JP2003225661A - Cross flow type filtration apparatus and filtration method - Google Patents
Cross flow type filtration apparatus and filtration methodInfo
- Publication number
- JP2003225661A JP2003225661A JP2002028656A JP2002028656A JP2003225661A JP 2003225661 A JP2003225661 A JP 2003225661A JP 2002028656 A JP2002028656 A JP 2002028656A JP 2002028656 A JP2002028656 A JP 2002028656A JP 2003225661 A JP2003225661 A JP 2003225661A
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- Japan
- Prior art keywords
- filtration
- membrane module
- tank
- calling
- pump
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、精密濾過，限外濾
過等の従来の膜濾過分野において、被処理液を送液ポン
プで大量に強制加圧循環すること無く、エアーリフトの
水流により、エネルギー効率、濾過効率を向上させ、ラ
ンニングコストの低減を図る濾過装置及び濾過方法に関
する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to conventional membrane filtration fields such as microfiltration and ultrafiltration, in which a liquid to be treated is not forced to circulate in a large amount by a liquid-feeding pump, but by a water flow of an air lift, The present invention relates to a filtration device and a filtration method that improve energy efficiency and filtration efficiency and reduce running costs.
【０００２】[0002]
【従来技術】従来型のクロスフロー加圧濾過は、膜面に
平行方向の流れを作り、その流れの力で膜面上の汚れを
洗浄しながら濾過を行うものである。適正な平行流とし
て、被処理液の液線速度を０．５〜５ｍ／ｓｅｃとる必
要がある。このために使用される循環・濾過を司るポン
プは濾過流束に対して極めて大容量な物が必要となり、
その為に濾過流束当りのエネルギー消費が大きくなり、
ランニングコスト中の電気代の占める割合が非常に高く
なっているのが現状である。このように、濾過に必要充
分な線速度と加圧濾過のエネルギーを得る為に、大きな
循環・濾過ポンプを必要とする事がこの濾過装置の欠点
である。又、大きな能力の循環・濾過ポンプによるクロ
スフロー加圧濾過では、膜表面の汚染層が圧縮、緻密化
し、これが濾過抵抗を増大させ、膜本来の濾過性能を充
分に発揮させる事が出来なかった。2. Description of the Related Art Conventional cross-flow pressure filtration creates a flow in a direction parallel to a membrane surface and performs filtration while washing dirt on the membrane surface by the force of the flow. As a proper parallel flow, it is necessary to set the liquid linear velocity of the liquid to be treated to 0.5 to 5 m / sec. The pump that controls circulation and filtration used for this purpose requires an extremely large volume for the filtration flux.
Therefore, the energy consumption per filtration flux becomes large,
The current situation is that the electricity bill accounts for a very high proportion of the running cost. As described above, it is a drawback of this filtration device that a large circulation / filtration pump is required in order to obtain a sufficient and sufficient linear velocity for filtration and energy for pressure filtration. Also, in cross-flow pressure filtration using a circulation / filtration pump with a large capacity, the contaminated layer on the membrane surface was compressed and densified, which increased filtration resistance and the membrane's original filtration performance could not be fully exhibited. .
【０００３】[0003]
【発明が解決しようとする課題】本発明は、循環・濾過
ポンプの消費電力を抑えて、ランニングコストの低減を
図った、高性能な膜モジュール濾過装置及び濾過方法を
提供することを目的とするものである。SUMMARY OF THE INVENTION It is an object of the present invention to provide a high performance membrane module filtration device and a filtration method which reduce the running cost by suppressing the power consumption of the circulation / filtration pump. It is a thing.
