JP2852958B2 - Operating method of membrane module - Google Patents
Operating method of membrane moduleInfo
- Publication number
- JP2852958B2 JP2852958B2 JP11562390A JP11562390A JP2852958B2 JP 2852958 B2 JP2852958 B2 JP 2852958B2 JP 11562390 A JP11562390 A JP 11562390A JP 11562390 A JP11562390 A JP 11562390A JP 2852958 B2 JP2852958 B2 JP 2852958B2
- Authority
- JP
- Japan
- Prior art keywords
- stock solution
- membrane module
- membrane
- tube
- pipe
- 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〕 本発明は並列配設の膜モジュールの運転方法に関する
ものである。Description: TECHNICAL FIELD The present invention relates to a method for operating membrane modules arranged in parallel.
近来、各種の工業分野において、液体からの固形分の
分離、特定液体の分離等に膜モジュールを用いることが
多い。特に、大規模設備の場合複数台の膜モジュールを
配設し、原液供給管の近端側より原液を送り各膜モジュ
ールで原液を処理し、膜による溶媒の透過で濃縮された
原液を濃縮原液流出用幹管で還流し、透過液を外部に取
出すことがある。2. Description of the Related Art Recently, in various industrial fields, a membrane module is often used for separation of a solid content from a liquid, separation of a specific liquid, and the like. In particular, in the case of large-scale equipment, multiple membrane modules are installed, the stock solution is sent from the near end of the stock solution supply pipe, the stock solution is processed in each membrane module, and the stock solution concentrated by permeation of the solvent through the membrane is concentrated stock solution. Reflux may occur in the effluent main pipe, and the permeate may be taken out.
しかしながら、本発明者の経験によれば上記並列膜モ
ジュールを長期間運転すると遠端側の膜モジュールの透
過量が顕著に低下することがあり、特に原液に多量の不
溶性粒子が含有されている場合に多く発生している。However, according to the experience of the present inventor, when the parallel membrane module is operated for a long period of time, the permeation amount of the far-end membrane module may be significantly reduced, particularly when the stock solution contains a large amount of insoluble particles. Many have occurred.
膜モジュールにおいては、使用時間の経過と共に膜に
目詰まりが発生し、透過量が次第に低下していく現象は
よく知られている。しかしながら、この現象では、上記
並列膜モジュールの運転において、遠端側の膜モジュー
ルが他の膜モジュールよりも目詰まりを発生し易いこと
を解明できない。In a membrane module, it is well known that the membrane is clogged with the elapse of use time and the amount of permeation gradually decreases. However, this phenomenon cannot elucidate that the far-end membrane module is more likely to cause clogging than the other membrane modules in the operation of the parallel membrane module.
そこで、本発明者においてはその解明を行うべく、鋭
意探求したところ、その原因は目詰まりを惹起する原液
中の不溶性粒子が、上記原液供給用幹管の流路断面中、
最も流速の大なる中央部に集まり、この中央部分の原液
流の大部分が上記最遠端の膜モジュールに流入し、他の
膜モジュールには原液供給用幹管における流路断面周囲
部での不溶性粒子量の少ない原液が流入する結果であ
り、後述の試験結果からも裏付けられる。Therefore, in order to elucidate the inventor, the inventor of the present invention sought intensively, and the cause was insoluble particles in the stock solution causing clogging, in the cross section of the flow path of the stock tube for stock solution supply,
The concentrate concentrates in the central part where the flow velocity is the largest, and most of the stock solution flow in this central part flows into the above-mentioned farthest end membrane module, and the other membrane modules are in the periphery of the cross section of the stock solution supply main pipe at the cross section of the flow channel. This is the result of a stock solution having a small amount of insoluble particles flowing therein, which is supported by the test results described later.
本発明の目的は、並列膜モジュールを運転する場合の
上記遠端側膜モジュールの目詰まりを防止し、全膜モジ
ュールの透過性能を長期にわたり安定に維持し得る膜モ
ジュールの運転方法を提供することにある。An object of the present invention is to provide a method of operating a membrane module that can prevent clogging of the above-mentioned far-end membrane module when operating a parallel membrane module and can stably maintain the permeation performance of all membrane modules over a long period of time. It is in.
