufficiently filled with water. The water flushing conditions are as follows: the pressure is below the operating pressure), the water type is 100 to 200 inches of water, and the flushing time is 5 to 200 inches.
30 minutes is preferable and necessary.
本発明の方法に２いてμ、尻凌効果ン尚めるために、過
ば化水索冨有液にアニオン基又１まノニオン系界面Ｔ占
性剤を硝加するのが好ましい。In the method of the present invention, it is preferable to add an anionic or nonionic interfacial T-occupant agent to the peroxidized water-containing liquid in order to improve the μ and lag effects.
界面活性剤の硝加には、その磯度が０．０５〜０．３重
′ｊＩｋｔｌｌ程度となるようにするのが好ましい。ア
ニオン系界面活性剤の具体例としては、アルキルペンセ
ンスルホン戚、尚級アルコール憾酸エステル、アルキル
硫欧エステル、アルキルヌルホンＩＬアルキルスルホコ
ハク瞭、ジアルキルスルホコハク戚、アルキルナフタリ
ンスルホン敵−ホルマリン縮合ｖｌＪ、 ｊルキルナフ
タリンスルホン戚及びそれらの塩等が挙けられ、ノニオ
ン系界面活性剤の具体例として框、ポリオキシエチレン
アルキルエーテル、ポリオキシエチレンアルキルアリー
ルエーテル、ホリエナレングリコール脂肪戚エステル、
ポリオキシエチレンＪ１ば肪酸アミドエーテル、多価ア
ルコール脂肪ばエステル、アルキロールアミド等が争け
りれる。When adding nitrate to the surfactant, it is preferable to adjust the degree of roughness to be about 0.05 to 0.3 weight. Specific examples of anionic surfactants include alkylpensene sulfones, higher alcohol acetic acid esters, alkylsulfosulfone esters, alkylnulphone IL alkylsulfosuccinates, dialkylsulfosuccinates, alkylnaphthalenesulfones-formalin condensation vlJ, Examples of nonionic surfactants include sulfone, polyoxyethylene alkyl ether, polyoxyethylene alkylaryl ether, polyenalene glycol fatty ester,
Polyoxyethylene J1 fatty acid amide ether, polyhydric alcohol fatty acid ester, alkylol amide, etc. are in contention.
本発明に２いてをユ、映汚染１勿の―鑓に応じて、遇叡
化水素台Ｍａにアルカリ、酸化剤、還元剤。In the present invention, according to the present invention, alkali, oxidizing agent, and reducing agent are added to hydrogen chloride, depending on the contamination.
分散剤、＃素、有ＭＡ俗媒寺七の他の暉〃ロ剤Ｙ：龜刀
口することもでさる。Dispersants, #base, and other dispersing agents Y: You can also use them.
本発明によれば、まず過ば１し水素言刹敢ン膜と接触さ
せて、暎１ｆｌｌの汚染物を剥離し易い状態にさせた仮
、過岐化水素？分解して気泡？発生せしめるカメラーゼ
を麻加して、気泡量ＩＰで通准佑猿させることにより、
気泡の乱流幼米で汚染Ｗを偵央に剥離除去することがで
きる。According to the present invention, hydrogen peroxide is first brought into contact with the hydrogen membrane to make it easy to peel off the contaminants. Does it decompose into bubbles? By controlling the generated camerase and controlling it with the amount of bubbles IP,
Contaminated W can be thoroughly peeled off and removed by the turbulent flow of air bubbles.
〔発明の実施例〕
以１に本先明ｆＪｒ：実施例により更に具体的に説明す
るが、不軸間はその戦旨を鳩えない限り以１：の実施例
に限定芒れるものではない。[Embodiments of the Invention] Hereinafter, the present invention will be explained in more detail with reference to the following examples, but the invention is not limited to the embodiments in 1: unless the purpose of the war is reflected. .
実施例１
市水な活性炭処理、ミックスベッド処理、ＵＶ殺菌処！
ｊｕ ｌ、た住、Ｈ東鬼気工業株式会仕製渦巻型限外濾
過１臭分ｌＩ！Ｉ装置に、圧力３〜５即／ｄ。Example 1 Activated carbon treatment, mixed bed treatment, and UV sterilization for city water!
Ju l, Tasumi, H Touki Kogyo Co., Ltd. Spiral type ultrafiltration 1 odor content lI! I device, pressure 3-5 instant/d.
水ｊｔ １．５ ｍ’／ ｂｒで６ケ月間通水処理した
。この１ＦｊＪ、遍ぼ１し水系浴液で１回此浄を何なっ
た。Water flow treatment was carried out for 6 months with water jt 1.5 m'/br. This 1FjJ, I used this water-based bath liquid once every 1 time.
