JPH0760073A - Membrane separation apparatus - Google Patents
Membrane separation apparatusInfo
- Publication number
- JPH0760073A JPH0760073A JP21306293A JP21306293A JPH0760073A JP H0760073 A JPH0760073 A JP H0760073A JP 21306293 A JP21306293 A JP 21306293A JP 21306293 A JP21306293 A JP 21306293A JP H0760073 A JPH0760073 A JP H0760073A
- Authority
- JP
- Japan
- Prior art keywords
- membrane
- membrane module
- permeated water
- module
- water
- 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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Links
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は膜分離装置に係り、特
に、精密濾過（ＭＦ）膜、限外濾過（ＵＦ）膜又は逆浸
透（ＲＯ）膜等を備えた膜モジュールにより原液を膜分
離処理するに当り、膜の破損による膜面からの一次側原
液の二次側透過水側への漏出を検出して、得られる処理
水の汚染を確実に防止する膜分離装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a membrane separation device, and particularly to a membrane separation of an undiluted solution by a membrane module equipped with a microfiltration (MF) membrane, an ultrafiltration (UF) membrane or a reverse osmosis (RO) membrane. The present invention relates to a membrane separation device which detects leakage of a primary side stock solution from a membrane surface to a secondary side permeated water side due to breakage of the membrane during treatment, and reliably prevents contamination of the obtained treated water.
【０００２】[0002]
【従来の技術】近年、膜分離技術の発達により、各種の
分野で膜濾過が適用されるようになった。2. Description of the Related Art In recent years, with the development of membrane separation technology, membrane filtration has come to be applied in various fields.
【０００３】即ち、従来、除濁、除菌などの分野におい
て、膜濾過は多用されていたが、近年、クロス・フロー
型の膜モジュールや、定期的な逆洗操作により長期間濾
過を継続できるデッドエンド型の膜モジュールの発達に
より、膜濾過を適用できる被処理液（原液）の濃度範囲
が拡大された。これらクロス・フロー型の膜モジュール
や、定期的に逆洗を行なうデッドエンド型の膜モジュー
ルを用いれば、原液の濁度変動があっても、濾過速度を
使用に耐えない程の速度にまで低下させることなく、膜
濾過を継続させることができる。That is, conventionally, membrane filtration has been widely used in fields such as turbidity removal and sterilization, but in recent years, filtration can be continued for a long time by a cross-flow type membrane module or regular backwashing operation. With the development of dead-end type membrane modules, the concentration range of the liquid to be treated (stock solution) to which membrane filtration can be applied has been expanded. By using these cross-flow type membrane modules and dead-end type membrane modules that perform regular backwashing, the filtration rate can be reduced to an unusable rate even if the turbidity of the stock solution changes. Membrane filtration can be continued without being performed.
【０００４】このため、河川水、工業用水、上水をＲＯ
膜分離するための前処理として、凝集，沈殿，濾過に代
わって、ＵＦ膜やＭＦ膜で膜濾過を行い、前処理プロセ
スを簡素化することが可能になった。For this reason, river water, industrial water and tap water are RO
As a pretreatment for membrane separation, it is possible to simplify the pretreatment process by performing membrane filtration with a UF membrane or an MF membrane instead of coagulation, precipitation and filtration.
【０００５】しかし、濾過水（透過水）を上水道などの
飲料水等に供じる場合には、高水質の処理水を確実に得
るために、上記の用途以上の安全装置、即ち、膜面から
の一次側原液の二次側透過水中への漏出を検出する経済
的な装置の実用化が課題であった。However, when the filtered water (permeated water) is supplied to drinking water such as tap water, in order to reliably obtain treated water of high water quality, a safety device more than the above-mentioned use, that is, a membrane surface is used. The practical application of an economical device for detecting the leakage of the undiluted solution on the primary side into the permeated water on the secondary side was a problem.
【０００６】従来、膜面からの一次側原液の漏出の検出
手段としては、透過水の濁度を測定する方法が浄水処理
分野では一般的な方法であった。しかし、ＭＦ膜、ＵＦ
膜、ＲＯ膜の透過水は、原理的に濁質を含んでいないた
め、光学的に濁度を検出してその水質を比較することは
できない。Conventionally, as a means for detecting the leakage of the primary side stock solution from the membrane surface, a method of measuring the turbidity of permeated water has been a general method in the field of water purification treatment. However, MF membrane, UF
Since the permeated water of the membrane and the RO membrane does not contain turbidity in principle, it is impossible to optically detect turbidity and compare the water quality.
