JPH1176769A - Cleaning method of filter membrane module - Google Patents
Cleaning method of filter membrane moduleInfo
- Publication number
- JPH1176769A JPH1176769A JP25129097A JP25129097A JPH1176769A JP H1176769 A JPH1176769 A JP H1176769A JP 25129097 A JP25129097 A JP 25129097A JP 25129097 A JP25129097 A JP 25129097A JP H1176769 A JPH1176769 A JP H1176769A
- Authority
- JP
- Japan
- Prior art keywords
- filtration membrane
- membrane module
- cleaning
- filtration
- filter membrane
- 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.)
- Withdrawn
Links
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、濾過膜モジュール
の洗浄方法に関し、特に、濾過膜モジュールを薬液によ
り洗浄して透水性能を回復させる場合、短時間の洗浄で
透水性能を回復させ、洗浄後も長期にわたり安定運転を
可能とする濾過膜モジュールの洗浄方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method of cleaning a filtration membrane module, and more particularly to a method of cleaning a filtration membrane module with a chemical solution to restore water permeability, by recovering the water permeability with a short time of washing, and after cleaning. The present invention also relates to a method for cleaning a filtration membrane module that enables stable operation for a long time.
【０００２】[0002]
【従来の技術及び発明が解決しようとする課題】従来、
透水性能が低下した濾過膜モジュールを薬液で洗浄する
方法として、例えば、透過液室の圧力と原液室の圧力を
等しくした状態で薬液を循環させる濾過膜モジュールの
洗浄方法が特開昭６１−１１１０８号公報に開示されて
いる。また、特開平３−７７６２９号公報や特開平４−
１６１２３２号公報には、透過側から薬液を加圧注入す
る濾過膜モジュールの洗浄方法が開示されている。しか
しながら、薬液のみの単独の洗浄方法では十分な洗浄効
果が得られないという問題点がある。洗浄効果が不十分
な場合、従来の方法では薬液の使用量を増したり、薬洗
時間を延ばして洗浄効果を上げる方法がとられている。2. Description of the Related Art
As a method of cleaning a filtration membrane module having reduced water permeability with a chemical, for example, a method of cleaning a filtration membrane module in which a chemical is circulated in a state in which the pressure of a permeate chamber is equal to the pressure of a stock solution chamber is disclosed in JP-A-61-11108. No. 6,086,045. Further, Japanese Patent Application Laid-Open No. 3-77629 and Japanese Patent Application Laid-Open
Japanese Patent No. 161232 discloses a method for cleaning a filtration membrane module in which a chemical solution is injected under pressure from the permeation side. However, there is a problem that a sufficient cleaning effect cannot be obtained by a single cleaning method using only a chemical solution. In the case where the cleaning effect is insufficient, in the conventional method, a method of increasing the use amount of the chemical solution or extending the chemical cleaning time to enhance the cleaning effect has been adopted.
【０００３】また、透過側から気体を圧入する濾過膜モ
ジュールの洗浄方法としては、例えば、専門誌 ”膜”
Vol.20 No.5, p328(1995)に開示されている。これは、
透過側から圧入された気体が濾過膜を瞬時に通過して目
詰まり物質を取り除き、濾過流束を維持する逆洗方法で
ある。しかしながら、この気体の圧入が薬液洗浄工程に
おける洗浄方法ではないため、酸化鉄や酸化マンガンな
どの濾過膜への吸着物質は除去することができないとい
う問題点がある。[0003] As a method for cleaning a filtration membrane module into which gas is injected from the permeation side, for example, a specialty magazine “Membrane” is used.
Vol.20 No.5, p328 (1995). this is,
This is a backwashing method in which gas injected from the permeation side instantaneously passes through a filtration membrane to remove clogged substances and maintain a filtration flux. However, since this gas injection is not a cleaning method in the chemical liquid cleaning step, there is a problem that adsorbed substances such as iron oxide and manganese oxide on the filtration membrane cannot be removed.
【０００４】そこで、本発明は、濾過膜の薬液洗浄工程
において、濾過膜への吸着物質の十分な除去ができ、洗
浄効果を向上でき、かつ薬液の使用量を減らすととも
に、短時間で薬液洗浄が行え、さらに、洗浄コストを下
げることのできる濾過膜モジュールの洗浄方法を提供す
ることを目的とする。Accordingly, the present invention provides a method for cleaning a chemical solution in a filtration membrane in a short time, in which a substance adsorbed on the filtration membrane can be sufficiently removed, a cleaning effect can be improved, and the amount of the chemical solution used can be reduced. It is another object of the present invention to provide a method for cleaning a filtration membrane module, which can reduce the cleaning cost.
【０００５】[0005]
【課題を解決するための手段】本発明者らは、濾過膜モ
ジュールの薬液洗浄工程の洗浄方法において、薬液の濾
過膜モジュールへの供給と気体の濾過膜への加圧のタイ
ミング等につき種々検討の結果、その加圧のタイミング
及び気体の加圧による洗浄効果に大きな差異を見いだ
し、且つ、濾過膜の種類、薬液の組み合わせ、薬液洗浄
の順序回数等につき種々検討の結果、短時間に優れた洗
浄効果が得られることを見いだし、本発明を完成するに
至った。Means for Solving the Problems The inventors of the present invention have made various studies on the timing of supply of a chemical solution to a filtration membrane module and pressurization of gas to a filtration membrane in a method of cleaning a filtration membrane module with a chemical solution. As a result, a great difference was found in the timing of pressurization and the cleaning effect due to pressurization of gas, and as a result of various studies on the type of filtration membrane, the combination of chemicals, the number of times of chemical cleaning, etc., the results were excellent in a short time. The inventors have found that a cleaning effect can be obtained, and have completed the present invention.
