JP5743095B2 - Membrane separation activated sludge equipment - Google Patents

Membrane separation activated sludge equipment Download PDF

Info

Publication number
JP5743095B2
JP5743095B2 JP2011246509A JP2011246509A JP5743095B2 JP 5743095 B2 JP5743095 B2 JP 5743095B2 JP 2011246509 A JP2011246509 A JP 2011246509A JP 2011246509 A JP2011246509 A JP 2011246509A JP 5743095 B2 JP5743095 B2 JP 5743095B2
Authority
JP
Japan
Prior art keywords
membrane
activated sludge
water
water flow
membrane separation
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
Application number
JP2011246509A
Other languages
Japanese (ja)
Other versions
JP2012176396A (en
Inventor
洋平 冨田
洋平 冨田
渕上 浩司
浩司 渕上
辻 猛志
猛志 辻
秀明 野間
秀明 野間
山本 勝一郎
勝一郎 山本
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
JFE Engineering Corp
Original Assignee
JFE Engineering Corp
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by JFE Engineering Corp filed Critical JFE Engineering Corp
Priority to JP2011246509A priority Critical patent/JP5743095B2/en
Publication of JP2012176396A publication Critical patent/JP2012176396A/en
Application granted granted Critical
Publication of JP5743095B2 publication Critical patent/JP5743095B2/en
Expired - Fee Related legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02WCLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00Technologies for wastewater treatment
    • Y02W10/10Biological treatment of water, waste water, or sewage

Description

本発明は、下水や工場排水の処理に用いられる膜分離活性汚泥装置に関する。   The present invention relates to a membrane separation activated sludge apparatus used for treatment of sewage and factory waste water.

活性汚泥装置は種々のものが知られているが、そのなかに、活性汚泥処理槽内に膜分離装置を備えたものがある(例えば、特許文献1)。これは、活性汚泥処理を行いながら処理水を膜で分離して抜き出すものであり、例えば、図7に示すように、活性汚泥処理槽1に膜分離装置2と、散気装置3、3‘を設けて、この散気によって、活性汚泥菌への酸素の供給と気泡による膜面の洗浄を行っている。   Various types of activated sludge apparatuses are known. Among them, there is an activated sludge treatment tank equipped with a membrane separation device (for example, Patent Document 1). This is to separate and extract the treated water with a membrane while performing the activated sludge treatment. For example, as shown in FIG. 7, the activated sludge treatment tank 1 has a membrane separation device 2 and aeration devices 3, 3 ′. The air is supplied with oxygen to the activated sludge bacteria and the membrane surface is cleaned with bubbles.

特開2004−337787号公報JP 2004-337787 A

通常、膜の洗浄は、常時膜の直下よりスクラビング(散気)して行っており、洗浄効果を高めるために粗大気泡(気泡径1〜10mm)が専ら用いられる。散気は、膜の洗浄のほかに活性汚泥への酸素供給を目的としているが、酸素溶解効率が、微細気泡による散気の場合20%程度であるのに比べて、粗大気泡の場合は10%程度と低い。よって、多くの場合には膜洗浄に必要なスクラビングだけでは活性汚泥の酸素供給をまかなうことができず、別途微細気泡による散気を行っており、ブロワの電力消費量が多くなる。通常、膜分離活性汚泥法の電力消費量は0.8kWh/m程度であり、標準活性汚泥法の値に比べてきわめて大きく運転費がかさむ。 Usually, the membrane is always scrubbed (diffused) from directly below the membrane, and coarse bubbles (bubble diameter 1 to 10 mm) are exclusively used to enhance the cleaning effect. Aeration is aimed at supplying oxygen to activated sludge in addition to cleaning the membrane, but the oxygen dissolution efficiency is about 10% in the case of coarse bubbles compared to 20% in the case of aeration with fine bubbles. As low as about%. Therefore, in many cases, the scrubbing required for membrane cleaning alone cannot supply the oxygen of the activated sludge, and aeration with fine bubbles is performed separately, which increases the power consumption of the blower. Usually, the power consumption of the membrane separation activated sludge method is about 0.8 kWh / m 3 , and the operation cost is very large compared to the value of the standard activated sludge method.

本発明の目的は、膜の洗浄と酸素供給を効率よく行って、電力消費量を節減できる膜分離活性汚泥装置を提供することにある。   An object of the present invention is to provide a membrane separation activated sludge apparatus that can efficiently clean the membrane and supply oxygen to reduce power consumption.

本発明は、上記課題を解決するべくなされたものであり、機械力を用いて水流を形成し、これを膜面に当てることによって、微細気泡を用いながら膜面を効率よく洗浄できるようにして、このような目的を達成したものである。   The present invention has been made to solve the above-mentioned problems, and by forming a water flow using mechanical force and applying it to the membrane surface, the membrane surface can be efficiently cleaned using fine bubbles. This has been achieved.

すなわち、本発明は、活性汚泥処理槽内に、浸透型膜分離装置と、活性汚泥への酸素供給と前記膜分離装置の膜の洗浄を兼ねた散気装置と、前記膜の面に向けた水流を形成する水流形成装置を備えた膜分離活性汚泥装置を提供するものである。   That is, the present invention is directed to the surface of the membrane, in the activated sludge treatment tank, an osmotic membrane separation device, an aeration device that serves to supply oxygen to the activated sludge and clean the membrane of the membrane separation device, and A membrane separation activated sludge apparatus provided with a water flow forming device for forming a water flow is provided.

