JP2794304B2 - Cleaning method for hollow fiber membrane module - Google Patents
Cleaning method for hollow fiber membrane moduleInfo
- Publication number
- JP2794304B2 JP2794304B2 JP1132330A JP13233089A JP2794304B2 JP 2794304 B2 JP2794304 B2 JP 2794304B2 JP 1132330 A JP1132330 A JP 1132330A JP 13233089 A JP13233089 A JP 13233089A JP 2794304 B2 JP2794304 B2 JP 2794304B2
- Authority
- JP
- Japan
- Prior art keywords
- hollow fiber
- fiber membrane
- stock solution
- module
- chamber
- 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.)
- Expired - Fee Related
Links
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Description
【発明の詳細な説明】 ＜産業上の利用分野＞ 本発明は、運転中の中空糸膜モジュールを所定期間ご
とに洗浄する場合に使用する洗浄方法の改良に関するも
のである。DETAILED DESCRIPTION OF THE INVENTION <Industrial Application Field> The present invention relates to an improvement in a cleaning method used for cleaning an operating hollow fiber membrane module at predetermined intervals.
＜従来の技術＞ 原液を透過膜によって濾過処理する場合、経時的に原
液中の懸濁物が膜面に付着していき、透過流束の低下が
避け得ないので、所定期間ごとに付着物を除去して膜の
透過性能を回復させることが必要である。而して、従来
から、膜モジュールの濾過運転中に定期的にモジュール
の膜洗浄を行っている。この洗浄方法には種々のものが
知られているが、膜モジュールの連続運転をほとんど阻
害することなく短期間で行い得る方法の一つとして逆洗
方法が知られている。<Prior art> When a stock solution is filtered through a permeable membrane, the suspended matter in the stock solution adheres to the membrane surface over time, and a decrease in the permeation flux cannot be avoided. It is necessary to restore the permeation performance of the membrane by removing the water. Conventionally, the membrane of the module is periodically cleaned during the filtration operation of the module. Various cleaning methods are known, and a backwash method is known as one of the methods that can be performed in a short period of time without substantially hindering the continuous operation of the membrane module.
第５図は中空糸膜束を用いたモジュールの一例を示
し、中空糸膜束12′（中空糸膜の上端は開口し、下端は
閉塞してある）をケース11′内に収納し、ケース内を仕
切板13′によって原液室Ａ′と透過液室Ｂ′とに分け、
原液を原液供給管15′によって原液室Ａ′内に圧入し、
この原液を中空糸膜で濾過し、透過液を中空糸膜内並び
に透過液室Ｂ′を経て透過液取出管９′より取出すもの
である。このモジュールを逆洗する場合は、バルブv1を
閉としたうえで、まず、バルブv2を開にして溢流液出口
ライン18′にまでケース11′内の原液レベルを下げ、原
液室上部に空間を形成し、次いで、バルブv3を閉にした
うえで、バルブv5並びにv6を開にして逆洗気体供給管
８′から中空糸膜内に気体を圧入し、中空糸膜表面から
気体を逸出させて膜表面の付着物を剥離し、膜からの逸
出気体を原液室の上部空間に集めたうえで、排気管19′
から排気している。FIG. 5 shows an example of a module using a hollow fiber membrane bundle, in which a hollow fiber membrane bundle 12 '(the upper end of the hollow fiber membrane is open and the lower end is closed) is housed in a case 11'. The inside is divided into a stock solution chamber A 'and a permeate chamber B' by a partition plate 13 ',
The undiluted solution is pressed into the undiluted solution chamber A 'by the undiluted solution supply pipe 15',
This undiluted solution is filtered through a hollow fiber membrane, and the permeate is taken out from the permeate outlet pipe 9 'through the hollow fiber membrane and the permeate chamber B'. When backwashing the module, a valve v 1 upon which is closed, first, the valve v 2 in the open lower the stock level in the 'case 11 to the' overflow liquid outlet line 18, the stock solution chamber upper a space is formed, then, the valve v 3 in terms of the closed, valve v 5 and v the gas is pressed into the hollow fiber membrane from the backwashing gas supply pipe 8 'and 6 to open, the hollow fiber membrane surface The gas escapes from the membrane to separate the deposits on the membrane surface, and the escaped gas from the membrane is collected in the upper space of the stock solution chamber, and then exhaust pipe 19 '
From the exhaust.