【０００７】従って、ＭＦ膜やＵＦ膜、ＲＯ膜などの膜
が損傷して微少量の一次側原液が二次側透過水中に漏出
したとしても、その量が微少量である場合には濁度とし
て検出することはできない。逆に、透過水の濁度を検出
できる場合、その処理水系は決定的な膜の損傷を抱えて
おり、これを修理、復旧するには多大な工数を必要とす
る。Therefore, even if a membrane such as an MF membrane, a UF membrane or an RO membrane is damaged and a small amount of the primary side stock solution leaks into the secondary side permeate, if the amount is very small, the turbidity will be high. Can not be detected as. On the contrary, when the turbidity of the permeate can be detected, the treated water system has a definite membrane damage, and it takes a lot of man-hours to repair and restore it.
【０００８】透過水を上水道などの飲料に供じる場合に
は、たとえ膜の損傷が生じたとしても、修理、復旧が速
やかにできるように、それを早期に検出することが重要
である。そこで、ＲＯ膜装置への給水水質を判定する指
標として開発されたＦＩ値の測定手法を、ＭＦ膜やＵＦ
膜、ＲＯ膜などの透過水の水質判定に転用することが、
現在行われている。When the permeated water is supplied to drinking water such as waterworks, it is important to detect the damage of the membrane early so that repair and restoration can be promptly performed even if the membrane is damaged. Therefore, the FI value measurement method developed as an index for determining the water quality of the water supplied to the RO membrane device is used as an MF membrane or UF membrane.
It can be diverted to determine the quality of permeated water such as membranes and RO membranes.
Currently being conducted.
【０００９】ＦＩ値の測定手法を用いれば、膜透過水を
１０〜２０リットル、孔径０．４５μｍのメンブレンフ
ィルタで濾過するために、膜透過水中に微少量の濁質が
含まれていても、メンブレンフィルタ上に捕捉してその
存在を検出することができる。When the FI value measuring method is used, the membrane permeated water is filtered with a membrane filter having a pore size of 0.45 μm and a membrane permeated water of 10 to 20 liters. Therefore, even if a slight amount of suspended matter is contained in the membrane permeated water, It can be captured on a membrane filter and its presence detected.
【００１０】[0010]
【発明が解決しようとする課題】しかし、このＦＩ値を
測定するには、１サンプルについて約３０分を要し、大
量のサンプルを継続的に測定するには多大な費用と労力
及び時間を必要とした。However, it takes about 30 minutes for one sample to measure the FI value, and it requires a great deal of cost, labor and time to continuously measure a large amount of sample. And
【００１１】また、ＦＩ値などで膜の損傷による微少量
の一次側原液の透過水中への漏出を検出できたとして
も、既に何らかの事故によって二次側透過水が汚染され
たことを検出したことに過ぎず、漏出を防止し得るもの
ではない。Further, even if the leakage of a small amount of the primary side stock solution into the permeated water due to the membrane damage can be detected by the FI value or the like, it has already been detected that the secondary side permeated water is contaminated due to some accident. It does not prevent leakage.
【００１２】このようなことから、膜の損傷による微少
量の一次側原液の二次側透過水中への漏出を効率的に検
出するだけでなく、同時に漏出を防止する装置の開発が
望まれているのが現状である。Therefore, it is desired to develop a device that not only efficiently detects a small amount of undiluted solution on the primary side into the permeated water on the secondary side due to damage to the membrane, but at the same time prevents the leakage. It is the current situation.
【００１３】なお、このような目的に対して、第１の膜
モジュールの透過水を第２の膜モジュールに通し、第１
の膜モジュールから漏洩した懸濁質を阻止するととも
に、第２の膜モジュールの圧力上昇を検出する方法が提
案されている。この方法においては、第２の膜モジュー
ルは第１の膜モジュールよりも幾分大きい０．１〜１μ
ｍ程度の孔径のＭＦ膜を用いる。For such a purpose, the permeated water of the first membrane module is passed through the second membrane module to obtain the first membrane module.
The method of preventing the suspended solids leaking from the second membrane module and detecting the pressure increase of the second membrane module has been proposed. In this method, the second membrane module is slightly larger than the first membrane module by 0.1-1 μm.
An MF membrane with a pore size of about m is used.
【００１４】しかし、本発明者は、前述したようにＦＩ
値測定などの手段による、膜損傷の検出法について検討
したところ、膜に異常がなくても、その膜の孔径より大
きい後段のＭＦ膜において、ＦＩ値が検出されることを
知見した。即ち、膜に異常がなく正常な第１の膜モジュ
ールの透過水を第２の膜モジュールのＭＦ膜に通水する
場合でも、経時により次第に第２の膜モジュールの圧力
上昇が生じることが明らかとなった。However, as described above, the present inventor
When the method for detecting the membrane damage by means such as value measurement was examined, it was found that the FI value was detected even in the MF membrane in the latter stage having a larger pore size than the membrane, even if the membrane had no abnormality. That is, even when the normal permeated water of the first membrane module having no abnormality in the membrane is passed through the MF membrane of the second membrane module, it is clear that the pressure increase of the second membrane module gradually occurs over time. became.