本発明者らは、上記装置において、膜モジュールにおける水流速が0.1〜1.0m/sであることが好ましく、また、この流速を低動力で発生させるために、機械力として旋回機構付プロペラ式水中攪拌機又は水流ポンプの使用が有効であることも見出した。また、膜分離装置を複数の膜ユニットとして、それぞれに短時間水流を供給するだけでも充分な膜洗浄効果が得られることを見出した。さらに散気を間欠的に行うことによって膜表面のせん断力を増大させ、膜の洗浄効果を高めることができることも見出した。   In the above apparatus, the inventors of the present invention preferably have a water flow rate of 0.1 to 1.0 m / s in the membrane module, and in order to generate this flow rate with low power, a turning mechanism is attached as a mechanical force. It has also been found that the use of a propeller-type underwater stirrer or water pump is effective. Further, it has been found that a sufficient membrane cleaning effect can be obtained by simply using a membrane separator as a plurality of membrane units and supplying a water flow for a short time to each of them. Furthermore, it has been found that by intermittently performing aeration, the shearing force on the film surface can be increased and the cleaning effect of the film can be enhanced.

従って、本発明は、上記装置において、水流形成装置が旋回機構付プロペラ式水中攪拌機である装置、水流形成装置が水流ポンプである装置、これらの水流形成装置によって形成される水流速が膜モジュール内において0.1〜1.0m/sである装置、および散気装置が間欠運転可能である装置をも提供するものである。   Therefore, the present invention provides a device in which the water flow forming device is a propeller type underwater agitator with a swivel mechanism, the water flow forming device is a water flow pump, and the water flow rate formed by these water flow forming devices is within the membrane module. The apparatus which is 0.1-1.0 m / s in this invention, and the apparatus in which the diffuser can intermittently operate are also provided.

本発明は、また、水流ポンプを用いた上記装置において、浸透型膜分離装置が複数の膜ユニットからなり、かつ、前記膜ユニットが、各々の下部に散気装置と上向きの水流吐出口を備え、水流ポンプより前記水流吐出口への水供給配管に各膜ユニット毎の自動開閉弁が設けられ、1または複数の水流吐出口毎に順次切替えて水供給を可能とされている装置をも提供するものである。   The present invention is also the above apparatus using a water flow pump, wherein the osmotic membrane separation device comprises a plurality of membrane units, and each of the membrane units includes a diffuser and an upward water flow outlet at the lower part thereof. In addition, an automatic opening / closing valve for each membrane unit is provided in the water supply pipe from the water flow pump to the water flow discharge port, and a device is provided that can supply water by sequentially switching to one or a plurality of water flow discharge ports. To do.

本発明により、電力消費量を大きく節減して、活性汚泥処理コストを低下させることができる。   According to the present invention, the power consumption can be greatly reduced and the activated sludge treatment cost can be reduced.

本発明の装置の一例の概略構成を示す側面断面図である。It is side surface sectional drawing which shows schematic structure of an example of the apparatus of this invention. 本発明の装置の別の例の概略構成を示す側面断面図である。It is side surface sectional drawing which shows schematic structure of another example of the apparatus of this invention. 本発明の装置のさらに別の例の概略構成を示す側面断面図である。It is side surface sectional drawing which shows schematic structure of another example of the apparatus of this invention. 図3の装置を平面で示した図である。It is the figure which showed the apparatus of FIG. 3 by the plane. 膜面を洗浄できる流速を測定した装置の構成を示す図である。It is a figure which shows the structure of the apparatus which measured the flow rate which can wash | clean a membrane surface. 図5の装置で測定した膜間差圧の経時変化を示すグラフである。It is a graph which shows the time-dependent change of the transmembrane differential pressure measured with the apparatus of FIG. 従来の装置の概略構成を示す側面断面図である。It is side surface sectional drawing which shows schematic structure of the conventional apparatus.

本発明の装置の本体である活性汚泥処理槽は、活性汚泥を収容して水処理を行なわせる槽であり、形状は、円筒形等種々の形態をとりうるが、通常は箱型である。   The activated sludge treatment tank, which is the main body of the apparatus of the present invention, is a tank that contains activated sludge and performs water treatment. The shape can take various forms such as a cylindrical shape, but is usually a box shape.

この活性汚泥処理槽内には膜分離装置を設ける。膜は、活性汚泥と処理水を分離するもので、膜の孔径に関しては精密濾過膜あるいは限外濾過膜を適用することができる。膜の形状は、平膜タイプ、中空糸タイプ、チューブラータイプ等を用いることができ、膜の透過流束と処理水量を基に適切な面積の膜を設置する。膜の配置は、通常は水流および気泡流を妨げないように互いに平行とする。   A membrane separation device is provided in the activated sludge treatment tank. The membrane separates activated sludge and treated water, and a microfiltration membrane or an ultrafiltration membrane can be applied for the pore size of the membrane. As the shape of the membrane, a flat membrane type, a hollow fiber type, a tubular type or the like can be used, and a membrane having an appropriate area is installed based on the permeation flux of the membrane and the amount of treated water. The arrangement of the membranes is usually parallel to each other so as not to disturb the water flow and bubble flow.