【０００６】すなわち、本発明の濾過膜モジュールの洗
浄方法は、水の膜浄化システムの透水性能が低下した濾
過膜モジュールを薬液によって洗浄して透水性能を回復
させる濾過膜モジュールの洗浄方法において、 薬液を
濾過膜モジュールに供給する前あるいは後のいずれか一
方またはその両方の時点で、気体を濾過膜モジュールの
濾過膜の透過側から圧力２０ｋＰａ以上バブルポイント
未満で加圧する気体加圧工程を０．１〜５分間設けるこ
とを特徴とするものである。That is, a method for cleaning a filtration membrane module according to the present invention is a method for cleaning a filtration membrane module, in which a filtration performance of a filtration membrane module having reduced water permeability of a water membrane purification system is restored by a chemical solution to recover the water permeability. A gas pressurizing step of pressurizing the gas at a pressure of 20 kPa or more and less than the bubble point from the permeation side of the filtration membrane of the filtration membrane module before and / or after supplying the gas to the filtration membrane module. It is characterized by being provided for up to 5 minutes.
【０００７】また、本発明の濾過膜モジュールの洗浄方
法は、水が、表流水であることを特徴とするものであ
る。Further, the method for cleaning a filtration membrane module of the present invention is characterized in that the water is surface water.
【０００８】また、本発明の濾過膜モジュールの洗浄方
法は、濾過膜が、限外濾過膜であることを特徴とするも
のである。[0008] The method for cleaning a filtration membrane module of the present invention is characterized in that the filtration membrane is an ultrafiltration membrane.
【０００９】また、本発明の濾過膜モジュールの洗浄方
法は、濾過膜モジュールが、中空糸膜からなる中空糸膜
モジュールであることを特徴とするものである。[0009] The method for cleaning a filtration membrane module of the present invention is characterized in that the filtration membrane module is a hollow fiber membrane module comprising a hollow fiber membrane.
【００１０】また、本発明の濾過膜モジュールの洗浄方
法は、濾過膜の膜材質が、酢酸セルロースであることを
特徴とするものである。[0010] The method for cleaning a filtration membrane module of the present invention is characterized in that the membrane material of the filtration membrane is cellulose acetate.
【００１１】また、本発明の濾過膜モジュールの洗浄方
法は、薬液による洗浄（薬液洗浄とも略す）が、クエン
酸、界面活性剤及び次亜塩素酸ナトリウムのうちから選
択される一種もしくは二種の組み合わせまたは１段もし
くは多段に組み合わて行うことを特徴とするものであ
る。Further, in the method for cleaning a filtration membrane module of the present invention, the cleaning with a chemical solution (also abbreviated as chemical solution cleaning) is performed by one or two types selected from citric acid, a surfactant and sodium hypochlorite. It is characterized in that it is performed in combination or in one or more stages.
【００１２】[0012]
【発明の実施の形態】本発明において、気体の加圧は薬
液を濾過膜モジュールに供給する前あるいは後のいずれ
か一方またはその両方の時点で行ってよいが、薬液を供
給する前あるいは両方が好ましい。濾過膜面に付着した
目詰まり物質を予め物理的に除去し、その後の薬液によ
る洗浄効果を上げる理由から、薬液を濾過膜モジュール
に供給する前が最も好ましい。本発明の濾過膜モジュー
ルの洗浄方法において、気体を濾過膜モジュールの濾過
膜の透過側から導入する圧力は、２０ｋＰａ以上バブル
ポイント未満であり、好ましくは４０ｋＰａ以上１５０
ｋＰａ以下である。ここに、気体の圧力を２０ｋＰａ以
上バブルポイント未満としたのは、圧力が２０ｋＰａよ
り低いと洗浄効果が不十分であり、目的とする洗浄回復
性が得られず、また、圧力がバブルポイント以上では濾
過膜モジュールに物理的ダメージを与えてしまうからで
ある。ここに、バブルポイントは濾過膜の材質、濾過膜
の分画分子量または膜孔径にもよるが、例えば膜孔径
０．１μｍの酢酸セルロース膜では約３００ｋＰａであ
る。DESCRIPTION OF THE PREFERRED EMBODIMENTS In the present invention, gas pressurization may be performed before or after supplying a chemical solution to a filtration membrane module, or at both times. preferable. It is most preferable before the chemical solution is supplied to the filtration membrane module, because the clogging substance adhering to the filtration membrane surface is physically removed in advance, and the cleaning effect by the subsequent chemical solution is improved. In the method for cleaning a filtration membrane module of the present invention, the pressure at which gas is introduced from the permeation side of the filtration membrane of the filtration membrane module is 20 kPa or more and less than the bubble point, preferably 40 kPa or more and 150 kPa or more.
kPa or less. Here, the reason why the gas pressure is set to 20 kPa or more and less than the bubble point is that if the pressure is lower than 20 kPa, the cleaning effect is insufficient, the intended cleaning recovery property cannot be obtained, and if the pressure is higher than the bubble point. This is because physical damage is given to the filtration membrane module. Here, the bubble point depends on the material of the filtration membrane, the molecular weight cut off of the filtration membrane or the pore diameter of the membrane, but is, for example, about 300 kPa for a cellulose acetate membrane having a membrane pore diameter of 0.1 μm.