【０００４】[0004]
【課題を解決するための手段】本発明者は、上記課題を
解決するために鋭意研究を重ねた結果、被処理液をエア
ーリフトで膜モジュールに供給する事により、その目的
に適合する事を見出し、この知見に基づいて本発明をな
すに至ったものである。すなわち、本発明は、エアーリ
フトによる被処理液の循環濾過装置及び方法に関する。
（１）少なくとも膜モジュール、呼出槽、これらの下部
を連結させた配管、膜モジュールからの被処理水を呼出
槽に戻す配管、エアーリフト用エアー供給手段および濾
過水ポンプで構成される濾過装置、（２）中空糸型、チ
ューブラー型またはスパイラル型の精密濾過膜または限
外濾過膜を用いた膜モジュールを特徴とする上記（１）
記載の濾過装置、（３）濾過水ポンプを、バルブの切り
替え操作により逆圧洗浄用としても使用する事を特徴と
する上記（１）、（２）記載の濾過装置、（４）膜モジ
ュール下部と呼出槽下部を連結させた配管にエアーを導
入し、膜モジュール内にエアーリフトを発生させて、被
処理水を呼出槽から膜モジュール内に吸い込み、膜モジ
ュール上部から被処理水を再び呼出槽に排出する液循環
を行うことを特徴とする濾過方法、（５）呼出槽内の液
面を、常時、膜モジュール上部と同等の高さになるよう
に運転することを特徴とする上記（４）記載の濾過方
法、に関するものである。Means for Solving the Problems As a result of intensive studies for solving the above problems, the present inventor has found that the liquid to be treated is supplied to a membrane module by an air lift to meet the purpose. The present invention has been completed based on the findings and this finding. That is, the present invention relates to an apparatus and method for circulating and filtering a liquid to be treated by an air lift. (1) At least a membrane module, a calling tank, a pipe connecting these lower parts, a pipe for returning water to be treated from the membrane module to the calling tank, an air-lifting air supply means, and a filtering device including a filtered water pump, (2) The above-mentioned (1), which is characterized by a membrane module using a hollow fiber type, tubular type or spiral type microfiltration membrane or ultrafiltration membrane.
The filtration device according to (3), wherein the filtration water pump is also used for back pressure cleaning by switching a valve, and the filtration device according to (1) or (2) above, or (4) lower part of the membrane module. Air is introduced into the pipe that connects the lower part of the membrane and the lower part of the calling tank, an air lift is generated in the membrane module, the treated water is sucked from the calling tank into the membrane module, and the treated water is again drawn from the upper part of the membrane module. (5) The filtration method characterized in that the liquid is circulated to discharge to (5) the liquid level in the inhalation tank is always operated so as to be at the same height as the upper part of the membrane module. ) The described filtration method.
【０００５】[0005]
【発明の実施の形態】以下、本発明について具体的に説
明する。
（ａ）原水タンクと呼出槽間で被処理液の循環を行う。
この循環は、原水タンクと呼出槽の間に循環・濾過ポン
プを設け、これにて原水タンクから呼出槽に送液し、呼
出槽の任意の高さに設けられたオーバフロー口から原水
タンクにもどす。送液量は、次工程の膜濾過流束を上ま
わる量を送液して、原水タンクと呼出槽内の液濃度がほ
ぼ一定になる量とする。又、河川水等の処理の場合は、
原水タンクを不要とし、河川水等から直接呼出槽への送
液循環とする。
（ｂ）呼出槽の横に膜モジュールを垂直にセットして、
その下部と呼出槽下部とを適当な径の配管で連結する。
膜モジュールからの被処理水を呼出槽に戻す配管を膜モ
ジュール上部に連結する。膜モジュール、呼出槽、これ
らの下部を連結させた配管および膜モジュールからの被
処理水を呼出槽に戻す配管の組み合わせからなるものを
濾過部本体と称す。BEST MODE FOR CARRYING OUT THE INVENTION The present invention will be specifically described below. (A) The liquid to be treated is circulated between the raw water tank and the calling tank.
For this circulation, a circulation / filtration pump is provided between the raw water tank and the calling tank, and the liquid is sent from the raw water tank to the calling tank, and returned to the raw water tank from the overflow port provided at any height of the calling tank. . The amount of liquid to be sent is such that the amount of liquid that exceeds the membrane filtration flux in the next step is sent so that the liquid concentrations in the raw water tank and the calling tank become substantially constant. In addition, when treating river water,
The raw water tank is not required, and the liquid is circulated directly from the river water to the calling tank. (B) Set the membrane module vertically next to the calling tank,
The lower part and the lower part of the calling tank are connected by a pipe having an appropriate diameter.
A pipe for returning the treated water from the membrane module to the calling tank is connected to the upper portion of the membrane module. A combination of a membrane module, a calling tank, a pipe connecting these lower parts and a pipe for returning water to be treated from the membrane module to the calling tank is referred to as a filtering unit body.