散気装置は、気泡を噴出させて、活性汚泥への酸素供給と膜分離装置の膜の洗浄を行うものである。構造は、基本的に通常の散気装置と同様でよく、箱や管などの形をしたマニホールドに多数の空気噴出口を設けたものである。空気噴出口は、微細孔でよく、ノズルを取付けてもよい。空気噴出口の口径は、酸素溶解効率を高くするために微細気泡を形成するように定められ、気泡の径は0.5〜4mm程度、特に0.5〜1.0mm程度とするのがよい。気泡径が過大では十分な酸素溶解効率が得られず、過小では散気装置の圧力損失が高く、安定した運転を行うことが困難である。0.5〜1.0mmの気泡径であれば、30〜40%の酸素溶解効率が得られるため、好適である。この気泡径では気泡による膜洗浄効果は十分には得られないが、後述する水流による洗浄を併用するため、膜の運転には特に支障は無い。   The air diffuser ejects bubbles to supply oxygen to the activated sludge and clean the membrane of the membrane separation device. The structure may be basically the same as that of a normal air diffuser, and a large number of air jets are provided in a manifold having a shape such as a box or a tube. The air outlet may be a fine hole, and a nozzle may be attached. The diameter of the air outlet is determined so as to form fine bubbles in order to increase the oxygen dissolution efficiency, and the diameter of the bubbles should be about 0.5 to 4 mm, particularly about 0.5 to 1.0 mm. . If the bubble diameter is too large, sufficient oxygen dissolution efficiency cannot be obtained, and if it is too small, the pressure loss of the air diffuser is high and it is difficult to perform stable operation. A bubble diameter of 0.5 to 1.0 mm is preferable because an oxygen dissolution efficiency of 30 to 40% can be obtained. With this bubble diameter, the membrane cleaning effect due to the bubbles cannot be obtained sufficiently, but there is no particular problem in the operation of the membrane because cleaning with a water flow described later is also used.

散気風量に関しては、粗大気泡と微細気泡を散気する既存方式では、膜の洗浄に必要な粗大気泡の風量が、膜投影面積から決定され、その際の酸素溶解効率から算出される酸素供給量と活性汚泥の必要酸素量との差分から、微細気泡の風量が決定される。本発明の方式では、微細気泡だけを用いて散気を行うが、その風量は活性汚泥の必要酸素量から決定される。ただし、微細気泡だけでは膜洗浄に必要なせん断力が得られないために、別途機械攪拌力による水流を与え、膜洗浄に必要なせん断力を確保する。   With regard to the amount of diffused air, in the existing method that diffuses coarse bubbles and fine bubbles, the amount of coarse bubbles required to clean the membrane is determined from the projected area of the membrane, and the oxygen supply calculated from the oxygen dissolution efficiency at that time The air volume of the fine bubbles is determined from the difference between the amount and the required oxygen amount of the activated sludge. In the system of the present invention, air is diffused using only fine bubbles, but the air volume is determined from the required oxygen amount of the activated sludge. However, since the shear force necessary for the membrane cleaning cannot be obtained with only the fine bubbles, a water flow is additionally provided by a mechanical stirring force to ensure the shear force necessary for the membrane cleaning.

また、一定流ではなく流速に変化をつけることが洗浄効果の観点から好ましく、散気を間欠流とすることによってこの効果が得られる。間欠流とする機構については、エアライン電磁弁のタイマーによる開閉制御が考えられるが、別途エアラインに蓄気室を設け、蓄気室の吐出口が一定圧力以上で開放するような機構とすることによっても、簡易に実現することができる。開放間隔は1〜30回/分程度、好ましくは、5〜15回/分程度とするのがよい。開放間隔が過小では膜の目詰まりが進行する。   In addition, it is preferable to change the flow rate instead of a constant flow from the viewpoint of the cleaning effect, and this effect can be obtained by making the aeration intermittent. The intermittent flow mechanism can be controlled by an airline solenoid valve timer. However, a separate air storage chamber is provided in the airline, and the discharge port of the air storage chamber opens at a certain pressure or higher. This can be realized easily. The opening interval is about 1 to 30 times / minute, preferably about 5 to 15 times / minute. If the opening interval is too small, clogging of the membrane proceeds.

水流形成装置は、機械力によって水流を形成するものであり、攪拌機や水中ポンプを設置する方法があるが、旋回機構付プロペラ式水中攪拌機を用いると、攪拌機が旋回するため、膜の全面に均等に水流を当てることができるため好適である。膜面部の流速を0.1m/s以上とすることによって、洗浄効果が得られるが、好ましくは0.2〜0.5m/sである。   A water flow forming device forms a water flow by mechanical force, and there is a method of installing a stirrer and a submersible pump. However, when a propeller type submerged stirrer with a swivel mechanism is used, the stirrer swirls, so the entire surface of the membrane is even. It is preferable because a water stream can be applied thereto. Although the cleaning effect can be obtained by setting the flow rate of the film surface portion to 0.1 m / s or more, it is preferably 0.2 to 0.5 m / s.