【００１３】また、気体加圧工程では、気体を膜の透過
側に導入する際、気体は濾過膜を透過し原水側に押し出
される必要はなく、気体が濾過膜の透過側から膜厚内部
に圧入されていればよい。このような気体による圧入を
行うと、気体が濾過膜モジュール内の濾過膜全体の膜厚
内部に侵入し、汚染した濾過膜の目詰まり物質を押し出
すため、濾過膜モジュール内部が均一に洗浄できるとい
う特長があるからである。通常の逆洗のように液体（薬
液）を濾過膜モジュールの透過側から加圧すると、液体
が膜面の比較的に目詰まりのない部分を透過してしま
い、目詰まり部分を透過しにくいため、目詰まり部分を
洗浄することができず、濾過膜の不均一な洗浄となる。In the gas pressurizing step, when introducing gas to the permeation side of the membrane, the gas does not need to permeate through the filtration membrane and be pushed out to the raw water side, and the gas flows from the permeation side of the filtration membrane to the inside of the membrane. It only needs to be press-fitted. When such gas injection is performed, the gas penetrates into the entire thickness of the filtration membrane in the filtration membrane module and pushes out the clogged substance of the contaminated filtration membrane, so that the inside of the filtration membrane module can be uniformly washed. This is because it has features. When a liquid (chemical liquid) is pressurized from the permeate side of the filtration membrane module as in normal backwashing, the liquid permeates relatively unclogged portions of the membrane surface and is less likely to permeate clogged portions. In addition, the clogged portion cannot be washed, resulting in uneven washing of the filtration membrane.
【００１４】また、気体の加圧時間（気体加圧工程）
は、気体が濾過膜モジュール内の濾過膜の全ての透過側
に実質的に加圧されている時間であり、０．１〜５分間
が望ましいが、洗浄効果と効率を考慮すると、好ましく
は０．５〜２分間である。ここに気体の加圧時間を０．
５〜５分間としたのは、０．５分未満では気体が目詰ま
り部分に十分に行きわたらず、目詰まり部分の洗浄の効
果が十分ではない、また、５分を超えると洗浄の効果の
向上は少なく、洗浄効率が低下するからである。Gas pressurization time (gas pressurization step)
Is a time during which the gas is substantially pressurized on all the permeating sides of the filtration membrane in the filtration membrane module, and is preferably 0.1 to 5 minutes, but is preferably 0 in consideration of the washing effect and efficiency. 0.5 to 2 minutes. Here, the gas pressurization time is set to 0.
The reason for 5 to 5 minutes is that the gas does not sufficiently reach the clogged portion in less than 0.5 minute, and the cleaning effect of the clogged portion is not sufficient. This is because the improvement is small and the cleaning efficiency is reduced.
【００１５】本発明の濾過膜モジュールの濾過膜は、特
に限定されないが、精密濾過膜、限外濾過膜、ナノ濾過
膜及び逆浸透膜などがある。精密濾過膜では、気体を透
過側から加圧すると、気体が濾過膜を通過してしまう場
合があるため、均一な洗浄が困難となる。また、ナノ濾
過膜や逆浸透膜では、濾過膜の膜孔径が小さすぎて気体
が濾過膜の孔内部に侵入できない場合があり、十分な洗
浄効果が得られなくなる。従って、本発明の濾過膜とし
ては、限外濾過膜が好ましい。ここで限外濾過膜とは、
分画分子量が１０3〜１０6であり、膜孔径が１〜１００
ｎｍの濾過膜をいう。The filtration membrane of the filtration membrane module of the present invention is not particularly limited, but includes a microfiltration membrane, an ultrafiltration membrane, a nanofiltration membrane and a reverse osmosis membrane. In a microfiltration membrane, when gas is pressurized from the permeation side, the gas may pass through the filtration membrane, making uniform cleaning difficult. In the case of a nanofiltration membrane or a reverse osmosis membrane, the membrane pore size of the filtration membrane may be too small to allow gas to enter the pores of the filtration membrane, and a sufficient cleaning effect may not be obtained. Therefore, as the filtration membrane of the present invention, an ultrafiltration membrane is preferable. Here, the ultrafiltration membrane is
The molecular weight cut-off is 10 3 to 10 6 , and the membrane pore size is 1 to 100.
nm refers to a filtration membrane.
【００１６】本発明の濾過膜モジュールの膜材質として
は、ポリエーテルスルホン、ポリアクリロニトリル共重
合体及び酢酸セルロースなどの高分子があるが、酢酸セ
ルロースが特に好ましい。The membrane material of the filtration membrane module of the present invention includes polymers such as polyethersulfone, polyacrylonitrile copolymer and cellulose acetate, and cellulose acetate is particularly preferred.
【００１７】本発明の濾過膜モジュールの膜形態として
は、プレート・アンド・フレーム型、プリーツ型、スパ
イラル型、チューブラー（管状）型及び中空糸型がある
が、中空糸型が好ましい。また、中空糸膜モジュールを
用いる場合には、中空糸膜の内側に原水を流入させる内
圧方式が好ましい。As the membrane form of the filtration membrane module of the present invention, there are a plate and frame type, a pleated type, a spiral type, a tubular (tubular) type and a hollow fiber type, and the hollow fiber type is preferred. When a hollow fiber membrane module is used, an internal pressure system in which raw water flows into the hollow fiber membrane is preferable.