【００１５】このように、単に第１の膜モジュールの膜
よりも幾分大きい０．１〜１μｍ程度の孔径のＭＦ膜を
備えた第２の膜モジュールを用いるだけでは、膜が正常
な場合でも、第２の膜モジュールのＭＦ膜を頻繁に取り
替える必要があり、経済的に不利である。このようなこ
とから、より有効な方法の開発が望まれている。Thus, even if the membrane is normal, simply using the second membrane module provided with the MF membrane having a pore size of about 0.1 to 1 μm, which is slightly larger than the membrane of the first membrane module. The MF membrane of the second membrane module needs to be frequently replaced, which is economically disadvantageous. Therefore, it is desired to develop a more effective method.
【００１６】本発明は上記従来の実情に鑑みてなされた
ものであって、膜の破損による膜面からの一次側原液の
二次側透過水への漏出を確実に検知して、得られる処理
水の汚染を防止する膜分離装置であって、膜の交換を頻
繁に行なう必要がない膜分離装置を提供することを目的
とする。The present invention has been made in view of the above-mentioned conventional circumstances, and the treatment obtained by surely detecting the leakage of the primary side stock solution from the membrane surface to the secondary side permeated water due to the damage of the membrane. An object of the present invention is to provide a membrane separation device that prevents water contamination and does not require frequent membrane replacement.
【００１７】[0017]
【課題を解決するための手段】本発明の膜分離装置は、
原液を受け入れて膜分離処理する第１の膜モジュール
と、該第１の膜モジュールの透過水を受け入れて膜分離
処理するＭＦ膜を有する第２の膜モジュールと、前記第
１の膜モジュールの透過水を該ＭＦ膜よりも上流側から
系外へ取り出す取出手段と、前記第１の膜モジュールの
透過水を前記取出手段と前記第２の膜モジュールとに切
り換えて流通させるための流路切換手段とを備えてなる
ことを特徴とする。Means for Solving the Problems The membrane separation device of the present invention comprises:
A first membrane module that receives the undiluted solution and performs the membrane separation treatment, a second membrane module that has an MF membrane that receives the permeated water of the first membrane module and performs the membrane separation treatment, and the permeation of the first membrane module. Withdrawal means for taking out water from the upstream side of the MF membrane to the outside of the system, and flow path switching means for switching the permeated water of the first membrane module to the withdrawal means and the second membrane module for circulation. It is characterized by comprising and.
【００１８】[0018]
【作用】本発明の膜分離装置にあっては、次のようにし
て膜分離処理を行うことができる。In the membrane separation apparatus of the present invention, the membrane separation treatment can be performed as follows.
【００１９】即ち、第１の膜モジュールを間欠的に運転
し、この第１の膜モジュールが運転を再開した直後の一
定期間だけ、第２の膜モジュールを運転させて、第１の
膜モジュールの透過水を第２の膜モジュールに導入する
流路を選択する。That is, the first membrane module is operated intermittently, and the second membrane module is operated only for a certain period immediately after the first membrane module is restarted to operate the first membrane module. A channel for introducing the permeated water into the second membrane module is selected.
【００２０】このとき、例えば、第２の膜モジュールの
差圧を測定し、所定の期間内に所定以上の圧力の上昇が
検出されなかった場合には、第１の膜モジュールの透過
水を第２の膜モジュールのＭＦ膜よりも上流側から系外
へ取り出す流路を選択する。At this time, for example, the differential pressure of the second membrane module is measured, and when the rise of the pressure more than a predetermined value is not detected within the predetermined period, the permeated water of the first membrane module is changed to the first The flow path to be taken out of the system from the upstream side of the MF membrane of the second membrane module is selected.
【００２１】第１の膜モジュールの膜に損傷が生じ、一
次側原液が二次側透過水中に漏出した場合には、この濁
質は第２の膜モジュールのＭＦ膜に捕捉されるため、系
外に排出される処理水（第２の膜モジュールの透過水）
に濁質が含まれることはない。この場合、所定期間内に
第２の膜モジュールの差圧の上昇が生じ、濁質の漏出が
検出されるため、第１の膜モジュールの透過水は直接系
外へ排出することなく、第２の膜モジュールに導入する
流路選択のまま処理を継続する。When the membrane of the first membrane module is damaged and the primary side stock solution leaks into the secondary side permeate, the suspended matter is captured by the MF membrane of the second membrane module. Treated water discharged to the outside (permeate of the second membrane module)
Does not contain turbidity. In this case, since the differential pressure of the second membrane module rises within a predetermined period and the leakage of suspended matter is detected, the permeated water of the first membrane module is not directly discharged to the outside of the system, The process is continued with the flow path selected to be introduced into the membrane module.