膜面を洗浄できる流速を調べた装置の構成を図5に示す。この装置は、1本の中空糸を透明塩ビ筒内に筒長方向に設置した膜分離装置と、活性汚泥槽からなり、活性汚泥槽の底部からは透明塩ビ筒の下部へ液を送るチューブが接続され、透明塩ビ筒の上部からは活性汚泥層の上面に液を戻すチューブが接続されて、活性汚泥槽内液の循環ラインが形成されている。この循環ラインの途中には循環ポンプ、圧力計、流量計および流量調整弁が設けられている。中空系の下部は、透明塩ビ筒の下端を突き抜けており、そこには吸引ポンプと圧力計が取り付けられている。中空系の下端の下には中空糸で濾過された液を受けるビーカが配置されている。この装置を用いて流速を0.25m/s、0.4m/s、0.55m/sに変えて膜間差圧の経時変化を調べた結果を図6に示す。同図に示すように、流速が0.25m/sと0.4m/sでは膜間差圧が時間と共に上昇して目詰まりを生じているが、流速が0.55m/sでは膜間差圧がほぼ一定で充分に洗浄が行われていることを示している。その結果、膜面を流れる流速が0.5m/s以上であれば充分に洗浄効果があることがわかった。   FIG. 5 shows the configuration of an apparatus for examining the flow rate at which the membrane surface can be cleaned. This device consists of a membrane separation device in which one hollow fiber is installed in a transparent PVC cylinder in the cylinder length direction and an activated sludge tank, and a tube for sending liquid from the bottom of the activated sludge tank to the lower part of the transparent PVC cylinder A tube for returning the liquid to the upper surface of the activated sludge layer is connected from the upper part of the transparent PVC cylinder, and a circulation line for the liquid in the activated sludge tank is formed. A circulation pump, a pressure gauge, a flow meter, and a flow rate adjusting valve are provided in the middle of the circulation line. The lower part of the hollow system penetrates the lower end of the transparent PVC cylinder, and a suction pump and a pressure gauge are attached to the lower part. A beaker for receiving the liquid filtered with the hollow fiber is disposed under the lower end of the hollow system. FIG. 6 shows the results of examining the time-dependent change in transmembrane pressure difference by changing the flow rate to 0.25 m / s, 0.4 m / s, and 0.55 m / s using this apparatus. As shown in the figure, when the flow rate is 0.25 m / s and 0.4 m / s, the transmembrane pressure difference increases with time, resulting in clogging. However, when the flow rate is 0.55 m / s, the transmembrane difference It shows that the pressure is almost constant and washing is performed sufficiently. As a result, it was found that if the flow velocity flowing on the membrane surface was 0.5 m / s or more, there was a sufficient cleaning effect.

水流を膜面に当てる角度はできるだけ浅いことが好ましく、0〜45度程度が適当である。活性汚泥処理槽に垂直に配置した膜において、槽全体に旋回流を生じさせると、効率的に膜面に平行な水流を生じることができる。   The angle at which the water flow is applied to the membrane surface is preferably as shallow as possible, and about 0 to 45 degrees is appropriate. When a swirl flow is generated in the entire tank in the membrane disposed vertically in the activated sludge treatment tank, a water flow parallel to the film surface can be efficiently generated.

水流形成装置として、水流ポンプも本発明の装置に有効である。水流ポンプは、水流を膜面に当てることによって微細気泡を用いながら膜面を効率よく洗浄するものであり、水流の吐出口は膜の下部から垂直に上向きとして膜面と平行な水流を形成するようにすることが好ましい。全ての膜の下から水流を吐出させるようにすれば、部分的に水流の弱いところがなくなり、膜全体を効率よく水流洗浄することができる。この水流ポンプは、活性汚泥も強制的に槽内循環させる作用も発揮する。水流ポンプの位置は槽内外を問わない。   As a water flow forming device, a water flow pump is also effective for the device of the present invention. The water flow pump is a device that efficiently cleans the membrane surface while applying fine air bubbles by applying the water flow to the membrane surface. The water flow outlet is vertically upward from the bottom of the membrane to form a water flow parallel to the membrane surface. It is preferable to do so. If the water flow is discharged from under all the membranes, there is no part where the water flow is weak, and the entire membrane can be efficiently washed with water. This water pump also exerts an action of forcibly circulating activated sludge in the tank. The position of the water pump does not matter inside or outside the tank.

また、ポンプにタイマーを接続して水流ポンプの作動をコントロールできるようにすることができる。例えば、膜からの処理水の吸引を一定時間毎に停止させて、その停止期間中に水流ポンプを作動させて効率よく水流洗浄を行うこともできる。このタイムスケジュールは適宜定めることができるが、例えば、処理水の吸引を5〜60分行って30秒〜5分間吸引を停止し、その間に水流ポンプを作動させて水流洗浄を行う。   In addition, a timer can be connected to the pump so that the operation of the water pump can be controlled. For example, the suction of treated water from the membrane can be stopped at regular intervals, and the water flow can be efficiently washed by operating the water flow pump during the stop period. The time schedule can be determined as appropriate. For example, the suction of the treated water is performed for 5 to 60 minutes, the suction is stopped for 30 seconds to 5 minutes, and the water flow pump is operated during that time to perform water flow cleaning.

本発明の装置においては、一つの膜分離装置を1ユニットとして複数の膜ユニットを設けることができる。そして、各膜ユニットの下部に散気装置と上向きの水流吐出口を設け、水流ポンプより前記水流吐出口への水供給配管に各膜ユニット毎の自動開閉弁を、1または複数の水流吐出口毎に順次切り替えて水を供給できるようにする。これは、本発明者が、膜面の洗浄は、洗浄の全時間水流を流す必要はなく、短時間の水流供給を間欠的に行なっても充分な膜面洗浄を達成できることを見出したことによるものである。各膜分離装置毎に適切な運転条件が異なるので実験でこれを求めるのがよい。適切な運転条件は膜面差圧の経時変化を調べることで設定でき、電力費などの運転コストも考慮して定める。一般的には水流を長時間にわたって停止するのは好ましくなく、水流の停止時間は30秒〜5分間程度とし、それに対して各膜ユニット毎の適切な水流供給時間を定めるのがよい。   In the apparatus of the present invention, a plurality of membrane units can be provided with one membrane separator as one unit. An air diffuser and an upward water flow outlet are provided at the lower part of each membrane unit, and an automatic on-off valve for each membrane unit is provided in the water supply pipe from the water flow pump to the water flow outlet. It is possible to supply water by sequentially switching every time. This is because the present inventor found that it is not necessary to flow the water flow for the entire cleaning time, and sufficient film surface cleaning can be achieved even if intermittent supply of water flow is performed for a short time. Is. Since appropriate operating conditions differ for each membrane separation device, it is preferable to obtain this through experiments. Appropriate operating conditions can be set by investigating changes over time in the differential pressure on the membrane surface, and are determined in consideration of operating costs such as power costs. In general, it is not preferable to stop the water flow for a long time. The stop time of the water flow is about 30 seconds to 5 minutes, and an appropriate water flow supply time for each membrane unit should be determined.