【００１８】本発明において、薬液洗浄を一種もしくは
二種以上の組み合わせて行う例として、クエン酸と界面
活性剤を組み合わせた「組み合わせ薬液」を用いること
を挙げることができる。また１段または多段に組み合わ
せるとは、１段の場合は上記の薬液による洗浄を一度だ
け行うことを意味し、多段の場合は薬液による洗浄を数
回行うことを意味する。クエン酸と界面活性剤を用いて
濾過膜モジュールを多段で洗浄する場合の形態として
は、クエン酸で洗浄し、つぎに界面活性剤で洗浄する
例、両者の組み合わせ薬液で数回洗浄する例、など種
々の組み合わせがある。これらの洗浄の間または前後に
気体加圧工程を適宜入れてもよいのは勿論である。薬液
洗浄時の薬液は、濾過膜の原水側を循環させてもよい
し、原水側から透過側に循環させてもよい。さらに、濾
過膜の透過側から原水側に流すようにしてもよい。In the present invention, as an example of performing the chemical cleaning by one kind or a combination of two or more kinds, use of a “combined chemical” combining citric acid and a surfactant can be mentioned. The combination of one stage or multiple stages means that the cleaning with the above-mentioned chemical solution is performed only once in the case of one stage, and that the cleaning with the chemical solution is performed several times in the case of multiple stages. Examples of the case where the filtration membrane module is washed in multiple stages using citric acid and a surfactant include an example of washing with citric acid and then washing with a surfactant, an example of washing several times with a combined chemical solution of both, There are various combinations. It goes without saying that a gas pressurizing step may be appropriately inserted before or after the washing. The chemical at the time of chemical cleaning may be circulated on the raw water side of the filtration membrane, or may be circulated from the raw water side to the permeation side. Furthermore, you may make it flow from the permeate side of a filtration membrane to the raw water side.
【００１９】[0019]
【実施例】以下、本発明の実施例を図面に基づき説明す
るが、本発明は、以下の実施例に限定されるものではな
い。図１は本発明の濾過膜モジュールの洗浄方法を実施
するための濾過膜モジュール１１Ａ〜Ｅを用いた膜浄化
システムである濾過運転装置１０の概略図であり、流量
計や圧力計などの付属設備は省略している。図１におい
て、１１は濾過膜モジュールであり、５本の組み合わせ
で、それぞれ濾過膜モジュール１１Ａ、１１Ｂ、１１
Ｃ、１１Ｄ、１１Ｅ（代表として１１で示す）とする。
濾過膜モジュール１１は、濾過膜１１Ｒの膜材質が酢酸
セルロースで、中空糸膜からなる中空糸膜モジュールを
表したものであり、各中空糸膜モジュールは内径０．８
ｍｍ、外径１．３ｍｍの中空糸からなり、一つのモジュ
ールの膜面積は０．５ｍ2である。１２はプレフィルタ
ーであり、プレフィルター１２は濾過膜モジュール１１
に供給する水である表流水中の異物を除去する。１３は
透過水タンクであり、透過水タンク１３は濾過膜モジュ
ール１１からの透過水を一時貯蔵する。１４、１５はポ
ンプである。６、７、８は、開閉弁である。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Embodiments of the present invention will be described below with reference to the drawings, but the present invention is not limited to the following embodiments. FIG. 1 is a schematic diagram of a filtration operation device 10 which is a membrane purification system using a filtration membrane module 11A to 11E for carrying out a method for cleaning a filtration membrane module of the present invention. Is omitted. In FIG. 1, reference numeral 11 denotes a filtration membrane module, and a combination of five filtration membrane modules 11A, 11B, 11
C, 11D and 11E (represented by 11).
The filtration membrane module 11 represents a hollow fiber membrane module made of cellulose acetate, wherein the membrane material of the filtration membrane 11R is cellulose acetate, and each hollow fiber membrane module has an inner diameter of 0.8.
mm, a hollow fiber having an outer diameter of 1.3 mm, and the membrane area of one module is 0.5 m 2 . Reference numeral 12 denotes a pre-filter, and the pre-filter 12 is a filtration membrane module 11
Foreign matter in surface water, which is water to be supplied to the water, is removed. Reference numeral 13 denotes a permeate tank, and the permeate tank 13 temporarily stores permeate from the filtration membrane module 11. 14 and 15 are pumps. Reference numerals 6, 7, and 8 are on-off valves.
【００２０】濾過運転時には、開閉弁７は閉じ、開閉弁
６、８は開いている。表流水である河川原水１は、取水
パイプ１６から供給され、プレフィルター１２で異物が
除去され、ポンプ１４で５本の濾過膜モジュール１１Ａ
〜１１Ｅのそれぞれに供給される。濾過膜モジュール１
１では、河川原水は中空糸濾過膜１１Ｒの内側に供給さ
れ、内圧クロスフロー濾過された透過水は開閉弁６を通
って集水され、透過水タンク１３に一時貯蔵され、浄化
水としてパイプ１７から送り出される。濾過されなかっ
た原水は循環パイプ１８を介して開閉弁８を通り、循環
するようになされている。濾過膜モジュール１１の濾過
は、クロスフロー線速０．２ｍ／ｓで、設定濾過流束
１．５ｍ／日の定流量濾過である。また、運転は、４５
分おきに１回の割合で、透過水を濾過膜モジュールの透
過側から１分間流す逆洗工程を設け、水回収率を９０％
とされている。逆洗運転時には、開閉弁７は開き、開閉
弁６、８は閉じ、ポンプ１４は停止している。そして透
過水の一部をポンプ１５を介して通常運転とは逆向きに
濾過膜モジュール１１の透過側に供給する逆洗を定期的
に実施できる様になっている。During the filtration operation, the on-off valve 7 is closed and the on-off valves 6, 8 are open. River raw water 1, which is surface water, is supplied from an intake pipe 16, foreign matter is removed by a pre-filter 12, and five filter membrane modules 11A are supplied by a pump 14.
To 11E. Filtration membrane module 1
In 1, the raw water of the river is supplied to the inside of the hollow fiber filtration membrane 11R, and the permeated water subjected to the internal pressure cross flow filtration is collected through the on-off valve 6, temporarily stored in the permeated water tank 13, and is supplied to the pipe 17 as purified water. Sent out from. The unfiltered raw water is circulated through the on-off valve 8 via the circulation pipe 18. The filtration of the filtration membrane module 11 is a constant flow filtration at a cross flow linear velocity of 0.2 m / s and a set filtration flux of 1.5 m / day. In addition, driving is 45
A backwashing step is performed in which permeated water flows from the permeation side of the filtration membrane module for one minute at a rate of once every minute, and the water recovery rate is 90%.