【０００６】（ｃ）呼出槽内の液面は、常時、膜モジュ
ール上部と同等の高さにするのが適切である。膜モジュ
ール上部の被処理液出口がモジュール壁面に付いている
場合は、呼出槽内の液面は、被処理液出口と同等の高さ
にするのが適切である。この呼出槽内の液面は、膜モジ
ュール上部から、膜モジュール長対比、上に３０％、下
に５０％の範囲でも可能である。
（ｄ）濾過部本体の呼出槽と膜モジュール間で被処理液
の循環を行う。エアーリフト用エアー供給手段とはエア
ーポンプとこれを濾過部本体につなぐエアー配管とから
なるものが好ましい。ポンプ以外の手段でエアーを供給
するものであってもよい。膜モジュール下部と呼出槽下
部を連結させた配管の膜モジュール直下の部分にエアー
配管を接続する。エアー配管は、直接膜モジュールに接
続することも可能であるが、配管の膜モジュール直下の
部分に接続する方が構造上簡単で好ましい。このエアー
配管から、エアーポンプでエアーを送入する事により、
膜モジュールにエアーリフトが造られる。このエアーリ
フトにより、呼出槽から膜モジュール下部へ、膜モジュ
ール下部から膜モジュール上部へ被処理水が誘導され
る。さらにこのエアーリフトによって、膜モジュール上
部より出た被処理水が呼出槽に戻る。戻し口は呼出槽内
の液面より上とする。また、被処理水循環量はエアー送
入量で調整することが好ましい。(C) It is appropriate that the liquid level in the calling tank is always at the same height as the upper part of the membrane module. When the liquid outlet in the upper part of the membrane module is attached to the wall surface of the module, it is appropriate that the liquid surface in the calling tank is at the same height as the liquid outlet. The liquid level in the calling tank can be within the range of 30% above and 50% below the length of the membrane module from the upper portion of the membrane module. (D) The liquid to be treated is circulated between the calling tank of the filtration unit body and the membrane module. The air supply means for the air lift is preferably an air pump and an air pipe connecting the air pump to the filtration unit main body. Air may be supplied by means other than a pump. The air pipe is connected to the portion directly below the membrane module of the pipe connecting the lower part of the membrane module and the lower part of the calling tank. The air pipe can be directly connected to the membrane module, but it is preferable in terms of structure that the air pipe is connected to a portion immediately below the membrane module. By sending air from this air pipe with an air pump,
An air lift is built on the membrane module. By this air lift, the water to be treated is guided from the calling tank to the lower part of the membrane module and from the lower part of the membrane module to the upper part of the membrane module. Further, this air lift returns the water to be treated which has come out from the upper part of the membrane module to the calling tank. The return port should be above the liquid level in the calling tank. Further, it is preferable that the circulating amount of water to be treated is adjusted by the air feeding amount.
【０００７】（ｅ）膜モジュールは、中空糸型、チュー
ブラー型、またはスパイラル型で、精密濾過膜または限
外濾過膜のいずれでも可能である。
（ｆ）膜モジュールの濾過出口に濾過水ポンプを取り付
ける。この濾過水ポンプを、必要に応じて膜表面の汚染
層除去の為に、濾過水を膜表面に対し濾過とは逆向きの
方向から流して洗浄する、逆圧洗浄用としても使用する
ことが可能である。濾過水ポンプを逆洗ポンプとして使
用するために、ポンプの吸込口、吐出口配管にそれぞれ
２個ずつ（計４個）自動弁を取り付けて、自動弁の開閉
で濾過、逆洗運転を切り替える。まず、濾過運転時は、
ポンプ吸込口の２個の自動弁のうち、膜モジュール−ポ
ンプライン（Ｂ）に取り付けた自動弁を開き、ポンプ−
濾過水受けタンクラインの自動弁（Ｄ）を閉じる。ま
た、ポンプ吐出口の自動弁は、膜モジュール−ポンプラ
イン（Ａ）を閉めて、ポンプ−濾過水受けタンクライン
（Ｃ）を開ける。逆洗洗浄時はこの逆動作とする。(E) The membrane module is a hollow fiber type, a tubular type or a spiral type, and can be either a microfiltration membrane or an ultrafiltration membrane. (F) Attach a filtered water pump to the filtration outlet of the membrane module. This filtered water pump can also be used for back pressure cleaning, in which filtered water is flowed from the direction opposite to the filtration to the membrane surface to remove the contaminated layer on the membrane surface, if necessary. It is possible. In order to use the filtered water pump as a backwash pump, two (4 in total) automatic valves are attached to each of the suction port and the discharge port of the pump, and filtration and backwash operation are switched by opening and closing the automatic valve. First, during filtration operation,
Of the two automatic valves at the pump inlet, open the automatic valve attached to the membrane module-pump line (B),
Close the automatic valve (D) of the filtered water receiving tank line. The automatic valve at the pump outlet closes the membrane module-pump line (A) and opens the pump-filtered water receiving tank line (C). This is the reverse operation when backwashing.