こうして定めた1回の水流供給時間で各膜ユニットに順次水流を供給し、全膜ユニットについて水流供給が終了する時間を1サイクルとし、吸引ポンプの停止時間中に1〜5サイクル程度の水流洗浄を実施する。   The water flow is sequentially supplied to each membrane unit in the single water flow supply time determined in this way, and the time for completing the water flow supply for all the membrane units is defined as one cycle, and the water flow cleaning is performed for about 1 to 5 cycles during the suction pump stop time. To implement.

この方式により、1台のポンプで複数の膜ユニットの洗浄を担当させることができ、電力をさらに節減することができる。   By this method, it is possible to perform cleaning of a plurality of membrane units with one pump, and it is possible to further reduce power.

活性汚泥処理槽には、その外、溶存酸素濃度計、pH計、温度計などが適宜設けられる。   In addition, the activated sludge treatment tank is appropriately provided with a dissolved oxygen concentration meter, a pH meter, a thermometer, and the like.

本発明の一実施態様である膜分離活性汚泥装置の概略構成を図1に示す。   A schematic configuration of a membrane separation activated sludge apparatus according to an embodiment of the present invention is shown in FIG.

この装置の活性汚泥処理槽1は箱型で、内部は邪魔板6で2つの領域に区分され、その一方に膜分離装置2散気装置3が、そして他方には水流形成装置4が設置されている。 The activated sludge treatment tank 1 of this apparatus is a box type, and the inside is divided into two regions by a baffle plate 6, one of which is a membrane separation device 2 and an air diffuser 3 , and the other is a water flow forming device 4. Has been.

膜分離装置2は中空糸タイプの膜を垂直に多数配置したもので、上下端が集水部に接続されており、吸引ポンプ8によってろ液を得られる。膜の孔径は0.01〜1μm程度の範囲である場合が多く、特に0.02〜0.5μmの範囲にあるものが清澄な処理水質が得られて経済的な透過水流束が得られるために多く用いられる。   The membrane separation device 2 is a device in which a large number of hollow fiber type membranes are arranged vertically. The upper and lower ends are connected to a water collecting section, and a filtrate can be obtained by a suction pump 8. In many cases, the pore diameter of the membrane is in the range of about 0.01 to 1 μm, and particularly in the range of 0.02 to 0.5 μm, a clear treated water quality is obtained and an economical permeate flux is obtained. Often used in

散気装置3は、平板や直管形状であり、表面はゴムや金属板、あるいはセラミック焼結体等で構成され、気泡放出用の細孔が多数形成されている。この細孔から放出される気泡は散気面直上部で径が1.5mm程度である。各直管は連結管で連結され、槽外のブロワ5に接続されている。   The air diffuser 3 has a flat plate or straight pipe shape, and the surface is made of rubber, a metal plate, a ceramic sintered body, or the like, and a large number of pores for releasing bubbles are formed. The bubbles released from the pores have a diameter of about 1.5 mm immediately above the diffuser surface. Each straight pipe is connected by a connecting pipe and connected to the blower 5 outside the tank.

水流形成装置4は、旋回機構付プロペラ式水中攪拌機が用いられている。この攪拌機は処理槽の上方に設置された駆動装置の動力を槽下部に設置されたプロペラに伝達する軸の回転に伴い、プロペラが左右に旋回する機構を備えた攪拌機である。この攪拌機によって形成される水流が活性汚泥処理槽内で旋回流を形成するとともに、膜設置部では上昇流となるように、処理槽1の膜分離装置と反対側の側面下部に取付けられている。本設備構成によって、膜表面の上向きの流速は最大値で0.4m/sとすることができた。また、本装置では散気装置の空気供給部に圧力弁を設けることによって、散気を間欠的に実施した。   The water flow forming device 4 uses a propeller type underwater stirrer with a turning mechanism. This stirrer is a stirrer provided with a mechanism in which the propeller turns left and right in accordance with the rotation of the shaft that transmits the power of the drive device installed above the treatment tank to the propeller installed at the bottom of the tank. The water flow formed by the agitator forms a swirl flow in the activated sludge treatment tank and is attached to the lower part of the side surface of the treatment tank 1 opposite to the membrane separation device so as to be an upward flow in the membrane installation section. . With this equipment configuration, the upward flow velocity on the membrane surface could be 0.4 m / s at the maximum. Moreover, in this apparatus, the aeration was intermittently implemented by providing a pressure valve in the air supply part of the aeration apparatus.

の装置で粗大気泡を散気して膜表面の汚泥を剥離しながら、下水を用いて通水実験したところ、単位処理水量当りの所要動力は0.80kWh/mであった。一方、同じ膜分離装置でありながら、本発明の装置では散気動力が0.51kWh/m、攪拌機動力が0.04kWh/mと合計で0.55kWh/mに減少させることができた。 A water flow experiment was conducted using sewage while aeration of coarse bubbles using the apparatus of FIG. 7 to remove sludge on the membrane surface. As a result, the required power per unit treated water amount was 0.80 kWh / m 3 . On the other hand, although it is the same membrane separation apparatus, in the apparatus of the present invention, the aeration power can be reduced to 0.51 kWh / m 3 and the agitator power can be reduced to 0.04 kWh / m 3 , which is 0.55 kWh / m 3 in total. It was.