It has been. During the backwash operation, the on-off valve 7 is open, the on-off valves 6, 8 are closed, and the pump 14 is stopped. Then, backwashing in which a part of the permeated water is supplied to the permeate side of the filtration membrane module 11 through the pump 15 in a direction opposite to the normal operation can be periodically performed.
【００２１】（実施例１）図２は本発明の実施例１を示
す図であり、２０は本発明の濾過膜モジュールの洗浄方
法を実施するための濾過膜モジュールの薬液洗浄装置で
ある。まず、図２に示す薬液洗浄装置２０の構成につき
説明する。２１は濾過膜モジュール、２２は濾過膜モジ
ュールを薬液洗浄するための薬液２２Ａを貯蔵した薬液
槽、２３は純水を貯蔵した純水槽、２４はポンプ、２５
は気体である圧縮空気２５Ａを貯蔵した空気圧ボンベ、
２６は圧力ゲージ、２７は圧力調節弁、２８、２９、３
０、３１、３２、３３、３４、３５、３６、３８、３９
および４０は開閉弁、３７はフィルターである。薬液洗
浄装置２０において、開閉弁３２および３９を閉じた状
態で、空気圧ボンベ２５のバルブを開き、圧力調節弁２
７を調節することにより、空気２５Ａを濾過膜モジュー
ル２１の透過側に所定の圧力で圧入できるようになされ
ている。また、開閉弁２９、３０、３３、３４、３５お
よび４０を開、開閉弁２８、３１、３２、３６、３８お
よび３９を閉として、ポンプ２４を駆動させることによ
り、薬液槽２２内の薬液２２Ａを循環させて、濾過膜モ
ジュール２１を薬液洗浄することが可能である。循環洗
浄後、さらに開閉弁２８を開として、薬液２２Ａを排出
した後、開閉弁３１、２９、３３、３４、３６、３２お
よび４０を開に、開閉弁３０、２８、３５、３８および
３９を閉にしてポンプ２４を稼働させて、回復率を求め
るための純水透過流束を測定できるようになされてい
る。(Embodiment 1) FIG. 2 is a view showing Embodiment 1 of the present invention, and reference numeral 20 is a chemical liquid cleaning apparatus for a filtration membrane module for implementing the method for cleaning a filtration membrane module of the invention. First, the configuration of the chemical cleaning device 20 shown in FIG. 2 will be described. 21 is a filtration membrane module, 22 is a chemical tank storing a chemical 22A for cleaning the filtration membrane module with a chemical, 23 is a pure water tank storing pure water, 24 is a pump, 25
Is a pneumatic cylinder storing compressed air 25A as a gas,
26 is a pressure gauge, 27 is a pressure control valve, 28, 29, 3
0, 31, 32, 33, 34, 35, 36, 38, 39
And 40 are an on-off valve and 37 is a filter. In the chemical cleaning device 20, with the on-off valves 32 and 39 closed, the valve of the pneumatic cylinder 25 is opened, and the pressure control valve 2 is opened.
By adjusting 7, the air 25A can be pressed into the permeate side of the filtration membrane module 21 at a predetermined pressure. In addition, the on-off valves 29, 30, 33, 34, 35, and 40 are opened, and the on-off valves 28, 31, 32, 36, 38, and 39 are closed, and the pump 24 is driven. Can be circulated to wash the filtration membrane module 21 with a chemical solution. After the circulation cleaning, the on-off valve 28 is further opened and the chemical solution 22A is discharged, and then the on-off valves 31, 29, 33, 34, 36, 32 and 40 are opened, and the on-off valves 30, 28, 35, 38 and 39 are opened. When the pump 24 is closed and the pump 24 is operated, the pure water permeation flux for obtaining the recovery rate can be measured.
【００２２】本実施例では、まず、図１における濾過運
転装置１０において、濾過膜モジュール１１に、純水透
過流束が８．４ｍ／日の純水透水能力を有する濾過膜モ
ジュール１１Ａ〜Ｅの５本を取り付けた。そして、河川
下流の河川原水（表流水）１を濾過運転装置の取水パイ
プ１６から取水し、濾過運転を開始した。濾過運転は、
中空糸膜の内側に原水を供給する内圧クロスフロー濾過
（クロスフロー線速０．２ｍ／ｓ）であり、設定濾過流
束１．５ｍ／日の定流量濾過で実施した。また、運転
は、４５分おきに１回、透過水を濾過膜モジュールの透
過側から１分間流す逆洗工程を設け、水回収率を９０％
とした。この定流量濾過運転では、濾過膜が原水中の異
物により汚れ、目詰まりするとともに、濾過圧力が徐々
に増加し、運転開始から約８ヶ月後に５本の濾過膜モジ
ュールがともに濾過圧力が１００ｋＰａに達して運転の
継続が行えなくなった。これらの５本の濾過膜モジュー
ル１１Ａ〜１１Ｅを濾過運転装置１０から取り外し、図
２に示す薬液洗浄装置２０の濾過膜モジュール２１に代
えて順に取り付け、濾過膜モジュール１１に純水を１０
０ｋＰａ加圧で透過し、純水透過流束を測定したとこ
ろ、いずれも１．３〜１．８ｍ／日であり、運転前の純
水透過流束８．４ｍ／日から著しく透水性能が低下し
た。In this embodiment, first, in the filtration operation device 10 shown in FIG. 1, the filtration membrane module 11 is provided with the filtration membrane modules 11A to 11E having a pure water permeation flux of 8.4 m / day. Five were attached. Then, the river raw water (surface water) 1 downstream of the river was taken in from the intake pipe 16 of the filtration operation device, and the filtration operation was started. Filtration operation is
Internal pressure cross flow filtration (cross flow linear velocity 0.2 m / s) for supplying raw water to the inside of the hollow fiber membrane was performed by constant flow filtration at a set filtration flux of 1.5 m / day. In addition, the operation is provided with a backwashing step in which permeated water flows for one minute from the permeation side of the filtration membrane module once every 45 minutes, and the water recovery rate is 90%.