【０００８】（ｇ）本発明のエアーリフトの液循環流は
脈流であることが好ましい。脈流が生じている場合の液
循環量の計算は、次のように行う。例えば、液循環脈流
が図５のような波形を示し、３秒に１回の割合で観察さ
れたとする。すなわち、脈流が３秒間隔で生じているの
で、１分間では脈流２０回を生じる。一定流量に換算す
ると、２Ｌ×２０回＝４０Ｌであり、４０Ｌ／ｍｉｎ相
当となる。このようにして、脈流が生じている場合の液
循環量を求める。
（ｈ）エアーリフト用エアーポンプとともに、膜モジュ
ールと呼出槽の間の配管にポンプ（送液ポンプと称す
る）を設置することも可能であるが、送液ポンプを用い
ずにエアーリフト用エアーポンプのみで液循環を行うこ
とが好ましい。(G) The liquid circulating flow of the air lift according to the present invention is preferably a pulsating flow. The calculation of the liquid circulation amount when the pulsating flow is generated is performed as follows. For example, it is assumed that the liquid circulation pulsating flow shows a waveform as shown in FIG. 5 and is observed once every 3 seconds. That is, since the pulsating flow is generated at intervals of 3 seconds, 20 pulsating flows are generated in 1 minute. When converted into a constant flow rate, 2L × 20 times = 40L, which corresponds to 40L / min. In this way, the liquid circulation amount when the pulsating flow is generated is obtained. (H) It is possible to install a pump (referred to as a liquid delivery pump) in the pipe between the membrane module and the calling tank together with the air lift air pump, but without using the liquid delivery pump. It is preferable to circulate the liquid only.
【０００９】[0009]
【実施例】次に、実施例及び比較例によって本発明を説
明する。The present invention will be described below with reference to Examples and Comparative Examples.
【００１０】［実施例１］使用した本発明にかかる装置
概略図を図１に示す。図１において、１が原水ポンプ、
２が循環ポンプであり、濾過部本体にあたる、３が呼出
槽、４が膜モジュールであり、これらの下部を連結させ
た配管、膜モジュール３から被処理水を戻す配管とが設
けられている。５がエアーポンプである。濾過水側の６
が濾過水／逆洗ポンプ、８が濾過水受けタンクである。
この本発明装置にて、原水タンクに米とぎ汁（濁度１４
００ＮＴＵ）３０Ｌを受け、膜モジュールはＵＭＰ−１
５３（旭化成製）、濾過時間５分、逆洗１０秒、エアー
量１０Ｌ／分の運転条件下の濾過能力を確認した。結
果、濾過所要時間は４時間、平均濾過流束１１２ｃｃ／
分の結果を得た。その時の液循環量だが、２Ｌ／分で流
れ方が一定流でなく脈流を生じる事を確認した。[Embodiment 1] FIG. 1 shows a schematic view of an apparatus according to the present invention used. In FIG. 1, 1 is a raw water pump,
Reference numeral 2 is a circulation pump, 3 is a filtration tank, 3 is a calling tank, 4 is a membrane module, and pipes connecting these lower parts and pipes for returning treated water from the membrane module 3 are provided. 5 is an air pump. 6 on the filtered water side
Is a filtered water / backwash pump, and 8 is a filtered water receiving tank.
With this device of the present invention, rice vinegar juice (turbidity 14
00NTU) 30L, membrane module is UMP-1
53 (manufactured by Asahi Kasei), filtration time 5 minutes, backwashing 10 seconds, air capacity 10 L / min. As a result, the filtration time was 4 hours, and the average filtration flux was 112 cc /
I got a minute result. Although it was the liquid circulation amount at that time, it was confirmed that at 2 L / min, the flow was not a constant flow but a pulsating flow.