本発明の別の実施態様である膜分離活性汚泥装置の概略構成を図2に示す。   FIG. 2 shows a schematic configuration of a membrane separation activated sludge apparatus which is another embodiment of the present invention.

この装置は、水流形成装置4に水流ポンプを用いた以外は実施例1と同じである。ただし、邪魔板は無いケースもある。邪魔板を設置する目的は同じで、旋回流を作ることで、膜面に対し上向流を作る、または、上向流の流速を上げることである。   This apparatus is the same as Example 1 except that a water flow pump is used for the water flow forming device 4. However, there are cases where there is no baffle. The purpose of installing the baffle plate is the same: to create a swirling flow, to create an upward flow with respect to the membrane surface, or to increase the flow velocity of the upward flow.

水流ポンプ4は活性汚泥処理槽1の槽外に取付けて、活性汚泥処理槽1の底部に引抜配管が接続され、一方、散気装置3と膜分離装置2の間には膜分離装置2の直下に水流を吹出する配管が設けられている。この配管は途中で多管に分岐され、それぞれに多数のノズルが上方に向けて垂直に膜全体を水流洗浄できるように均等に配置されている。   The water flow pump 4 is attached to the outside of the activated sludge treatment tank 1, and a drawing pipe is connected to the bottom of the activated sludge treatment tank 1, while the membrane separation apparatus 2 is connected between the air diffuser 3 and the membrane separation apparatus 2. A pipe for blowing a water flow is provided directly below. This pipe is branched into multi-tubes in the middle, and a large number of nozzles are arranged uniformly so that the whole membrane can be washed with water vertically upward.

この実施例2の水流ポンプを用いた場合と、実施例1のプロペラ攪拌機を用いた場合と、従来の散気洗浄を行った場合の、下水1mを処理するための動力を比較した結果を表1に示す。 The results of comparing the power for treating 1 m 3 of sewage when the water flow pump of Example 2 is used, when the propeller stirrer of Example 1 is used, and when performing conventional aeration cleaning are shown. Table 1 shows.

Figure 0005743095
Figure 0005743095

本発明の別の実施態様である膜分離活性汚泥装置の概略構成を図3に側面断面図で、図4に平面図で示す。   A schematic configuration of a membrane separation activated sludge apparatus as another embodiment of the present invention is shown in a side sectional view in FIG. 3 and in a plan view in FIG.

この装置は、膜ユニット2が8基配置され、各々の下部には散気装置3と上向きの水流吐出口41を有する水流形成装置4を設けられ、各散気装置3は連結されて槽外のブロワ5に接続されている。各水流形成装置4は、いずれも自動開閉弁43を介して水流洗浄ポンプに接続されている。42は水流洗浄ポンプと水流吐出口41を結ぶ水供給管である。各自動開閉弁はコンピュータ(図示されていない)によってその開閉が自動制御されている。処理される原水は原水ポンプ7によって活性汚泥処理槽1に投入されて活性汚泥処理され、処理水は吸引ポンプ8で吸引されて膜を通過して系外に出される。そして、各膜ユニット21はコンピュータの指令によって自動開閉弁43が開閉して洗浄水流の供給、停止を行う。この自動開閉弁43の開閉は、膜洗浄中は、いずれか1つのみの自動開閉弁43が開いており、水流は1基のポンプで供給されるようになっている。吸引ポンプにはタイマー44が接続されており、これにより、処理水の吸引を一定時間ごとに停止させて、その停止期間中に水流ポンプを作動させて水流洗浄を効率よく行うことができる。 The device, membrane unit 2 1 is arranged eight, the lower portion of each provided with a water jet forming device 4 having a water discharge port 41 of the upward and air diffuser 3, the air diffuser 3 is connected to the tank It is connected to an external blower 5. Each of the water flow forming devices 4 is connected to a water flow cleaning pump via an automatic opening / closing valve 43. A water supply pipe 42 connects the water washing pump and the water discharge outlet 41. The opening / closing of each automatic opening / closing valve is automatically controlled by a computer (not shown). The raw water to be treated is fed into the activated sludge treatment tank 1 by the raw water pump 7 and treated with activated sludge, and the treated water is sucked by the suction pump 8 and passes through the membrane to be discharged out of the system. In each membrane unit 21, the automatic opening / closing valve 43 is opened / closed by a command from the computer to supply and stop the cleaning water flow. As for the opening / closing of the automatic opening / closing valve 43, only one of the automatic opening / closing valves 43 is open during membrane cleaning, and the water flow is supplied by a single pump. A timer 44 is connected to the suction pump, whereby the suction of the treated water is stopped at regular intervals, and the water pump can be operated during the stop period to efficiently perform the water flow cleaning.

図5に示す装置を用い、MF膜とUF膜について、洗浄水流量と洗浄水流の供給時間と停止時間を変えて膜間差圧の変化を測定した結果を表2、表3、に示す。   Tables 2 and 3 show the results of measuring the change in transmembrane pressure difference for the MF membrane and the UF membrane using the apparatus shown in FIG. 5 while changing the cleaning water flow rate, the cleaning water flow supply time, and the stop time.