本発明に係る膜モジュールの運転方法は、遠端を閉鎖
した原液供給用幹管と、同じく遠端を閉鎖した濃縮原液
流出用幹管との間に数台の膜モジュールを配設し、原液
供給用管の近端側より原液を送って当該原液を処理する
方法において、原液供給用幹管と濃縮原液流出用幹管と
を、最遠端の膜モジュールよりも遠方側においてバイパ
ス管で連通し、原液を該バイパス管にバイパスさせつつ
処理することを特徴とする構成である。The method for operating a membrane module according to the present invention comprises disposing several membrane modules between a stock solution supply main pipe having a closed distal end and a concentrated stock solution flowing main pipe also having a closed distal end. In the method of processing a stock solution by sending the stock solution from the near end side of the supply tube, the stock solution supply main tube and the concentrated stock solution outflow main tube are connected by a bypass tube at a farther side than the farthest end membrane module. Then, the processing is performed while the stock solution is bypassed to the bypass pipe.
膜の目詰まりを惹起する原液中の不溶性粒子は原液供
給用幹管の流路断面中、管との摩擦が小さく、流速の最
も大なる中央部を流れ、この中央部の原液流量の大部分
が最遠端のバイパス管を流れるので、上記不溶性粒子を
バイパス管でバイパスさせ得、膜モジュールに流入する
のを軽減できる。Insoluble particles in the stock solution that cause clogging of the membrane flow through the center of the stock solution supply main pipe, where the friction with the pipe is small and the flow velocity is the highest, in the cross section of the flow path of the stock solution supply pipe, and the bulk of the stock solution flow rate at this center is Flows through the bypass pipe at the farthest end, the insoluble particles can be bypassed by the bypass pipe, and the inflow of the particles into the membrane module can be reduced.
本発明において対象とする原液は、通常0.5μｍ以上
の不溶性粒子を含有している水溶液、または懸濁液であ
り、特に１μｍ以上の粒子を含有している場合に極めて
有効である。The undiluted solution to be used in the present invention is usually an aqueous solution or suspension containing insoluble particles of 0.5 μm or more, and is particularly effective when particles of 1 μm or more are contained.
以下、図面により本発明の実施例について説明する。 Hereinafter, embodiments of the present invention will be described with reference to the drawings.
図面は、本発明において使用する膜分離システムを示
している。The drawings show the membrane separation system used in the present invention.
図において、１は原液供給用幹管、２は濃縮原液流出
用幹管であり、共に遠端10,20を閉鎖してある。M1,M2,
……は互いに並列な膜モジュールであり、原液供給用幹
管１と濃縮原液流出用幹管２との間に枝管3,3によって
連結してある。4,……は膜モジュールM1,……の透過液
取出管を、５は原液タンクを、61は原液供給ポンプを、
62はフイルターを、63は原液循環ポンプを、７は循環配
管をそれぞれ示している。Ａはバイパス管であり、最遠
端の膜モジュールM5よりも遠方側において、原液供給用
幹管１と濃縮原液流出用幹管２とを該バイパス管Ａによ
り連通してある。ｖは開閉弁である。In the figure, 1 is a main tube for supplying a stock solution, 2 is a main tube for outflow of a concentrated stock solution, and both of the distal ends 10 and 20 are closed. M 1 , M 2 ,
.. Are membrane modules parallel to each other, and are connected by branch pipes 3, 3 between the main solution supply main pipe 1 and the concentrated stock solution discharge main pipe 2. 4, ...... membrane module M 1, the permeate extraction tube ......, the starting solution tank 5, 61 the starting solution feed pump,
62 indicates a filter, 63 indicates a stock solution circulation pump, and 7 indicates a circulation pipe. A is a bypass pipe, the far side of the membrane module M 5 of the farthest end, the stock solution supply stem tube 1 and the concentrated stock solution outflow stem tube 2 are communicated with the bypass tube A. v is an on-off valve.