この模分陣鉄置ン、谷々）記表ＩＫボ丁仇伊液を用い、
ノ戯次にｉｌｌ欣偵槙（熾１）（圧力１．０ｋｌ？／１
−１１１ ％水ｋｓ００Ｊ／ｈｒ、循狽時ｉＭｊ ｌ
５分）→静止接触（接触時間２時間）→通′ｔＬｖＩｉ
嬢（嵐２）（条件ｄＮｎｌの通液循環と同じ）→水フラ
ッシング（フラッシング時間５分）することにより洗浄
し、洗浄後の限外ｐ過膜の性能を倉品限外Ｖ過嗅及び（
ｋ、＃なしない汚染限外濾過嗅の性能と比較した。結末
な表１に示す。Using this Moibunjin Tetsuin, Taniya) notation IK Bocho Chii liquid,
Nogi next ill 欣detective (熾1) (pressure 1.0kl?/1
-111% water ks00J/hr, iMj l during circulation
5 minutes) → Stationary contact (contact time 2 hours) → Time'tLvIi
(Arashi 2) (same conditions as dNnl liquid circulation) → Clean by water flushing (flushing time 5 minutes), and the performance of the ultrap membrane after cleaning was evaluated by Kurashin UltraV hyperosmosis and (
k, # compared with the performance of ultrafiltration without contamination. The results are shown in Table 1.
なお、膜の性能は、各々の膜分離装置に、人口圧１．１
ｋｐ／ｃｄ、水１８００Ｊ／ｈｒにおいて３０分純水
を通水した後の、幌の差圧乞徂ｉｊ定することによりテ
ストした。The performance of the membrane is determined by the population pressure of 1.1 for each membrane separation device.
The test was conducted by determining the differential pressure of the hood after passing pure water for 30 minutes at kp/cd and 1800 J/hr of water.
表 １
Ｍ ： ０．５４ＪＭｚＬ）ｚ俗ＦＩＩ（ＰＨ７）Ｈ＋
Ｃ： ０．５ ｆｙ ＭｚＬｈ 溶液にカタラーゼｌ−
ｖ＃Ｙｈ５≦加したｍ歇（ｐｉｔ ７ ）
表１より不発明の方法によれは、差圧の回復が極めて良
好でめり、α＃幼幼果曖れていることが認められる。ま
た比較方法２の如く、初回からカタラーゼを含有τる山
０２溶液で杭葎しても、洸＃効果は良くないことが明ら
かでおる。Table 1 M: 0.54JMzL)z Common FII (PH7)H+
C: Catalase l- in 0.5 fy MzLh solution
v#Yh5≦added m interval (pit 7) From Table 1, it can be seen that in the uninvented method, the recovery of the differential pressure was very good, and α# young and young fruits were lost. Furthermore, it is clear that even if the seedlings are plucked with a catalase-containing Yama02 solution from the beginning, as in Comparative Method 2, the effect is not good.
以上詳述した如く、本発明の膜分′Ｎ１装置の沈砂方法
は、Ｈ２Ｏ２で膜に付着したスケール、クライム類等を
剥れ易くシ、仄いて°、カタラーゼを６≦加して１１ｚ
（Ｊｚ ’（！’ ｆ） Ｈし、気を包を発生させるこ
とにより付着吻を模かも電制剥離するようにしたもので
少り、模面に析出、付層した汚染物を容易かつ確実に味
去することがでぴる。しかして。As detailed above, the method for settling the membrane N1 apparatus of the present invention is to use H2O2 to easily remove scales, climbs, etc. attached to the membrane.
(Jz '(!' f) H) It is designed to electrically peel off the adhering proboscis by generating air bubbles, so it can easily and reliably remove contaminants deposited and attached to the pattern. However, it is possible to remove the taste.
従米、系品抗浄のみでは除去困−であったスライム負等
の除去Ｖこもイ（効でろり、°また勧善型膜エレメント
の′ｄｉ、＃にも極めてＭ幼でろる。従って、本発明の
方法によれば、量率な方法で確実に、１漠汚染による走
圧上昇等の障害を回復することができ、工業的に極めて
有利である。It is very effective to remove slime, etc., which is difficult to remove with conventional anti-cleaning methods alone. According to the method of the invention, it is possible to reliably recover from problems such as an increase in running pressure caused by a single contamination in a quantitative manner, which is extremely advantageous industrially.
特奸出狐人 栗田工業株式会社Special Foxman Kurita Industries Co., Ltd.
Claims (4)
でカタラーゼ含有液を供′給することを特徴とする膜分
離装置の洗浄方法。(1) A method for cleaning a membrane separation device, comprising supplying a hydrogen peroxide-containing solution to the membrane separation device, and then supplying a catalase-containing solution.
ものであることを特徴とする特許請求の範囲第１項に記
載の方法。(2) The method according to claim 1, wherein the membrane separation device is equipped with a reverse osmosis membrane or an ultrafiltration membrane.
特徴とする特許請求の範囲第１項又は第２項に記載の方
法。(3) The method according to claim 1 or 2, wherein the hydrogen peroxide-containing liquid contains a surfactant.