Figure 0005743095
表2の結果から、1分運転−7分停止では膜間差圧が上昇し、2分運転−6分停止の条件から徐々に膜表面にケーキが堆積して洗浄が不十分になっていたことが分かる。0.8m/分で10秒運転−50秒停止が最も好ましかった。
Figure 0005743095
From the results of Table 2, the 1-minute operation-7-minute stop showed an increase in the transmembrane pressure, and the 2-minute operation-6-minute stop condition gradually accumulated cake on the film surface, resulting in insufficient cleaning. I understand that. A 10 second run at 0.8 m 3 / min-50 second stop was most preferred.

この経験から、水流量を0.8m/分とし、運転時間を10〜30秒とし、停止時間を105〜160秒にして膜間差圧の変化を調べた結果を表3に示す。 From this experience, Table 3 shows the results of examining the change in transmembrane pressure with the water flow rate set to 0.8 m 3 / min, the operation time set to 10 to 30 seconds, and the stop time set to 105 to 160 seconds.

Figure 0005743095
この結果、15秒運転−105秒停止で膜面を洗浄でき、これにより、1台のポンプで8基の膜ユニットの洗浄を担当させることができることが分かった。
Figure 0005743095
As a result, it was found that the membrane surface could be cleaned by running for 15 seconds-stopping for 105 seconds, thereby allowing the single membrane pump to be responsible for cleaning the eight membrane units.

本発明により、活性汚泥処理に使用する電力を大幅に節減することができるので、膜分離活性汚泥処理設備に広く利用できる。   According to the present invention, since the electric power used for the activated sludge treatment can be greatly reduced, it can be widely used in membrane separation activated sludge treatment equipment.

1 活性汚泥処理槽
2 浸透型膜分離装置
21 膜ユニット
3、3‘ 散気装置
4 水流形成装置
41 水流吐出口
42 水供給管
43 自動開閉弁
44 タイマー
5、5‘ ブロワ
6 邪魔板
7 原水ポンプ
8 吸引ポンプ
DESCRIPTION OF SYMBOLS 1 Activated sludge processing tank 2 Permeation type membrane separator 21 Membrane unit 3, 3 'Air diffuser 4 Water flow forming device 41 Water flow outlet 42 Water supply pipe 43 Automatic open / close valve 44 Timer 5, 5' Blower 6 Baffle plate 7 Raw water pump 8 Suction pump

Claims (4)

活性汚泥処理槽内に、浸透型膜分離装置と、活性汚泥への酸素供給と前記膜分離装置の膜の洗浄を兼ねた散気装置と、前記膜の面に向けた水流を形成する水流形成装置を備えた膜分離活性汚泥装置であって、前記水流形成装置が、前記活性汚泥処理槽を2つの領域に区分する邪魔板を挟んで前記浸透型膜分離装置と反対側の槽側面下部に取り付けられた旋回機構付プロペラ式水中撹拌機であることを特徴とする膜分離活性汚泥装置。 In the activated sludge treatment tank, an osmotic membrane separation device, an air diffuser that also serves to supply oxygen to the activated sludge and clean the membrane of the membrane separation device, and water flow formation that forms a water flow toward the surface of the membrane A membrane separation activated sludge apparatus provided with a device , wherein the water flow forming device is disposed at a lower portion of the tank side surface opposite to the osmotic membrane separation apparatus with a baffle plate dividing the activated sludge treatment tank into two regions. A membrane separation activated sludge apparatus, which is a propeller-type underwater agitator with a swivel mechanism attached. 活性汚泥処理槽内に、浸透型膜分離装置と、活性汚泥への酸素供給と前記膜分離装置の膜の洗浄を兼ねた散気装置と、前記膜の面に向けた水流を形成する水流形成装置を備えた膜分離活性汚泥装置であって、前記浸透型膜分離装置が複数の膜ユニットからなり、前記水流形成装置が、前記膜ユニットの各々の下部に散気装置とともに設けられた上向きの水流吐出口とそれに水を送る水流ポンプであり、かつ、前記水流ポンプより前記水流吐出口への水供給配管に各膜ユニット毎の自動開閉弁が設けられ、1または複数の水流吐出口毎に順次切替えて水供給を可能とされていることを特徴とする膜分離活性汚泥装置。 In the activated sludge treatment tank, an osmotic membrane separation device, an air diffuser that also serves to supply oxygen to the activated sludge and clean the membrane of the membrane separation device, and water flow formation that forms a water flow toward the surface of the membrane A membrane separation activated sludge apparatus provided with a device, wherein the osmotic membrane separation device comprises a plurality of membrane units, and the water flow forming device is provided with an air diffuser at the lower part of each of the membrane units. a water pump sends the water discharge port and its water, and automatic opening and closing valves for each membrane unit is formed from the water pump to the water supply pipe to the water discharge port, for each of one or more water discharge ports it characterized in that it is capable of sequentially switching and water supply membrane bioreactor device. 前記散気装置と前記水流形成装置によって形成される水の流速が膜モジュール内において0.1〜1.0m/sであること特徴とする請求項1または請求項2のいずれかに記載の膜分離活性汚泥装置。 The membrane according to any one of claims 1 and 2 , wherein a flow rate of water formed by the air diffuser and the water flow forming device is 0.1 to 1.0 m / s in the membrane module. Separation activated sludge equipment. 前記散気装置が間欠運転であることを特徴とする請求項1乃至請求項のいずれか1項に記載の膜分離活性汚泥装置。 The membrane separation activated sludge device according to any one of claims 1 to 3 , wherein the air diffuser is operated intermittently.
JP2011246509A 2010-11-30 2011-11-10 Membrane separation activated sludge equipment Expired - Fee Related JP5743095B2 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP2011246509A JP5743095B2 (en) 2010-11-30 2011-11-10 Membrane separation activated sludge equipment