上記膜モジュールM1…には限外濾過膜モジュール、逆
透過膜モジュール、精密濾過膜モジュール等を使用でき
る。また、モジュールの形成としては、スパイラル型、
中空糸膜型、チューブラー型、平膜型等を使用できる
が、特に本発明は原液流路断面の小さいスパイラル型、
中空糸膜型、平膜型に有効である。上記バイパス管に
は、流量調整弁、ストレーナー等を設けることもでき
る。モジュールの並列台数は通常２台以上であるが１台
でもよい。本発明により、上記の膜分離システムを運転
するには、原液をバイパス管Ａにバイパスさせつつ循環
ポンプ63により、原液供給用幹管１→各膜モジュール
M1,……→濃縮原液流出用幹管２→循環用配管７の回路
で循環させ、透過水量に応じて原液供給ポンプ61により
原液を補給する。バイパス管Ａの原液流量Q1と、全膜モ
ジュールM1,……に対する原液流量Q2との比Q1/Q2は0.01
〜1.0とすることが適当である。As the membrane module M 1 , an ultrafiltration membrane module, a reverse permeable membrane module, a microfiltration membrane module, or the like can be used. In addition, spiral type,
A hollow fiber membrane type, a tubular type, a flat membrane type, etc. can be used.
It is effective for hollow fiber membrane type and flat membrane type. The bypass pipe may be provided with a flow control valve, a strainer, and the like. The number of parallel modules is usually two or more, but may be one. According to the present invention, in order to operate the above-mentioned membrane separation system, the stock solution supply main pipe 1 → each membrane module is operated by the circulation pump 63 while the stock solution is bypassed to the bypass pipe A.
M 1 ,... → the concentrated stock solution outflow main pipe 2 → circulation pipe 7 circulates in the circuit, and stock solution is supplied by stock solution supply pump 61 according to the amount of permeated water. The ratio Q 1 / Q 2 of the stock solution flow rate Q 1 of the bypass pipe A to the stock solution flow rate Q 2 for all the membrane modules M 1 ,.
It is appropriate to set it to 1.0.
この補給原液中の不溶性粒子はフイルター62で除去で
きる。しかし、フイルター62を通過した極微細粒子が原
液循環路内で結合して粗大化し、（0.5μｍ以上）ま
た、原液循環路内に新に粗大粒子が生成し、これらの不
溶性粒子が原液供給用幹管１内を流れる。この場合、こ
れら不溶性粒子の大部分は原液供給用幹管１の流路断面
中、流速の最も大きい中央部に集中する。而るに、途中
の原液供給用幹管１の最遠側のバイパス管Ａに流入する
原液は、同上流路断面の中央部を流れるものが大部分で
ある。従って、上記不溶粒子の大部分はバイパス管Ａに
流入し、各膜モジュールM2,……に流入する不溶性粒子
量は僅かであるから、その不溶性粒子による膜モジュー
ルの目詰まりをよく軽減できる。Insoluble particles in the stock solution can be removed by the filter 62. However, the ultrafine particles that have passed through the filter 62 are combined and coarsened in the stock solution circulation path (0.5 μm or more), and coarse particles are newly generated in the stock solution circulation path, and these insoluble particles are used for stock solution supply. It flows inside the main pipe 1. In this case, most of these insoluble particles are concentrated at the central portion where the flow velocity is the highest in the cross section of the flow path of the stock solution supply main pipe 1. The majority of the undiluted solution flowing into the bypass pipe A on the farthest side of the undiluted solution supply main pipe 1 flows in the middle of the cross section of the same flow path. Therefore, most of the insoluble particles flow into the bypass pipe A, and the amount of insoluble particles flowing into each of the membrane modules M 2 ,... Is small, so that clogging of the membrane modules by the insoluble particles can be reduced well.
このことは、次の試験例からも明らかである。 This is clear from the following test examples.
膜モジュールの使用台数は５台とし、各膜モジュール
にはUF膜モジュールを使用した。原液にカチオン電着塗
料を使用し、前記したQ1/Q2を約0.2にして本発明により
膜モジュールを運転し各膜モジュールの初期透過水量並
びに１年後での透過量を測定したところ第一表の通りで
あった。The number of membrane modules used was 5, and a UF membrane module was used for each membrane module. Using the cationic electrodeposition paint as the stock solution, the above-mentioned Q 1 / Q 2 was set to about 0.2, the membrane module was operated according to the present invention, and the initial permeated water amount of each membrane module and the permeation amount after one year were measured. It was as shown in the table.