And In this constant flow filtration operation, the filtration membrane is contaminated and clogged by foreign substances in raw water, and the filtration pressure gradually increases. After about eight months from the start of operation, the filtration pressure of all five filtration membrane modules is increased to 100 kPa. It has become impossible to continue driving. These five filtration membrane modules 11A to 11E are detached from the filtration operation device 10 and attached in place of the filtration membrane module 21 of the chemical liquid cleaning device 20 shown in FIG.
When the pure water permeation flux was measured at a pressure of 0 kPa and the pure water permeation flux was 1.3 to 1.8 m / day, the permeation performance was significantly reduced from the pure water permeation flux of 8.4 m / day before operation. did.
【００２３】次いで、上記運転後の濾過膜モジュール１
１の洗浄を行った。先ず、運転後の濾過膜モジュール１
１Ａ（純水透過流束１．５ｍ／日）を、図２に示す薬液
洗浄装置２０の濾過膜モジュール２１の代わりに取り付
け、開閉弁３２および３９を閉の状態で空気圧ボンベ２
５から圧力調節弁２７によって空気圧５０ｋＰａに調節
した空気２５Ａを濾過膜モジュール２１の透過側に１分
間圧入した。すなわち、気体加圧工程を設けた。次い
で、薬液洗浄のため、開閉弁２９、３０、３３、３４、
３５および４０を開、開閉弁２８、３１、３２、３６、
３８および３９を閉として、ポンプ２４を駆動させて、
薬液タンク２４中のクエン酸水溶液（１ｗｔ％）を膜面
での平均線速が０．５ｍ／ｓとなるように３０分間循環
させて、濾過膜モジュールを薬液洗浄した後、開閉弁２
８を開とし、薬液を排出した。その後、前記と同様にし
て、濾過膜モジュール１１Ａの純水透過流束を測定した
ところ、８．３ｍ／日であり、ほぼ運転前の透過流束に
まで回復するという優れた洗浄効果を得ることができ
た。Next, the filtration membrane module 1 after the above operation
1 was performed. First, the filtration membrane module 1 after operation
1A (pure water permeation flux: 1.5 m / day) was installed in place of the filtration membrane module 21 of the chemical liquid cleaning device 20 shown in FIG. 2, and the pneumatic cylinder 2 with the on-off valves 32 and 39 closed.
5, air 25A adjusted to an air pressure of 50 kPa by the pressure adjusting valve 27 was pressed into the permeation side of the filtration membrane module 21 for 1 minute. That is, a gas pressurizing step was provided. Then, for chemical cleaning, the on-off valves 29, 30, 33, 34,
Open 35 and 40, open / close valves 28, 31, 32, 36,
38 and 39 are closed, the pump 24 is driven,
After the citric acid aqueous solution (1 wt%) in the chemical liquid tank 24 is circulated for 30 minutes so that the average linear velocity on the membrane surface becomes 0.5 m / s, and the filtration membrane module is washed with the chemical liquid, the on-off valve 2 is opened.
8 was opened and the drug solution was discharged. Thereafter, the pure water permeation flux of the filtration membrane module 11A was measured in the same manner as described above, and it was 8.3 m / day, and an excellent cleaning effect of recovering to almost the permeation flux before operation was obtained. Was completed.
【００２４】（実施例２）実施例２においては、実施例
１における濾過運転装置１０を用い、定流量濾過運転に
より透水性能が低下した濾過膜モジュール１１Ｂ（純水
透過流束１．８ｍ／日）を、図２に示す薬液洗浄装置２
０の濾過膜モジュール２１の代わりに取り付けた。そし
て濾過膜モジュール１１Ｂの透過側に空気を圧入する前
に、クエン酸水溶液（１ｗｔ％）を１０分間循環させて
洗浄した後、透過側に１００ｋＰａの空気２５Ａを圧入
して、濾過膜モジュール１１Ｂの透過側を１分間空気２
５Ａに接触させる（すなわち、気体加圧工程）と同時に
薬液２２Ａを排出した。そして、再びクエン酸水溶液
（１ｗｔ％）を１０分間循環させて濾過膜モジュール１
１Ｂを洗浄し、再び薬液を排出した。すなわち、一種類
の薬液を気体加圧工程の前後に２段に組み合わせて洗浄
した。その後濾過膜モジュール１１Ｂの純水透過流束を
測定したところ、８．０ｍ／日であり、薬洗時間が約２
０分間と比較的短い時間で運転前の透過流束の９５％ま
で回復するという優れた洗浄効果を得ることができた。(Embodiment 2) In Embodiment 2, using the filtration operation device 10 of Embodiment 1, a filtration membrane module 11B (pure water permeation flux of 1.8 m / day) having reduced water permeability due to constant flow filtration operation. ) To the chemical cleaning device 2 shown in FIG.
0 instead of the filtration membrane module 21. Then, before injecting air into the permeation side of the filtration membrane module 11B, the citric acid aqueous solution (1 wt%) is circulated for 10 minutes and washed, and then 100 kPa of air 25A is press-injected into the permeation side, and the filtration membrane module 11B Air 2 per minute on permeate side
The chemical solution 22A was discharged at the same time as the contact with the 5A (that is, the gas pressurizing step). Then, the aqueous citric acid solution (1 wt%) is circulated again for 10 minutes, and the filtration membrane module 1 is circulated.