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
JP2010266280 2010-11-30
JP2010266280 2010-11-30
JP2011017425 2011-01-31
JP2011017425 2011-01-31
JP2011246509A JP5743095B2 (en) 2010-11-30 2011-11-10 Membrane separation activated sludge equipment

Publications (2)

Publication Number Publication Date
JP2012176396A JP2012176396A (en) 2012-09-13
JP5743095B2 true JP5743095B2 (en) 2015-07-01

Family

ID=46978644

Family Applications (1)

Application Number Title Priority Date Filing Date
JP2011246509A Expired - Fee Related JP5743095B2 (en) 2010-11-30 2011-11-10 Membrane separation activated sludge equipment

Country Status (1)

Country Link
JP (1) JP5743095B2 (en)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2014231033A (en) * 2013-05-28 2014-12-11 株式会社日立製作所 Cleaning method of membrane surface in flat membrane type membrane separation device and flat membrane type membrane separation device
JP6425067B2 (en) * 2014-09-16 2018-11-21 Jfeエンジニアリング株式会社 Membrane separation activated sludge treatment system
HUE059189T2 (en) 2014-10-22 2022-10-28 Koch Separation Solutions Inc Membrane module system with bundle enclosures and pulsed aeration
USD779631S1 (en) 2015-08-10 2017-02-21 Koch Membrane Systems, Inc. Gasification device

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH04110090A (en) * 1990-08-30 1992-04-10 Kubota Corp Activated-sludge treating device
JPH04247288A (en) * 1991-01-31 1992-09-03 Kubota Corp Water treating apparatus
JP3480049B2 (en) * 1994-07-14 2003-12-15 栗田工業株式会社 Immersion type membrane separation device
JPH09122686A (en) * 1995-10-30 1997-05-13 Nitto Denko Corp Waste water treatment method
JP3204125B2 (en) * 1996-10-28 2001-09-04 均 大同 Biological treatment method
JP4075332B2 (en) * 2001-02-16 2008-04-16 Jfeエンジニアリング株式会社 Sewage treatment tank
JP3831942B2 (en) * 2002-03-01 2006-10-11 栗田工業株式会社 Membrane separator
JP4361432B2 (en) * 2004-07-02 2009-11-11 株式会社西原 Water treatment equipment
JP2007130579A (en) * 2005-11-10 2007-05-31 Mitsubishi Rayon Eng Co Ltd Filtration membrane cleaning apparatus and method for membrane filtration unit in activated sludge treatment

Also Published As

Publication number Publication date
JP2012176396A (en) 2012-09-13

Similar Documents

Publication Publication Date Title
AU2008101317A4 (en) Cleaning method for simple filtration systems
JP2018108585A (en) Air diffusion device, air diffusion method, and water treatment apparatus
JP5308028B2 (en) Cleaning method for air diffuser
JP2004008981A (en) Membrane separation apparatus
JP5743095B2 (en) Membrane separation activated sludge equipment
JP2000343095A (en) Activated sludge treating device
JP5743096B2 (en) Membrane separation activated sludge equipment
JP2012157849A (en) Membrane separation activated sludge apparatus
JP6358878B2 (en) Membrane filtration device
JP5324117B2 (en) Water treatment facility having a diffuser and a membrane concentrator equipped with the diffuser
JP5135267B2 (en) Air diffuser, submerged membrane separation apparatus equipped with the air diffuser, and method of operating the air diffuser
JP2017064574A (en) Water treatment apparatus
JP6172531B2 (en) Membrane separation activated sludge treatment equipment
JP2015226884A (en) Hollow fiber membrane module and cleaning method therefor
JP6411051B2 (en) Immersion membrane separator and method for operating the same
JP2006198462A (en) Washing method of flat membrane element
JP2007209948A (en) Air diffuser cleaning method when collecting liquid filtrate of solid-liquid mixed treatment liquid
KR20120044594A (en) Air diffuser forming separated diffuser frame and air chamber
JP7311242B2 (en) Air diffuser, air diffusion method, and water treatment device
JP6425067B2 (en) Membrane separation activated sludge treatment system
JP2006035175A (en) Bath water cleaner
JP2019111461A (en) Air diffuser, air diffusion method, and water treatment apparatus
JP2017209618A (en) Air diffuser and air diffusing method
JP2017217579A (en) Hollow fiber membrane filtration device and method for cleaning the same
JP2016215165A (en) Water treatment method and water treatment device

Legal Events

Date Code Title Description
A621 Written request for application examination

Free format text: JAPANESE INTERMEDIATE CODE: A621

Effective date: 20140306

A977 Report on retrieval

Free format text: JAPANESE INTERMEDIATE CODE: A971007

Effective date: 20150113

A131 Notification of reasons for refusal

Free format text: JAPANESE INTERMEDIATE CODE: A131

Effective date: 20150122

A521 Request for written amendment filed

Free format text: JAPANESE INTERMEDIATE CODE: A523

Effective date: 20150312

A521 Request for written amendment filed

Free format text: JAPANESE INTERMEDIATE CODE: A523

Effective date: 20150313

TRDD Decision of grant or rejection written
A01 Written decision to grant a patent or to grant a registration (utility model)

Free format text: JAPANESE INTERMEDIATE CODE: A01

Effective date: 20150408

A61 First payment of annual fees (during grant procedure)

Free format text: JAPANESE INTERMEDIATE CODE: A61

Effective date: 20150421

R150 Certificate of patent or registration of utility model

Ref document number: 5743095

Country of ref document: JP

Free format text: JAPANESE INTERMEDIATE CODE: R150

LAPS Cancellation because of no payment of annual fees