【００２２】このように、第１の膜モジュールの膜の異
常により一次側原液が二次側透過水中に漏出した場合に
は、この透過水は第２の膜モジュールのＭＦ膜で処理さ
れるため、第１の膜モジュールで漏出した濁質が系外へ
排出される処理水中に混入するのを阻止することができ
る。In this way, when the primary side stock solution leaks into the secondary side permeate due to the abnormality of the membrane of the first membrane module, this permeate is treated by the MF membrane of the second membrane module. It is possible to prevent the suspended matter leaked from the first membrane module from being mixed into the treated water discharged to the outside of the system.
【００２３】また、第１の膜モジュールの膜に異常がな
く、第２の膜モジュールの差圧の上昇が規定以内の場合
には、第２の膜モジュールによる処理は継続されず、第
２の膜モジュールの運転は停止されるため、第２の膜モ
ジュールの膜が不必要な汚染を起こすことはない。Further, when there is no abnormality in the membrane of the first membrane module and the increase in the differential pressure of the second membrane module is within the specified range, the treatment by the second membrane module is not continued and the second membrane module does not continue. Since the operation of the membrane module is stopped, the membrane of the second membrane module does not cause unnecessary contamination.
【００２４】このため、第２の膜モジュールのＭＦ膜を
頻繁に交換する必要はなくなる。Therefore, it is not necessary to frequently replace the MF membrane of the second membrane module.
【００２５】なお、本発明の膜分離装置において、第１
の膜モジュールは間欠的に運転する場合に限られず、後
述の如く、連続運転にて行うことができることは言うま
でもない。In the membrane separation device of the present invention, the first
It is needless to say that the membrane module of (1) is not limited to the case where it is operated intermittently, and can be performed in continuous operation as described later.
【００２６】[0026]
【実施例】以下、図面を参照して本発明の実施例につい
て詳細に説明する。Embodiments of the present invention will now be described in detail with reference to the drawings.
【００２７】図１，２は各々本発明の膜分離装置の一実
施例を示す系統図である。1 and 2 are system diagrams showing an embodiment of the membrane separation apparatus of the present invention.
【００２８】図１において、１は第１の膜モジュール、
２は第２の膜モジュールであり、それぞれ膜１Ａ，２Ａ
（２ＡはＭＦ膜）により原液室１ａ，２ａと透過水室１
ｂ，２ｂとに仕切られている。３は演算装置であり、１
１〜１５の各符号は配管を示す。Ｖ1 ，Ｖ2 ，Ｖ3 はバ
ルブ、Ｐ1 ，Ｐ2 はポンプ、ＰＩは圧力計（差圧計）で
ある。In FIG. 1, 1 is a first membrane module,
2 is a second membrane module, which is membrane 1A, 2A, respectively
(2A is an MF membrane) with the stock solution chambers 1a and 2a and the permeate chamber 1
It is divided into b and 2b. 3 is an arithmetic unit, 1
Each code | symbol of 1-15 shows piping. V 1 , V 2 and V 3 are valves, P 1 and P 2 are pumps, and PI is a pressure gauge (differential pressure gauge).
【００２９】第２の膜モジュール２はデッドエンド濾過
方式のものであり、この第２の膜モジュール２の上流側
及び下流側に設けられたバルブＶ1 ，Ｖ2 は自動弁であ
って、第１の膜モジュール１の濾過工程と連動して作動
する電気操作回路を有する。The second membrane module 2 is of a dead end filtration type, and the valves V 1 and V 2 provided on the upstream side and the downstream side of the second membrane module 2 are automatic valves. 1 has an electric operation circuit that operates in conjunction with the filtration process of the membrane module 1.
【００３０】図１において、演算装置３には圧力計ＰＩ
の測定値が入力されると共に、ポンプＰ2 の作動、停止
及びバルブＶ1 ，Ｖ2 ，Ｖ3 の開閉制御信号が出力され
る。In FIG. 1, the arithmetic unit 3 includes a pressure gauge PI.
Is input, and at the same time, the operation and stop of the pump P 2 and the open / close control signals of the valves V 1 , V 2 and V 3 are output.
【００３１】図１に示す膜分離装置は、加圧ポンプＰ1
と吸引ポンプＰ2 との併用により第１の膜モジュールの
濾過を行う型式のものである。The membrane separation device shown in FIG. 1 has a pressure pump P 1
And a suction pump P 2 are used together to filter the first membrane module.
【００３２】このような膜により処理を行うには、ポン
プＰ1 ，Ｐ2 を作動させて配管１１より原液を第１の膜
モジュール１に導入し、透過水を配管１２より取り出
す。一方、濃縮水は配管１３より取り出す。In order to carry out the treatment with such a membrane, the pumps P 1 and P 2 are operated to introduce the stock solution into the first membrane module 1 through the pipe 11, and the permeated water is taken out through the pipe 12. On the other hand, the concentrated water is taken out from the pipe 13.