これに対し、バイパス管Ａのバルブを閉にし、従来法
により膜モジュールを運転し、各膜モジュールの初期透
過量並びに１年後での透過量を測定したところ第二表の
通りであり、遠端側のNO4並びにNO5膜モジュールに顕著
な透過量の低下が観られた。On the other hand, the valve of the bypass pipe A was closed, the membrane module was operated by the conventional method, and the initial permeation amount and the permeation amount after one year of each membrane module were measured. A remarkable decrease in the permeation amount was observed in the NO4 and NO5 membrane modules on the end side.
上述した通り、本発明に係る並列膜モジュールの運転
方法によれば、最遠端の膜モジュールよりも遠方側にバ
イパス管を設け、原液をこのバイパス管にバイパスさせ
つつ処理するだけで遠端側膜モジュールの目詰まりを軽
減できる。従って、バイパス管を付加するだけの極めて
簡単な措置で、長期にわたって安定な透過性能を維持で
きる。As described above, according to the operating method of the parallel membrane module according to the present invention, the bypass pipe is provided farther than the farthest end membrane module, and the raw solution is processed while being bypassed to the bypass pipe. Clogging of the membrane module can be reduced. Therefore, stable permeation performance can be maintained for a long period of time with a very simple measure simply by adding a bypass pipe.
図面は本発明において使用する膜分離システムの一例を
示す説明図である。 １……原液供給用幹管、２……濃縮原液流出用幹管、M1
〜M5……膜モジュール、Ａ……バイパス管The drawing is an explanatory view showing one example of a membrane separation system used in the present invention. 1 ... Main tube for supply of undiluted solution, 2 ... Main tube for outflow of concentrated undiluted solution, M 1
~ M 5 …… membrane module, A …… bypass
Claims (1)
遠端を閉鎖した濃縮原液流出用幹管との間に数台の膜モ
ジュールを配設し、原液供給用幹管の近端側より原液を
送って当該原液を処理する方法において原液供給用幹管
と濃縮原液流出用幹管とを、最遠端の膜モジュールより
も遠方側においてバイパス管で連通し、原液を該バイパ
ス管にバイパスさせつつ処理することを特徴とする膜モ
ジュールの運転方法。(1) A plurality of membrane modules are arranged between a stock solution supply main pipe closed at a far end and a concentrated stock solution flow main pipe also closed at a far end. In the method of treating the undiluted solution by sending the undiluted solution from the end side, the undiluted solution supply main tube and the concentrated undiluted solution outflow main tube are communicated with a bypass tube farther than the farthest end membrane module, and the undiluted solution is bypassed. A method for operating a membrane module, wherein the treatment is performed while bypassing the tube.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11562390A JP2852958B2 (en) | 1990-05-01 | 1990-05-01 | Operating method of membrane module |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11562390A JP2852958B2 (en) | 1990-05-01 | 1990-05-01 | Operating method of membrane module |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0411929A JPH0411929A (en) | 1992-01-16 |
| JP2852958B2 true JP2852958B2 (en) | 1999-02-03 |
Family
ID=14667238
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP11562390A Expired - Fee Related JP2852958B2 (en) | 1990-05-01 | 1990-05-01 | Operating method of membrane module |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2852958B2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3040313A3 (en) * | 2004-06-24 | 2016-11-23 | Desalitech Ltd | Continuous closed-circuit desalination apparatus without containers |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| IL157430A (en) * | 2003-08-17 | 2009-08-03 | Avi Efraty | Apparatus for continuous closed circuit desalination under variable pressure with a single container |
| EP1743689A1 (en) * | 2005-07-13 | 2007-01-17 | KRONES Aktiengesellschaft | Crossflow filtration apparatus and process |
| JP4929202B2 (en) * | 2008-02-20 | 2012-05-09 | 三菱重工業株式会社 | Method and apparatus for cleaning reverse osmosis membrane module |
| AU2010274473B2 (en) * | 2009-07-21 | 2015-07-02 | Toray Industries, Inc. | Water producing system |
-
1990
- 1990-05-01 JP JP11562390A patent/JP2852958B2/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3040313A3 (en) * | 2004-06-24 | 2016-11-23 | Desalitech Ltd | Continuous closed-circuit desalination apparatus without containers |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0411929A (en) | 1992-01-16 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| LAPS | Cancellation because of no payment of annual fees |