ーゼを添加してなることを特徴とする特ｆ！ｆｆ請求の
範囲第１項ないし第３項のいずれか１項に記載の方法。(4) The catalase-containing liquid is made by adding catalase to a hydrogen peroxide-containing liquid! ff The method according to any one of claims 1 to 3.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3206084A JPS60175504A (en) | 1984-02-22 | 1984-02-22 | Method for washing membrane separation apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3206084A JPS60175504A (en) | 1984-02-22 | 1984-02-22 | Method for washing membrane separation apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS60175504A true JPS60175504A (en) | 1985-09-09 |
| JPH0131403B2 JPH0131403B2 (en) | 1989-06-26 |
Family
ID=12348334
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3206084A Granted JPS60175504A (en) | 1984-02-22 | 1984-02-22 | Method for washing membrane separation apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS60175504A (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62294406A (en) * | 1986-06-11 | 1987-12-21 | Japan Organo Co Ltd | Washing method for hollow yarn module |
| JPS63270595A (en) * | 1987-04-30 | 1988-11-08 | Kurita Water Ind Ltd | Treatment of wafer process waste water |
| US5240613A (en) * | 1991-08-15 | 1993-08-31 | Maruzen Petrochemical Co., Ltd. | Process for regenerating clogged filters |
| JP2002045660A (en) * | 2000-08-01 | 2002-02-12 | Mitsubishi Rayon Co Ltd | Method for handling membrane module |
| JP2003024754A (en) * | 2001-07-17 | 2003-01-28 | Maezawa Ind Inc | Membrane module washing method |
| WO2007026867A1 (en) * | 2005-09-01 | 2007-03-08 | Novel Technology Co., Ltd. | Separation membrane washing composition |
| JP2019501775A (en) * | 2015-12-16 | 2019-01-24 | エコラブ ユーエスエイ インク | Peroxyformic acid composition for membrane filtration purification |
| US10524470B2 (en) | 2016-12-15 | 2020-01-07 | Ecolab Usa Inc. | Peroxyformic acid compositions for membrane filtration cleaning in energy services |
| US11241009B2 (en) | 2016-04-15 | 2022-02-08 | Ecolab Usa Inc. | Performic acid biofilm prevention for industrial CO2 scrubbers |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS54162684A (en) * | 1978-06-14 | 1979-12-24 | Ebara Infilco Co Ltd | Preliminary treating method for contaminated membrane |
-
1984
- 1984-02-22 JP JP3206084A patent/JPS60175504A/en active Granted
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS54162684A (en) * | 1978-06-14 | 1979-12-24 | Ebara Infilco Co Ltd | Preliminary treating method for contaminated membrane |
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62294406A (en) * | 1986-06-11 | 1987-12-21 | Japan Organo Co Ltd | Washing method for hollow yarn module |
| JPS63270595A (en) * | 1987-04-30 | 1988-11-08 | Kurita Water Ind Ltd | Treatment of wafer process waste water |
| JPH0722752B2 (en) * | 1987-04-30 | 1995-03-15 | 栗田工業株式会社 | Wafer process wastewater treatment method |
| US5240613A (en) * | 1991-08-15 | 1993-08-31 | Maruzen Petrochemical Co., Ltd. | Process for regenerating clogged filters |
| JP2002045660A (en) * | 2000-08-01 | 2002-02-12 | Mitsubishi Rayon Co Ltd | Method for handling membrane module |
| JP4536227B2 (en) * | 2000-08-01 | 2010-09-01 | 三菱レイヨン株式会社 | Handling method of membrane module |
| JP2003024754A (en) * | 2001-07-17 | 2003-01-28 | Maezawa Ind Inc | Membrane module washing method |
| WO2007026867A1 (en) * | 2005-09-01 | 2007-03-08 | Novel Technology Co., Ltd. | Separation membrane washing composition |
| JP2019501775A (en) * | 2015-12-16 | 2019-01-24 | エコラブ ユーエスエイ インク | Peroxyformic acid composition for membrane filtration purification |
| US10737302B2 (en) | 2015-12-16 | 2020-08-11 | Ecolab Usa Inc. | Peroxyformic acid compositions for membrane filtration cleaning |
| US11117172B2 (en) | 2015-12-16 | 2021-09-14 | Ecolab Usa Inc. | Peroxyformic acid compositions for membrane filtration cleaning |
| US11241009B2 (en) | 2016-04-15 | 2022-02-08 | Ecolab Usa Inc. | Performic acid biofilm prevention for industrial CO2 scrubbers |
| US11882826B2 (en) | 2016-04-15 | 2024-01-30 | Ecolab Usa Inc. | Performic acid biofilm prevention for industrial CO2 scrubbers |
| US10524470B2 (en) | 2016-12-15 | 2020-01-07 | Ecolab Usa Inc. | Peroxyformic acid compositions for membrane filtration cleaning in energy services |
| US11026420B2 (en) | 2016-12-15 | 2021-06-08 | Ecolab Usa Inc. | Peroxyformic acid compositions for membrane filtration cleaning in energy services |
| US11647747B2 (en) | 2016-12-15 | 2023-05-16 | Ecolab Usa Inc. | Peroxyformic acid compositions for membrane filtration cleaning in energy services |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0131403B2 (en) | 1989-06-26 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EXPY | Cancellation because of completion of term |