【００１１】［比較例１］実施例１の濾過装置に変え
て、図２に示す従来のクロスフロー加圧濾過装置を用い
て、エアーを導入しないこと以外は実施例１と同条件に
して濾過能力の比較評価を行った。その結果、濾過所要
時間６．３時間、平均濾過流束７２ｃｃ／分の結果を得
た。又、実施例１と比較例１の濾過流束比較結果を図３
に示す。[Comparative Example 1] A filtration was carried out under the same conditions as in Example 1 except that air was not introduced using the conventional cross-flow pressure filtration device shown in FIG. 2 instead of the filtration device of Example 1. A comparative evaluation of abilities was performed. As a result, the time required for filtration was 6.3 hours, and the average filtration flux was 72 cc / min. In addition, FIG. 3 shows the results of comparing the filtration fluxes of Example 1 and Comparative Example 1.
Shown in.
【００１２】［比較例２］実施例１の濾過装置で、膜モ
ジュールと呼出槽の間の配管に、エアー供給手段を設け
る代わりに、送液ポンプを設けたほかは実施例１と同条
件にして濾過能力を確認した。結果、濾過開始約40分経
過し、濾液トータル量１０Ｌになった時点で、実施例１
に比較して約１／４まで濾過流束が低下したので、運転
を停止した。濾過流束低下原因としては、膜モジュール
に３０ＫＰａ以上の内圧がかかり、従来のクロスフロー
加圧濾過処理特有の膜表面に汚染層の圧縮緻密化現象が
生じ、濾過抵抗が増大したために起きたものと考えられ
る。実施例１と比較例２の濾過流束比較結果を図４に示
す。[Comparative Example 2] The same conditions as in Example 1 were used except that the filtration apparatus of Example 1 was provided with a liquid feed pump instead of the air supply means in the pipe between the membrane module and the calling tank. Then, the filtration ability was confirmed. As a result, about 40 minutes after the start of filtration, and when the total volume of the filtrate reached 10 L, Example 1
Since the filtration flux was reduced to about 1/4 as compared with, the operation was stopped. The cause of the decrease in the filtration flux was that the membrane module was subjected to an internal pressure of 30 KPa or more, and the contaminated layer was compressed and densified on the surface of the membrane, which is peculiar to the conventional cross-flow pressure filtration treatment, and the filtration resistance increased. it is conceivable that. FIG. 4 shows the results of comparing the filtration fluxes of Example 1 and Comparative Example 2.
【００１３】［実施例２、比較例３］実施例２として、
実施例１と同様の装置、運転条件で、また比較例３とし
て、比較例１と同様の装置、運転条件で運転を行ない、
被処理液の循環流の流れを観察した。実施例２の本発明
装置の場合、エアーリフト液循環流は脈流であった。一
方、比較例３の従来のクロスフロー加圧濾過装置の場合
は一定流であり、その流れ方の違いによる液線速度値を
比較した結果を表１に示す。表１から明らかなように、
従来クロスフロー加圧装置の液線速度は１ｍ／ｓｅｃ近
辺に対し、本発明の装置は、瞬間的にだが３倍近い非常
に高い液線速度を示す。Example 2, Comparative Example 3 As Example 2,
Operation was performed under the same apparatus and operating conditions as in Example 1, and as Comparative Example 3 under the same apparatus and operating conditions as in Comparative Example 1,
The circulation flow of the liquid to be treated was observed. In the case of the device of the present invention of Example 2, the air lift liquid circulating flow was a pulsating flow. On the other hand, in the case of the conventional cross-flow pressure filtration device of Comparative Example 3, the flow rate is constant, and the results of comparing the liquid linear velocity values due to the difference in the flow method are shown in Table 1. As is clear from Table 1,
The liquid linear velocity of the conventional cross-flow pressurizing device is in the vicinity of 1 m / sec, whereas the device of the present invention instantaneously shows a very high liquid linear velocity of nearly 3 times.