＜解決しようとする課題＞ ところで、中空糸膜モジュールとして、筒状ケース内
に中空糸膜束を60〜90％もの高占有率で収納したものが
公知である。しかし、本発明者等の実験によれば、中空
糸膜をかかる高占有率で用いた中空糸膜モジュールを、
従来の逆洗方法によって洗浄しても、透過性能のほぼ完
全な回復は困難である。<Problem to be Solved> By the way, a hollow fiber membrane module in which a hollow fiber membrane bundle is housed in a cylindrical case with a high occupancy of 60 to 90% is known. However, according to experiments by the present inventors, a hollow fiber membrane module using a hollow fiber membrane at such a high occupancy rate is
Even if it is washed by a conventional backwashing method, it is difficult to almost completely recover the permeation performance.
従来の逆洗方法において、膜を原液中に存在させた状
態で逆洗することを要件としている理由の一つは、中空
糸膜の内部から外部に逸出した気体を原液中に気泡の形
態で上昇させていき、この上昇気泡の上記付着物への接
触または、上昇気泡によって惹起される原液の回流によ
っても、上記付着物の剥離を促進することにある。しか
しながら、上記中空糸膜を60〜90％といった高占有率で
用いた中空糸膜モジュールにおいては、膜を原液中に存
在させた状態で逆洗しても余り効果がなく、その理由
は、上昇気泡による原液の回流が殆ど期待できないため
であると考えられる。One of the reasons that the conventional backwashing method requires backwashing while the membrane is present in the stock solution is one of the reasons that gas escaping from the inside of the hollow fiber membrane to the outside is in the form of bubbles in the stock solution. The purpose of the present invention is to promote the separation of the deposits by contact of the rising bubbles with the deposits or circulation of the stock solution caused by the rising bubbles. However, in a hollow fiber membrane module using the above hollow fiber membrane at a high occupancy rate of 60 to 90%, backwashing in a state where the membrane is present in the stock solution has no significant effect. It is considered that the circulation of the stock solution due to the bubbles can hardly be expected.
本発明の目的は、上記中空糸膜を高占有率で用いた中
空糸膜モジュールを有効に洗浄できる逆洗方法を開発
し、その洗浄時間の短縮化を可能にし、同上モジュール
の運転中に、その運転継続性を実質的に阻害することな
く、所定期間ごとに洗浄するのを可能にすることにあ
る。An object of the present invention is to develop a backwashing method capable of effectively washing a hollow fiber membrane module using the above hollow fiber membrane at a high occupancy rate, enabling a reduction in the washing time, and during operation of the module, It is an object of the present invention to enable cleaning at predetermined intervals without substantially impairing the continuity of operation.
＜課題を解決するための手段＞ 本発明に係る中空糸膜モジュールの洗浄方法は、中空
糸膜束を筒状ケース内に収容し、ケース内を原液室と
し、中空糸膜内を透過側とする中空糸膜モジュールの濾
過運転中にそのモジュールを洗浄する方法において、未
洗浄膜に接している原液室内の被処理液を排出して該室
内を空状態にし、かかる状態のもとで、透過側より逆圧
を加えて洗浄を行うことを特徴とする方法である。<Means for Solving the Problems> In the method for cleaning a hollow fiber membrane module according to the present invention, a hollow fiber membrane bundle is housed in a cylindrical case, the case is used as a stock solution chamber, and the hollow fiber membrane is used as a permeate side. In a method of cleaning a hollow fiber membrane module during a filtration operation of the module, a liquid to be treated in a raw solution chamber in contact with an uncleaned membrane is discharged to empty the chamber, and permeation is performed under such a state. This is a method characterized in that washing is performed by applying a reverse pressure from the side.