【００３３】このような第１の膜モジュール１による濾
過は間欠的に実施し、濾過休止時には第１の膜モジュー
ル１の膜１Ａのケーク層の除去処理を行う。このケーク
層の除去は、気液混合液による膜面の擦洗や、透過水側
からの逆流洗浄などにより行われる。Filtration by the first membrane module 1 is intermittently performed, and the cake layer of the membrane 1A of the first membrane module 1 is removed when the filtration is stopped. The cake layer is removed by scrubbing the membrane surface with a gas-liquid mixture, backwashing from the permeate side, or the like.
【００３４】前述の如く、第１の膜モジュール１の運転
時には、バルブＶ1 ，Ｖ2 が自動的に開き、一定の期
間、第１の膜モジュール１の透過水は配管１２より第２
の膜モジュール２に導入される。そして、第２の膜モジ
ュール２の透過水が配管１４より系外へ排出される。As described above, during the operation of the first membrane module 1, the valves V 1 and V 2 are automatically opened, and the permeated water of the first membrane module 1 is supplied to the second pipe through the pipe 12 for a certain period.
Is introduced into the membrane module 2. Then, the permeated water of the second membrane module 2 is discharged out of the system through the pipe 14.
【００３５】このように、第１の膜モジュール１及び第
２の膜モジュール２による２段膜分離処理を一定期間行
ったときに、圧力計ＰＩにより第２の膜モジュール２の
差圧の上昇が所定値以下であった場合には、演算装置３
よりバルブＶ2 を閉、バルブＶ3 を開とする信号を出力
し、第１の膜モジュール１の透過水を配管１２、第２の
膜モジュール２の原液室２ａ、配管１３を経て直接系外
へ排出する。As described above, when the two-stage membrane separation process by the first membrane module 1 and the second membrane module 2 is performed for a certain period, the pressure gauge PI increases the differential pressure of the second membrane module 2. If it is less than the predetermined value, the arithmetic unit 3
A signal for closing the valve V 2 and opening the valve V 3 is output, and the permeated water of the first membrane module 1 is directly outside the system through the pipe 12, the stock solution chamber 2 a of the second membrane module 2 and the pipe 13. To discharge.
【００３６】即ち、第２の膜モジュール２において、所
定以上の差圧の上昇が認められない場合には、第１の膜
モジュール１の膜１Ａに異常がなく、第１の膜モジュー
ル１の一次側原液が二次側透過水中に漏出しておらず、
第１の膜モジュール１の透過水は高水質透過水であるこ
とを示すことから、第１の膜モジュール１の透過水は直
接系外へ排出する。That is, in the second membrane module 2, when the rise of the differential pressure more than a predetermined value is not recognized, the membrane 1A of the first membrane module 1 has no abnormality and the primary membrane module 1 has a primary structure. Side stock solution has not leaked into the secondary side permeate,
Since the permeated water of the first membrane module 1 is shown to be high quality permeated water, the permeated water of the first membrane module 1 is directly discharged to the outside of the system.
【００３７】一方、上記期間内において、第２の膜モジ
ュール２に所定以上の差圧の上昇が検出された場合に
は、このまま、第２の膜モジュール２の処理を継続し、
第１の膜モジュール１の透過水を第２の膜モジュール２
で２段処理した後、系外へ排出する。On the other hand, within the above-mentioned period, when an increase in the differential pressure above the predetermined level is detected in the second membrane module 2, the processing of the second membrane module 2 is continued as it is,
The permeated water of the first membrane module 1 is transferred to the second membrane module 2
After two-stage treatment with, it is discharged out of the system.
【００３８】即ち、第２の膜モジュール２において、所
定以上の差圧の上昇が認められる場合には、第１の膜モ
ジュール１の膜１Ａに異常があり、第１の膜モジュール
１の一次側原液が二次側透過水中に漏出し、第１の膜モ
ジュール１の透過水中に濁質が含まれることを示すこと
から、第１の膜モジュール１の透過水を第２の膜モジュ
ールで処理した後、系外へ排出する。That is, in the second membrane module 2, when a rise in the differential pressure above a predetermined level is recognized, the membrane 1A of the first membrane module 1 is abnormal, and the primary side of the first membrane module 1 is in the abnormal state. Since the undiluted solution leaked into the secondary side permeate and showed that the permeate of the first membrane module 1 contained suspended matter, the permeate of the first membrane module 1 was treated with the second membrane module. Then, it is discharged out of the system.
【００３９】この場合には、必要に応じて、第１の膜モ
ジュール１の運転を停止するなどの警報信号を発信す
る。In this case, an alarm signal for stopping the operation of the first membrane module 1 is issued if necessary.