【００１４】［実施例３、比較例４］実施例３として、
実施例１と同様の装置、運転条件で、また比較例４とし
て、比較例１と同様の装置、運転条件で運転を行ない、
ポンプの消費電力を計測した。本発明装置と、従来のク
ロスフロー加圧濾過装置とのそれぞれのポンプ消費電力
値を表２に示す。表２から明らかなように、本発明装置
のポンプ消費電力は、従来クロスフロー加圧装置対比約
９０％低減であり、非常に優れた省エネ装置である。[Example 3 and Comparative Example 4] As Example 3,
Operation was performed under the same apparatus and operating conditions as in Example 1, and as Comparative Example 4 under the same apparatus and operating conditions as in Comparative Example 1,
The power consumption of the pump was measured. Table 2 shows the pump power consumption values of the device of the present invention and the conventional cross-flow pressure filtration device. As is clear from Table 2, the pump power consumption of the device of the present invention is about 90% lower than that of the conventional cross-flow pressurizing device, which is a very excellent energy-saving device.
【００１５】[0015]
【表１】 [Table 1]
【００１６】[0016]
【表２】 [Table 2]
【００１７】[0017]
【発明の効果】本発明のエアーリフト濾過装置及び濾過
方法は、大きな循環・濾過ポンプを使用しないため、膜
表面の汚染層の圧縮、緻密化現象が起き難くなる。ま
た、小さい液循環量でも瞬間的な液線速度を２．５〜
３．５ｍ／ｓｅｃと大きくすることができ、液線速度が
従来型対比約２．５〜３．５倍の大きな流れの汚染層除
去力が得られる。この両者の働きから高い濾過流束が維
持され、ついては、濾過所要時間の短縮となる。さら
に、本発明装置は大きな循環・濾過ポンプを使用しない
事と、前記の濾過所要時間の短縮からランニングコスト
の電気代を安くでき、省エネ的にも優れたものである。EFFECTS OF THE INVENTION Since the air-lift filtration device and filtration method of the present invention do not use a large circulation / filtration pump, the phenomenon of compression and densification of the contaminated layer on the membrane surface is less likely to occur. Even with a small amount of liquid circulation, the instantaneous liquid velocity is 2.5-
It can be increased to 3.5 m / sec, and a large flow contaminated layer removing force with a liquid linear velocity of about 2.5 to 3.5 times that of the conventional type can be obtained. A high filtration flux is maintained by the functions of both of them, and the time required for filtration is shortened. Furthermore, the device of the present invention is excellent in terms of energy saving, because it does not use a large circulation / filtration pump, and because the time required for filtration is shortened, the running cost of electricity can be reduced.
【図１】本発明の濾過装置概略図である。FIG. 1 is a schematic view of a filtration device of the present invention.
【図２】従来のクロスフロー加圧濾過装置概略図であ
る。FIG. 2 is a schematic view of a conventional cross-flow pressure filtration device.
【図３】実施例と比較例１の濾過能力比較図ある。FIG. 3 is a comparison diagram of filtration capacities of Example and Comparative Example 1.
【図４】実施例と比較例２の濾過能力比較図である。FIG. 4 is a comparison diagram of filtration capacities of Example and Comparative Example 2.
【図５】本発明の液循環脈流の波形の例を示す模式図。FIG. 5 is a schematic diagram showing an example of a waveform of a liquid circulation pulsating flow of the present invention.
（１）原水タンク （２）循環・濾過ポンプ （３）呼出槽 （４）膜モジュール （５）エアーポンプ （６）濾過水／逆洗ポンプ（本発明装置） （７）逆洗ポンプ（従来加圧濾過装置） （８）濾過水受けタンク (1) Raw water tank (2) Circulation / filtration pump (3) Calling tank (4) Membrane module (5) Air pump (6) Filtered water / backwash pump (device of the present invention) (7) Backwash pump (conventional pressure filtration device) (8) Filtered water receiving tank
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.7 識別記号 ＦＩ テーマコート゛(参考） Ｂ０１Ｄ 63/10 Ｂ０１Ｄ 63/10 65/02 65/02 ５２０ ５２０ Ｆターム(参考） 4D006 GA06 GA07 HA04 HA21 HA61 JA53A JA58A JA63A KA42 KC03 KC13 KE21Q KE22Q MA01 MA02 MA04 MB02 PA01 PB02 PB22 PC51 ─────────────────────────────────────────────────── ─── Continuation of front page (51) Int.Cl. 7 Identification code FI theme code (reference) B01D 63/10 B01D 63/10 65/02 65/02 520 520 F term (reference) 4D006 GA06 GA07 HA04 HA21 HA61 JA53A JA58A JA63A KA42 KC03 KC13 KE21Q KE22Q MA01 MA02 MA04 MB02 PA01 PB02 PB22 PC51
Claims (5)
らの下部を連結させた配管、膜モジュールからの被処理
水を呼出槽に戻す配管、エアーリフト用エアー供給手段
および濾過水ポンプで構成される濾水装置。1. A filter comprising at least a membrane module, a calling tank, piping connecting these lower parts, piping for returning treated water from the membrane module to the calling tank, air supply means for air lift, and filtered water pump. Water equipment.