＜実施例の説明＞ 以下、図面により本発明の実施例について説明する。<Description of Example> Hereinafter, an example of the present invention will be described with reference to the drawings.
第１図は本発明において使用する液体濾過システムを
示している。第１図において、１は中空糸膜モジュール
であり、原液室内における中空糸膜の占有率が75〜90％
もの高占有率のものを使用している。この中空糸膜に
は、例えば、第２図に示すように、筒状ケース11内に中
空糸膜束12を収容し、ケース両端に樹脂隔壁13・14を設
け、ケースの一端部に原液入口15を、ケースの他端部に
濃縮原液出口16をそれぞれ設け、ケースの両端に透過水
室17・17をそれぞれ設け、筒状ケース内を原液室とし、
中空糸膜内を透過側としたものを使用できる。第１図に
おいて、２は原液室に連通した加圧気体導入管である。
３は原液タンク、４はポンプである。５は原液戻し管で
ある。６は濃縮原液戻し管である。７は逆洗タンクであ
り、モジュールの透過液室17に連通している。８は逆洗
用加圧気体導入管である。９は透過液取出管である。FIG. 1 shows a liquid filtration system used in the present invention. In FIG. 1, reference numeral 1 denotes a hollow fiber membrane module, which occupies 75 to 90% of the hollow fiber membrane in the stock solution chamber.
The one with a high occupancy rate is used. In this hollow fiber membrane, for example, as shown in FIG. 2, a hollow fiber membrane bundle 12 is accommodated in a cylindrical case 11, resin partition walls 13 and 14 are provided at both ends of the case, and an undiluted liquid inlet is provided at one end of the case. 15, the concentrated stock solution outlet 16 is provided at the other end of the case, the permeated water chambers 17 and 17 are provided at both ends of the case, and the inside of the cylindrical case is used as the stock solution chamber,
A hollow fiber membrane having a permeate side can be used. In FIG. 1, reference numeral 2 denotes a pressurized gas introduction pipe communicating with a stock solution chamber.
3 is a stock solution tank and 4 is a pump. 5 is a stock solution return pipe. 6 is a concentrated stock solution return pipe. Reference numeral 7 denotes a backwash tank, which communicates with the permeate chamber 17 of the module. Reference numeral 8 denotes a pressurized gas introduction pipe for backwashing. 9 is a permeate extraction pipe.
原液を濾過処理するには、バルブV1、V2、V5、並びに
v7を開にし、バルブV3、V6並びにV8を閉にし、ポンプ４
を駆動して、原液タンク３中の原液をモジュール１の原
液室に圧入すればよく、この場合、操作圧力は調圧弁V4
の開閉度を調節することによって設定する。而して、原
液が原液室内において中空糸膜により濾過され、中空糸
膜内の透過水が逆洗タンク７を経て透過液取出管９によ
って取出される。従って、逆洗タンク７内には取出管９
のレベルにまで透過水が貯えられる。上記濾過によって
濃縮された原液は、濃縮液戻り管６を経て原液タンクに
回収される。To filter the stock solution, valves V 1 , V 2 , V 5 , and
The v 7 is opened, the valve V 3, V 6 and V 8 closed, the pump 4
By driving the well be pressed into stock in the stock solution tank 3 for mass chamber of the module 1, In this case, the operation pressure regulating valve V 4
It is set by adjusting the degree of opening and closing. Thus, the undiluted solution is filtered by the hollow fiber membrane in the undiluted liquid chamber, and the permeated water in the hollow fiber membrane is taken out through the backwash tank 7 by the permeated liquid take-out pipe 9. Therefore, in the backwash tank 7, the discharge pipe 9
Permeated water is stored up to the level. The undiluted solution concentrated by the filtration is collected in the undiluted solution tank via the concentrated solution return pipe 6.