【００４０】図２に示す膜分離装置は、第１の膜モジュ
ール１の濾過を加圧ポンプＰ1 のみで行うものである。
また、この膜分離装置は、第１の膜モジュール１及び第
２の膜モジュール２の透過水を貯留する透過水槽４と、
この透過水槽４内の透過水を第１の膜モジュール１の透
過水室１ｂに逆流させて逆洗するための手段（配管１
６、ポンプＰ3 及びバルブＶ4 ）を備える。In the membrane separation device shown in FIG. 2, the filtration of the first membrane module 1 is performed only by the pressure pump P 1 .
Further, this membrane separation device includes a permeated water tank 4 that stores permeated water of the first membrane module 1 and the second membrane module 2,
Means for back-flowing the permeated water in the permeated water tank 4 into the permeated water chamber 1b of the first membrane module 1 for backwashing (pipe 1
6, a pump P 3 and a valve V 4 ).
【００４１】この膜分離装置においても、図１に示す膜
分離装置と同様に膜分離処理を行うことができる。そし
て、第１の膜モジュール１の運転停止時には、必要に応
じて、バルブＶ4 を開としてポンプＰ3 を作動させて透
過水槽４中の透過水を逆流させることにより、第１の膜
モジュール１の逆洗を行うことができる。Also in this membrane separation apparatus, the membrane separation treatment can be carried out similarly to the membrane separation apparatus shown in FIG. Then, when the operation of the first membrane module 1 is stopped, the valve V 4 is opened and the pump P 3 is operated to cause the permeated water in the permeated water tank 4 to flow backward, if necessary. Can be backwashed.
【００４２】図１，２のいずれの膜分離装置において
も、第１の膜モジュール１の膜１Ａに異常がある場合に
は第１の膜モジュール１の透過水を第２の膜モジュール
２で処理することにより、処理水中への濁質の混入を確
実に阻止し、一方、第１の膜モジュール１の膜１Ａに異
常がなく、第１の膜モジュールの透過水が十分に高水質
である場合には、第２の膜モジュールを停止して、第２
の膜モジュール２の膜２Ａの不必要な汚染を防止するこ
とができる。In both of the membrane separation apparatuses of FIGS. 1 and 2, when the membrane 1A of the first membrane module 1 is abnormal, the permeated water of the first membrane module 1 is treated by the second membrane module 2. By doing so, it is possible to reliably prevent turbidity from mixing into the treated water, while the membrane 1A of the first membrane module 1 has no abnormality, and the permeated water of the first membrane module has sufficiently high water quality. To stop the second membrane module and
Unnecessary contamination of the membrane 2A of the membrane module 2 can be prevented.
【００４３】なお、上記の説明では、第１の膜モジュー
ルを間欠運転する場合について示したが、本発明の膜分
離装置は間欠運転に限らず、第１の膜モジュールを連続
運転させることもできることは言うまでもない。この場
合には、第１の膜モジュールを連続運転させる一方、第
２の膜モジュールを一定期間毎に所定時間運転し、差圧
の上昇を調べ、差圧の上昇が認められない場合には、再
度第１の膜モジュールのみの処理とし、差圧の上昇が認
められた場合には、第１の膜モジュールと第２の膜モジ
ュールとの２段処理とし、必要に応じて膜分離装置を停
止して第１の膜モジュールの膜の交換を行えば良い。In the above description, the case where the first membrane module is operated intermittently has been described, but the membrane separation apparatus of the present invention is not limited to intermittent operation, and the first membrane module can be operated continuously. Needless to say. In this case, while the first membrane module is continuously operated, the second membrane module is operated at regular intervals for a predetermined time, and the increase in differential pressure is examined. If no increase in differential pressure is observed, If only the first membrane module is treated again, and if an increase in the differential pressure is observed, then it is a two-stage treatment of the first membrane module and the second membrane module, and the membrane separation device is stopped if necessary. Then, the membrane of the first membrane module may be replaced.
【００４４】本発明において、第１の膜モジュールの膜
としては、ＭＦ膜、ＵＦ膜、ＲＯ膜のいずれをも用いる
ことができる。この第１の膜モジュールの濾過方式には
特に制限はなく、全量濾過（デッドエンド濾過）やクロ
スフロー濾過などの通水方式、或いは、単位モジュール
を接続したモジュールスタック、水槽などに膜モジュー
ルを浸漬する方式など、各種の方式を採用することがで
きる。In the present invention, as the membrane of the first membrane module, any of MF membrane, UF membrane and RO membrane can be used. The filtration method of the first membrane module is not particularly limited, and the membrane module is immersed in a water passage method such as dead end filtration or cross-flow filtration, or a module stack in which unit modules are connected, a water tank, or the like. It is possible to adopt various methods such as a method of performing.