ラル型の精密濾過膜または限外濾過膜を用いた膜モジュ
ールを特徴とする請求項１記載の濾過装置。2. The filtration device according to claim 1, which is a membrane module using a hollow fiber type, tubular type or spiral type microfiltration membrane or ultrafiltration membrane.
により逆圧洗浄用としても使用する事を特徴とする請求
項１または２記載の濾過装置。3. The filtration apparatus according to claim 1, wherein the filtration water pump is also used for back pressure cleaning by switching a valve.
せた配管にエアーを導入し、膜モジュール内にエアーリ
フトを発生させて、被処理水を呼出槽から膜モジュール
内に吸い込み、膜モジュール上部から被処理水を再び呼
出槽に排出する液循環を行うことを特徴とする濾過方
法。4. Air is introduced into a pipe connecting the lower part of the membrane module and the lower part of the calling tank to generate an air lift in the membrane module so that the water to be treated is sucked from the calling tank into the membrane module and the upper part of the membrane module. A method for filtering, characterized in that a liquid is circulated so that the water to be treated is discharged again to the calling tank.
上部と同等の高さになるように運転することを特徴とす
る請求項４記載の濾過方法。5. The filtration method according to claim 4, wherein the liquid level in the calling tank is constantly operated so as to be at the same height as the upper part of the membrane module.
Priority Applications (1)
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|---|---|---|---|
| JP2002028656A JP2003225661A (en) | 2002-02-05 | 2002-02-05 | Cross flow type filtration apparatus and filtration method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2002028656A JP2003225661A (en) | 2002-02-05 | 2002-02-05 | Cross flow type filtration apparatus and filtration method |
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| Publication Number | Publication Date |
|---|---|
| JP2003225661A true JP2003225661A (en) | 2003-08-12 |
Family
ID=27749765
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2002028656A Pending JP2003225661A (en) | 2002-02-05 | 2002-02-05 | Cross flow type filtration apparatus and filtration method |
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| Country | Link |
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| JP (1) | JP2003225661A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9873088B2 (en) | 2011-05-17 | 2018-01-23 | Natrix Separations Inc. | Layered tubular membranes for chromatography, and methods of use thereof |
| JP2018103119A (en) * | 2016-12-27 | 2018-07-05 | オルガノ株式会社 | Method and apparatus for treating water containing polysaccharide thickener |
| US10800808B2 (en) | 2008-09-02 | 2020-10-13 | Merck Millipore Ltd. | Chromatography membranes, devices containing them, and methods of use thereof |
-
2002
- 2002-02-05 JP JP2002028656A patent/JP2003225661A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US10800808B2 (en) | 2008-09-02 | 2020-10-13 | Merck Millipore Ltd. | Chromatography membranes, devices containing them, and methods of use thereof |
| US10981949B2 (en) | 2008-09-02 | 2021-04-20 | Merck Millipore Ltd. | Chromatography membranes, devices containing them, and methods of use thereof |
| US11884701B2 (en) | 2008-09-02 | 2024-01-30 | Merck Millipore Ltd. | Chromatography membranes, devices containing them, and methods of use thereof |
| US9873088B2 (en) | 2011-05-17 | 2018-01-23 | Natrix Separations Inc. | Layered tubular membranes for chromatography, and methods of use thereof |
| US10195567B2 (en) | 2011-05-17 | 2019-02-05 | Natrix Separations Inc. | Layered tubular membranes for chromatography, and methods of use thereof |
| US10874990B2 (en) | 2011-05-17 | 2020-12-29 | Merck Millipore Ltd. | Layered tubular membranes for chromatography, and methods of use thereof |
| JP2018103119A (en) * | 2016-12-27 | 2018-07-05 | オルガノ株式会社 | Method and apparatus for treating water containing polysaccharide thickener |
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