上記の濾過運転中、所定期間ごとに逆洗によって膜を
洗浄する。この逆洗にあたっては、まず、バルブV3を開
にし、原液タンク３からの原液の一部を原液戻し管５を
経て原液タンク３に戻して原液供給流量を低下させる。
ポンプ４は駆動したままとしておく。この状態でバルブ
V8を開にして、モジュールの原液室に加圧気体を注入
し、原液室の原液を濃縮液戻し管６を経て原液タンク３
に戻し、原液室を空の状態にし（空の状態になれば、バ
ルブ８を閉にする）、而るのち、バルブV7を閉にし、バ
ルブV6を開にして、逆洗タンク７内に加圧気体を導入
し、逆洗タンク７内の透過液を中空糸膜内に圧入して、
逆洗を行う。所定時間逆洗を行えば、バルブV7を開に
し、バルブV3、バルブV6を閉にして、濾過処理を再開す
る。During the above-mentioned filtration operation, the membrane is washed by back washing every predetermined period. The In is backwashed, firstly, the valve V 3 is opened, to lower the starting solution feed rate back to the stock tank 3 through the stock return pipe 5 a portion of the stock solution from the stock solution tank 3.
The pump 4 is kept running. In this state the valve
And the V 8 is opened, the pressurized gas is injected into the stock solution chamber of the module, the stock solution tank 3 a stock solution of the stock solution chamber through the concentrate return pipe 6
The back, the stock solution chamber empty (if the empty, the valve 8 to close), then而Ru, the valve V 7 closed, and the valve V 6 is opened, the backwash tank 7 And pressurized gas in the backwash tank 7 is injected into the hollow fiber membrane,
Perform backwash. By performing a predetermined time backwash, the valve V 7 is opened, valve V 3, and the valve V 6 to the closed, resume filtration.
上記において、加圧気体を中空糸膜内に直接導入する
こともできる。また、バルブV2を閉にし、バルブV3を開
にして、ポンプ４の駆動下、原液戻し管５を含むループ
回路に原液を循環させて、モジュール原液室での原液流
量を零にし、かかる状態で原液室内の原液を自然に流下
させて、原液室を空にすることもできる。In the above, the pressurized gas can be directly introduced into the hollow fiber membrane. Further, the valve V 2 in the closed, and the valve V 3 is opened, under the drive of the pump 4, by circulating stock solution loop circuit including the stock solution return pipe 5, and the stock solution flow rate in the module stock chamber to zero, such In this state, the undiluted solution in the undiluted solution chamber can be allowed to flow naturally to empty the undiluted solution chamber.
本発明においては、中空糸膜の占有率の高い中空糸膜
モジュールを対象とし、原液室を空にした状態で逆洗を
行っており、原液室を原液で満たしたままで逆洗を行う
場合に較べて、洗浄効率が高く、膜の透過性能を初期性
能に容易に保持できる。この効果を具体的な実施例によ
り比較例との対比のもとで説明する。In the present invention, the hollow fiber membrane module having a high occupancy rate of the hollow fiber membrane is targeted, and the backwash is performed with the stock solution chamber empty, and the backwash is performed while the stock solution chamber is filled with the stock solution. In comparison, the cleaning efficiency is high, and the permeability of the membrane can be easily maintained at the initial performance. This effect will be described with reference to specific examples in comparison with a comparative example.