【００４５】一方、第２の膜モジュールのＭＦ膜として
は、孔径０．３〜０．８μｍ程度のＭＦ膜を用いたもの
が好ましい。このＭＦ膜の孔径が、０．８μｍを超える
と、正常時の圧力損失は極めて小さいものの、濁質漏出
時にも圧力損失が小さく差圧の上昇を検知しにくくな
る。逆に、孔径０．３μｍ未満のものでは、正常時の圧
力損失が極めて大きく実用に供さない。このような正常
時の圧力損失の増大は、第１の膜モジュールで阻止され
ずに流出する溶存有機物の部分的な阻止現象によるもの
と考えられている。On the other hand, as the MF membrane of the second membrane module, it is preferable to use an MF membrane having a pore diameter of about 0.3 to 0.8 μm. When the pore diameter of the MF membrane exceeds 0.8 μm, the pressure loss in the normal state is extremely small, but the pressure loss is small even when the suspended matter leaks out, and it becomes difficult to detect the rise in the differential pressure. On the other hand, if the pore diameter is less than 0.3 μm, the pressure loss during normal operation is extremely large and it cannot be put to practical use. It is considered that such an increase in pressure loss during normal operation is due to a partial blocking phenomenon of the dissolved organic matter that flows out without being blocked by the first membrane module.
【００４６】本発明において、第２の膜モジュールの濾
過方式は、好ましくはデッドエンド濾過とするのが望ま
しい。In the present invention, the filtration method of the second membrane module is preferably dead end filtration.
【００４７】図１，２に示す実施例のうち、図１に示す
膜は、第１の膜モジュール１の透過水取出配管に吸引ポ
ンプＰ2 を設けたものであるが、このように、吸引ポン
プＰ2 を設けることにより、第１の膜モジュール１の吸
引濾過の推進力と第２の膜モジュール２の加圧濾過の推
進力とを１つのポンプで共用でき、装置の簡素化に有利
である。Of the embodiments shown in FIGS. 1 and 2, the membrane shown in FIG. 1 is obtained by providing a suction pump P 2 in the permeated water extraction pipe of the first membrane module 1. By providing the pump P 2 , one pump can share the driving force for suction filtration of the first membrane module 1 and the driving force for pressure filtration of the second membrane module 2, which is advantageous in simplifying the apparatus. is there.
【００４８】なお、図１，２に示す膜分離装置はいずれ
も本発明の一実施例であって、本発明はその要旨を超え
ない限り、何ら図示のものに限定されるものではない。
例えば、図１，２のいずれにおいても、第１の膜モジュ
ール１の透過水は第２の膜モジュール２の原液室２ａを
経て系外に取り出す構成とされているが、この第１の膜
モジュール１の透過水は、配管１２に分岐する配管（図
１，２において破線で示す配管２０）を設け、直接系外
へ排出するようにすることもできる。The membrane separation apparatus shown in FIGS. 1 and 2 is an embodiment of the present invention, and the present invention is not limited to the illustrated apparatus unless it exceeds the gist.
For example, in both of FIGS. 1 and 2, the permeated water of the first membrane module 1 is configured to be taken out of the system through the stock solution chamber 2a of the second membrane module 2. The permeated water of No. 1 can be directly discharged to the outside of the system by providing a pipe branching to the pipe 12 (pipe 20 shown by a broken line in FIGS. 1 and 2).
【００４９】また、図１，２においては、第１の膜モジ
ュール１個に対して、第２の膜モジュールを１個設けた
ものとしているが、第１の膜モジュールは複数並列に設
け、このようなユニットに対して、第２の膜モジュール
を１個以上設けたものとすることもできる。Further, in FIGS. 1 and 2, one second membrane module is provided for one first membrane module, but a plurality of first membrane modules are provided in parallel. One or more second membrane modules may be provided for such a unit.
【００５０】さらに、第２の膜モジュールは、差圧の測
定に限らず、膜の着色度を測定して第１の膜モジュール
の膜の異常を検知するようにしても良い。Further, the second membrane module is not limited to the measurement of the differential pressure, but the coloration degree of the membrane may be measured to detect the abnormality of the membrane of the first membrane module.
【００５１】[0051]
【発明の効果】以上詳述した通り、本発明の膜分離装置
によれば、第１の膜モジュールの膜の異常により一次側
原液が二次側透過水中に漏出した場合、この濁質を第２
の膜モジュールで除去することにより、高水質の処理水
を安定かつ確実に得ることができる。しかも、第２の膜
モジュールの運転は、必要時のみ行うため、第２の膜モ
ジュールのＭＦ膜の汚染は低減され、膜を頻繁に交換す
る必要はなくなる。As described in detail above, according to the membrane separation apparatus of the present invention, when the primary side stock solution leaks into the secondary side permeate due to the abnormality of the membrane of the first membrane module, this turbidity is Two
By removing it with the membrane module, it is possible to stably and reliably obtain high-quality treated water. Moreover, since the operation of the second membrane module is performed only when necessary, the contamination of the MF membrane of the second membrane module is reduced, and it is not necessary to replace the membrane frequently.