1B was washed and the chemical solution was discharged again. That is, one type of chemical solution was combined and washed in two stages before and after the gas pressurizing step. After that, when the pure water permeation flux of the filtration membrane module 11B was measured, it was 8.0 m / day, and the chemical washing time was about 2 hours.
An excellent cleaning effect of recovering to 95% of the permeation flux before operation was obtained in a relatively short time of 0 minute.
【００２５】（実施例３）実施例３においては、実施例
１における濾過運転装置１０を用い、定流量濾過運転に
より透水性能が低下した濾過膜モジュール１１Ｃ（純水
透過流束１．６ｍ／日）を、図２に示す薬液洗浄装置２
０の濾過膜モジュール２１の代わりに取り付けた。そし
て開閉弁３２および３９を閉の状態で濾過膜モジュール
１１Ｃの透過側から空気圧５０ｋＰａの空気２５Ａを圧
入して濾過膜１１Ｒの透過側に１分間空気で接触させた
（すなわち、気体加圧工程）後、開閉弁２８、２９、３
０、３３、３４、３８および３９を開、開閉弁２７、３
１、３２、３５、３６および４０を閉として、ポンプ２
４を駆動させ、薬液槽２２中の界面活性剤（ウルトラジ
ル＃５３、ヘンケル白水社製）の１ｗｔ％水溶液を濾過
膜モジュール１１Ｃの透過側から圧力１００ｋＰａで１
分間圧入透過した。そして、薬液を排出した。その後、
濾過膜モジュール１１Ｃの純水透過流束を測定したとこ
ろ、７．６ｍ／日であり、運転前の透過流束の約９０％
まで回復するという優れた洗浄効果を得ることができ
た。(Embodiment 3) In Embodiment 3, a filtration membrane module 11C (pure water permeation flux of 1.6 m / day) having a reduced water permeability due to a constant flow filtration operation was performed using the filtration operation device 10 of Embodiment 1. ) To the chemical cleaning device 2 shown in FIG.
0 instead of the filtration membrane module 21. Then, with the on-off valves 32 and 39 closed, air 25A having an air pressure of 50 kPa was injected from the permeation side of the filtration membrane module 11C and brought into contact with the permeation side of the filtration membrane 11R with air for one minute (ie, a gas pressurization step). Later, on-off valves 28, 29, 3
0, 33, 34, 38 and 39 are opened, and the on-off valves 27 and 3
1, 32, 35, 36 and 40 are closed and pump 2
4 is driven, and a 1 wt% aqueous solution of a surfactant (Ultrasil # 53, manufactured by Henkel Hakusui Co., Ltd.) in the chemical solution tank 22 is supplied from the permeation side of the filtration membrane module 11C at a pressure of 100 kPa to 1
Pressed through for minutes. Then, the chemical solution was discharged. afterwards,
The pure water permeation flux of the filtration membrane module 11C was measured to be 7.6 m / day, which was about 90% of the permeation flux before operation.
An excellent cleaning effect of recovering up to a maximum was obtained.
【００２６】（比較例１）比較例１においては、実施例
１における濾過運転装置１０を用い、定流量濾過運転に
より透水性能が低下した濾過膜モジュール１１Ｄ（純水
透過流束１．３ｍ／日）を、図２に示す薬液洗浄装置２
０の濾過膜モジュール２１の代わりに取り付けた。そし
て濾過膜モジュール１１Ｄの透過側に空気を圧入せず
に、薬液としてクエン酸水溶液（１ｗｔ％）を実施例１
と同様に３０分間循環させて濾過膜モジュール１１Ｄの
洗浄を行った後、薬液を排出した。その後、濾過膜モジ
ュール１１Ｄの純水透過流束を測定したところ、５．６
ｍ／日であり、薬洗時間を約３０分間要したが、運転前
の透過流束の６５％と洗浄回復性は著しく低かった。(Comparative Example 1) In Comparative Example 1, using the filtration operation device 10 of Example 1, a filtration membrane module 11D (pure water permeation flux of 1.3 m / day) having reduced water permeability due to constant flow filtration operation was used. ) To the chemical cleaning device 2 shown in FIG.
0 instead of the filtration membrane module 21. Example 1 A citric acid aqueous solution (1 wt%) was used as a chemical solution without injecting air into the permeate side of the filtration membrane module 11D.
After circulating for 30 minutes in the same manner as described above to wash the filtration membrane module 11D, the chemical solution was discharged. Then, when the pure water permeation flux of the filtration membrane module 11D was measured, it was 5.6.
m / day, and took about 30 minutes for washing, but the permeation flux before the operation was 65%, and the washing recovery was extremely low.
【００２７】（比較例２）運転により透水性能が低下し
た濾過膜モジュール１１Ｅ（純水透過流束１．６ｍ／
日）を、図２に示す薬液洗浄装置２０の濾過膜モジュー
ル２１の代わりに取り付けた。そして、濾過膜モジュー
ル１１Ｅの透過側に空気を圧入せずに、実施例３と同様
に、薬液槽２２中の界面活性剤（ウルトラジル＃５３、
ヘンケル白水社製）の１ｗｔ％水溶液を濾過膜モジュー
ル１１Ｅの透過側から圧力１００ｋＰａで１分間圧入透
過して洗浄を行った。そして薬液を排出した。その後、
純水透過流束を測定したところ、４．３ｍ／日であり、
運転前の透過流束の５１％と洗浄回復性は著しく低かっ
た。(Comparative Example 2) A filtration membrane module 11E (permeate flux 1.6 m / p.