実施例 中空糸膜モジュールには、内径100mm、長さ1000mmの
筒状ケース内に、外径0.4mmの中空糸膜を50000本収納し
たものを使用し、その中空糸膜の占有率は約80％であ
る。このモジュールによって、懸濁物濃度2000mg/の
発酵液を、運転圧力1kg/cm2、膜面流速0.7m/秒、温度35
℃の条件で処理した。初期純水透過水量は圧力1kg/m2、
温度25℃のもとで、96m3/日であった。24時間乃至40時
間毎に、膜面流速を0.2〜0.3m/秒に低下させ、原液室内
に加圧気体を注入して原液室内の抜き出し、而るのち
に、圧力3kg/m2の加圧気体で、１分間、逆洗タンク内を
加圧して逆洗を行った。Example The hollow fiber membrane module used was one in which 50,000 hollow fiber membranes having an outer diameter of 0.4 mm were housed in a cylindrical case having an inner diameter of 100 mm and a length of 1000 mm, and the occupancy of the hollow fiber membrane was about 80%. %. This module, the suspension concentration 2000 mg / fermentations, operating pressure 1 kg / cm 2, the film surface velocity 0.7 m / s, temperature 35
It processed at the conditions of ° C. Initial pure water permeation amount of water pressure 1 kg / m 2,
At a temperature of 25 ° C., it was 96 m 3 / day. Every 24 hours to 40 hours, to reduce the membrane surface flow rate 0.2 to 0.3 m / sec, extracted stock solution chamber by injecting pressurized gas into the stock solution chamber, after而Ru, pressurization of the pressure 3 kg / m 2 The inside of the backwash tank was pressurized with gas for 1 minute to perform backwash.
比較例 実施例と同一のモジュールを使用し、同一の原液を同
一の条件で処理し、24時間ごとに原液室に原液を満たし
たままで、逆洗タンクを圧力3kg/m2の加圧気体で１分間
加圧して、逆洗を行った。Using the same modules and Comparative Example Example was treated the same stock solution under the same conditions, while satisfying the stock to stock chamber every 24 hours, a backwash tank pressurized gas pressure 3 kg / m 2 Backwashing was performed by pressing for 1 minute.
＜発明の効果＞ 実施例の透過水量は第３図に示す通りであり、400時
間経過後においても、逆洗によって透過性能を初期値に
回復でき、長期にあたって安定な透過性能を確保でき
る。これに対し、比較例の透過水量は第４図に示す通り
であり、実施例よりも洗浄回数を全体として多くしてい
るにもかかわらず、透過性能が次第に低下しており、約
400時間経過後では、初期値の1/2にしか回復できていな
い。<Effect of the Invention> The amount of permeated water in the example is as shown in FIG. 3, and even after 400 hours, the permeation performance can be restored to the initial value by backwashing, and a stable permeation performance can be secured over a long period of time. On the other hand, the amount of permeated water in the comparative example is as shown in FIG. 4, and the permeation performance is gradually lowered despite the fact that the number of washings is increased as a whole as compared with the example.
After 400 hours, it has only recovered to half of the initial value.
上述した通り、本発明に係る中空糸膜モジュールの洗
浄方法によれば、中空糸膜の占有率が高い中空糸膜モジ
ュールを効率よく洗浄でき、モジュールの運転中、１〜
２日間に約１分間洗浄する程度でもモジュールの透過性
能を初期性能に回復でき、中空糸膜モジュールの透過性
能の長期安定性をよく保証できる。As described above, according to the method for cleaning a hollow fiber membrane module according to the present invention, a hollow fiber membrane module having a high occupancy rate of a hollow fiber membrane can be efficiently cleaned, and 1 to 1 during operation of the module.
The permeation performance of the module can be restored to the initial performance even by washing for about one minute every two days, and the long-term stability of the permeation performance of the hollow fiber membrane module can be well guaranteed.
第１図は本発明において使用する液体処理システムを示
す説明図、第２図は本発明において用いる中空糸膜モジ
ュールの一例を示す説明図、第３図は本発明の方法によ
る透過水量特性を示す図表、第４図は従来方法による透
過水量特性を示す図表、第５図は従来の逆洗方法を示す
説明図である。 １……中空糸膜モジュール、２……気体導入管、 ８……逆洗用加圧気体導入管。FIG. 1 is an explanatory diagram showing a liquid treatment system used in the present invention, FIG. 2 is an explanatory diagram showing an example of a hollow fiber membrane module used in the present invention, and FIG. 3 shows a permeated water amount characteristic by the method of the present invention. FIG. 4 is a chart showing a permeated water amount characteristic by the conventional method, and FIG. 5 is an explanatory view showing the conventional backwashing method. 1 ... hollow fiber membrane module, 2 ... gas introduction tube, 8 ... pressurized gas introduction tube for backwashing.