【図１】本発明の膜分離装置の一実施例を示す系統図で
ある。FIG. 1 is a system diagram showing an embodiment of a membrane separation device of the present invention.
【図２】本発明の膜分離装置の別の実施例を示す系統図
である。FIG. 2 is a system diagram showing another embodiment of the membrane separation device of the present invention.
１ 第１の膜モジュール １Ａ 膜 １ａ 原液室 １ｂ 透過水室 ２ 第２の膜モジュール ２Ａ ＭＦ膜 ２ａ 原液室 ２ｂ 透過水室 ３ 演算装置 ４ 透過水槽 1 1st Membrane Module 1A Membrane 1a Stock Solution Chamber 1b Permeate Water Room 2 2nd Membrane Module 2A MF Membrane 2a Stock Solution Room 2b Permeate Water Room 3 Computing Device 4 Permeate Tank
Claims (1)
膜モジュールと、 該第１の膜モジュールの透過水を受け入れて膜分離処理
する精密濾過膜を有する第２の膜モジュールと、 前記第１の膜モジュールの透過水を該精密濾過膜よりも
上流側から系外へ取り出す取出手段と、 前記第１の膜モジュールの透過水を前記取出手段と前記
第２の膜モジュールとに切り換えて流通させるための流
路切換手段とを備えてなる膜分離装置。1. A first membrane module for receiving a raw solution for membrane separation treatment, and a second membrane module having a microfiltration membrane for receiving permeated water of the first membrane module for membrane separation treatment, said first membrane module comprising: A take-out means for taking out the permeated water of the first membrane module from the upstream side of the microfiltration membrane to the outside of the system, and a permeated water of the first membrane module being switched between the take-out means and the second membrane module for distribution. A membrane separation device comprising a flow path switching means for performing the above.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP21306293A JP3401541B2 (en) | 1993-08-27 | 1993-08-27 | Membrane separation device and its operation method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP21306293A JP3401541B2 (en) | 1993-08-27 | 1993-08-27 | Membrane separation device and its operation method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0760073A true JPH0760073A (en) | 1995-03-07 |
| JP3401541B2 JP3401541B2 (en) | 2003-04-28 |
Family
ID=16632905
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP21306293A Expired - Lifetime JP3401541B2 (en) | 1993-08-27 | 1993-08-27 | Membrane separation device and its operation method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3401541B2 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6228271B1 (en) * | 1996-05-28 | 2001-05-08 | Omnium De Traitement Et De Valorisation (Otv) | Method and installation for in situ testing of membrane integrity |
| JP2007313445A (en) * | 2006-05-26 | 2007-12-06 | Nippon Rensui Co Ltd | Wastewater treatment method, wastewater treatment apparatus, and wastewater recovery system |
| CN106731864A (en) * | 2016-12-27 | 2017-05-31 | 贵阳时代沃顿科技有限公司 | A kind of device for the detection of dense net resistance tocrocking |
| JP2017518176A (en) * | 2014-05-30 | 2017-07-06 | ゼットナノ エルエルシーｚＮａｎｏ ＬＬＣ | System for treating water |
| JP2021522794A (en) * | 2018-05-04 | 2021-09-02 | ジェンザイム・コーポレーション | Perfusion bioreactor with filtration system |
| US11401179B2 (en) | 2010-05-21 | 2022-08-02 | Diamond Gold Investors, Llc | Self-assembled surfactant structures |
| CN115403113A (en) * | 2022-11-02 | 2022-11-29 | 山东辰智电子科技有限公司 | Sewage filtering device with switchable filtering components |
-
1993
- 1993-08-27 JP JP21306293A patent/JP3401541B2/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6228271B1 (en) * | 1996-05-28 | 2001-05-08 | Omnium De Traitement Et De Valorisation (Otv) | Method and installation for in situ testing of membrane integrity |
| JP2007313445A (en) * | 2006-05-26 | 2007-12-06 | Nippon Rensui Co Ltd | Wastewater treatment method, wastewater treatment apparatus, and wastewater recovery system |
| US11401179B2 (en) | 2010-05-21 | 2022-08-02 | Diamond Gold Investors, Llc | Self-assembled surfactant structures |
| JP2017518176A (en) * | 2014-05-30 | 2017-07-06 | ゼットナノ エルエルシーｚＮａｎｏ ＬＬＣ | System for treating water |
| CN106731864A (en) * | 2016-12-27 | 2017-05-31 | 贵阳时代沃顿科技有限公司 | A kind of device for the detection of dense net resistance tocrocking |
| JP2021522794A (en) * | 2018-05-04 | 2021-09-02 | ジェンザイム・コーポレーション | Perfusion bioreactor with filtration system |
| CN115403113A (en) * | 2022-11-02 | 2022-11-29 | 山东辰智电子科技有限公司 | Sewage filtering device with switchable filtering components |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3401541B2 (en) | 2003-04-28 |
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