2) was attached in place of the filtration membrane module 21 of the chemical solution cleaning device 20 shown in FIG. Then, as in the third embodiment, the surfactant (Ultrasil # 53,
A 1 wt% aqueous solution of Henkel Hakusui Co., Ltd.) was injected through the permeation side of the filtration membrane module 11E at a pressure of 100 kPa for 1 minute to perform cleaning. Then, the drug solution was discharged. afterwards,
When the pure water flux was measured, it was 4.3 m / day,
The permeation flux before the operation was 51%, and the washing recovery was extremely low.
【００２８】[0028]
【発明の効果】以上、説明したように、本発明によれ
ば、濾過膜モジュールの薬液洗浄工程に気体加圧工程を
適宜に設けることにより、濾過膜モジュールの洗浄効果
を著しく向上することができ、薬液の使用量を減らせる
とともに、短時間で薬液洗浄が行えることによって、洗
浄コストを大幅に下げることができる。As described above, according to the present invention, the cleaning effect of the filtration membrane module can be remarkably improved by appropriately providing the gas pressurizing step in the chemical solution cleaning step of the filtration membrane module. In addition, the use amount of the chemical solution can be reduced, and the chemical solution can be cleaned in a short time, so that the cleaning cost can be significantly reduced.
【図１】本発明の濾過膜モジュールの洗浄方法を実施す
るための濾過膜モジュールを用いた濾過運転装置の概略
図FIG. 1 is a schematic diagram of a filtration operation device using a filtration membrane module for performing a filtration membrane module cleaning method of the present invention.
【図２】本発明の濾過膜モジュールの洗浄方法を実施す
るための濾過膜モジュールの薬液洗浄装置の概略図FIG. 2 is a schematic diagram of a chemical liquid cleaning apparatus for a filtration membrane module for performing the filtration membrane module cleaning method of the present invention.
１ 河川原水、表流水（水） １０ 濾過運転装置（膜浄化システム） １１ 濾過膜モジュール（中空糸膜モジュール） １１Ｒ 濾過膜（中空糸膜） ２２Ａ 薬液 ２５Ａ 空気（気体） Reference Signs List 1 River raw water, surface water (water) 10 Filtration operation device (membrane purification system) 11 Filtration membrane module (hollow fiber membrane module) 11R Filtration membrane (hollow fiber membrane) 22A Chemical solution 25A Air (gas)
フロントページの続き (51)Int.Cl.6 識別記号 ＦＩ Ｂ０１Ｄ 71/16 Ｂ０１Ｄ 71/16 Ｃ０２Ｆ 1/44 Ｃ０２Ｆ 1/44 Ｈ Continued on the front page (51) Int.Cl. 6 Identification code FI B01D 71/16 B01D 71/16 C02F 1/44 C02F 1/44 H
Claims (6)
濾過膜モジュールを薬液によって洗浄して透水性能を回
復させる濾過膜モジュールの洗浄方法において、 薬液
を濾過膜モジュールに供給する前あるいは後のいずれか
一方またはその両方の時点で、気体を濾過膜モジュール
の濾過膜の透過側から圧力２０ｋＰａ以上バブルポイン
ト未満で加圧する気体加圧工程を０．１〜５分間設ける
ことを特徴とする濾過膜モジュールの洗浄方法。1. A method for cleaning a filtration membrane module in which a filtration performance of a filtration membrane module with reduced water permeability of a water membrane purification system is restored by a chemical solution to recover the permeability performance, before or after supplying the chemical solution to the filtration membrane module. A filter pressurizing step for pressurizing the gas at a pressure of 20 kPa or more and less than a bubble point from the permeation side of the filtration membrane of the filtration membrane module at one or both of the times, for 0.1 to 5 minutes; How to clean the module.
項１に記載の濾過膜モジュールの洗浄方法。2. The method for cleaning a filtration membrane module according to claim 1, wherein the water is surface water.
する請求項１または２に記載の濾過膜モジュールの洗浄
方法。3. The method for cleaning a filtration membrane module according to claim 1, wherein the filtration membrane is an ultrafiltration membrane.
空糸膜モジュールであることを特徴とする請求項１〜３
のいずれか１項に記載の濾過膜モジュールの洗浄方法。4. The filter module according to claim 1, wherein the filtration membrane module is a hollow fiber membrane module comprising a hollow fiber membrane.
The method for cleaning a filtration membrane module according to any one of the above.
ことを特徴とする請求項１〜４のいずれか１項に記載の
濾過膜モジュールの洗浄方法。5. The method for cleaning a filtration membrane module according to claim 1, wherein the membrane material of the filtration membrane is cellulose acetate.
及び次亜塩素酸ナトリウムのうちから選択される一種も
しくは二種以上の組み合わせまたは１段もしくは多段に
組み合わて行うことを特徴とする請求項１〜５のいずれ
か１項に記載の濾過膜モジュールの洗浄方法。6. The method according to claim 1, wherein the washing with the chemical solution is carried out by one or a combination of two or more selected from citric acid, a surfactant and sodium hypochlorite. Item 6. The method for cleaning a filtration membrane module according to any one of Items 1 to 5.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP25129097A JPH1176769A (en) | 1997-09-01 | 1997-09-01 | Cleaning method of filter membrane module |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP25129097A JPH1176769A (en) | 1997-09-01 | 1997-09-01 | Cleaning method of filter membrane module |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH1176769A true JPH1176769A (en) | 1999-03-23 |
Family
ID=17220614
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP25129097A Withdrawn JPH1176769A (en) | 1997-09-01 | 1997-09-01 | Cleaning method of filter membrane module |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH1176769A (en) |
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1997
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