フロントページの続き (72)発明者 池端 永 大阪府茨木市下穂積１丁目１番２号 日 東電工株式会社内 (72)発明者 大谷 肇 大阪府茨木市下穂積１丁目１番２号 日 東電工株式会社内 (56)参考文献 特開 平２−17924（ＪＰ，Ａ) 特開 昭58−183906（ＪＰ，Ａ) 特開 昭63−252507（ＪＰ，Ａ) (58)調査した分野(Int.Cl.6，ＤＢ名) B01D 65/02 B01D 63/02Continued on the front page (72) Inventor Eiji Ikehata 1-2-1, Shimozumi, Ibaraki-shi, Osaka Nitto Denko Corporation (72) Inventor Hajime Hajime 1-2-1, Shimohozumi, Ibaraki-shi, Osaka Nitto (56) References JP-A-2-17924 (JP, A) JP-A-58-183906 (JP, A) JP-A-63-252507 (JP, A) (58) Fields investigated (Int .Cl. 6 , DB name) B01D 65/02 B01D 63/02
Claims (1)
ス内を原液室とし、中空糸膜内を透過側とする中空糸膜
モジュールの濾過運転中にそのモジュールを洗浄する方
法において、未洗浄膜に接している原液室内の被処理液
を排出して該室内を空状態にし、かかる状態のもとで、
透過液側から中空糸膜内を加圧して逆洗を行うことを特
徴とする中空糸膜モジュールの洗浄方法。A method for washing a hollow fiber membrane bundle during a filtration operation of a hollow fiber membrane module in which a hollow fiber membrane bundle is housed in a cylindrical case, the case is used as a stock solution chamber, and the hollow fiber membrane is used as a permeate side. Discharging the liquid to be treated in the undiluted solution chamber in contact with the uncleaned film to empty the chamber, and under such a state,
A method for cleaning a hollow fiber membrane module, wherein backwashing is performed by pressurizing the inside of the hollow fiber membrane from the permeate side.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1132330A JP2794304B2 (en) | 1989-05-24 | 1989-05-24 | Cleaning method for hollow fiber membrane module |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1132330A JP2794304B2 (en) | 1989-05-24 | 1989-05-24 | Cleaning method for hollow fiber membrane module |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH03114A JPH03114A (en) | 1991-01-07 |
| JP2794304B2 true JP2794304B2 (en) | 1998-09-03 |
Family
ID=15078802
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1132330A Expired - Fee Related JP2794304B2 (en) | 1989-05-24 | 1989-05-24 | Cleaning method for hollow fiber membrane module |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2794304B2 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5968551A (en) | 1991-12-24 | 1999-10-19 | Purdue Pharma L.P. | Orally administrable opioid formulations having extended duration of effect |
| JP2500181B2 (en) * | 1992-09-11 | 1996-05-29 | 日本碍子株式会社 | Backwashing method for ceramic membrane |
| US7087173B2 (en) | 1995-08-11 | 2006-08-08 | Zenon Environmental Inc. | Inverted cavity aerator for membrane module |
| DE69627397T2 (en) | 1995-08-11 | 2003-12-04 | Zenon Environmental Inc., Oakville | System for permeate removal from a liquid substrate with several components |
| DE69924642T2 (en) | 1998-11-23 | 2006-02-09 | Zenon Environmental Inc., Oakville | WATER FILTRATION BY UNDERWATER MEMBRANES |
| JP5453711B2 (en) * | 2006-03-29 | 2014-03-26 | 東レ株式会社 | Cleaning method for external pressure hollow fiber membrane module |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0624612B2 (en) * | 1987-04-10 | 1994-04-06 | オルガノ株式会社 | Filtration method using hollow fiber membrane |
-
1989
- 1989-05-24 JP JP1132330A patent/JP2794304B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH03114A (en) | 1991-01-07 |
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| LAPS | Cancellation because of no payment of annual fees |