JP4492268B2 - Biological treatment equipment - Google Patents
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- JP4492268B2 JP4492268B2 JP2004270111A JP2004270111A JP4492268B2 JP 4492268 B2 JP4492268 B2 JP 4492268B2 JP 2004270111 A JP2004270111 A JP 2004270111A JP 2004270111 A JP2004270111 A JP 2004270111A JP 4492268 B2 JP4492268 B2 JP 4492268B2
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- Y—GENERAL 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
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Description
本発明は、高濃度の有機物を含む排水から有機物を効率的に除去するための生物処理装置に関する。 The present invention relates to a biological treatment apparatus for efficiently removing organic matter from wastewater containing high-concentration organic matter.
従来、高濃度の有機物を含む排水から生物処理によって有機物を除去する方法として、微生物を付着させた担体を被処理水中で流動させて微生物に有機物を消費ないし吸収させる流動床担体生物処理法が知られている。この方法は、一般的な活性汚泥法と比べて処理槽容積当たりの有機物負荷を高く取ることができ、処理効率に優れる。このような流動床担体生物処理法の具体的手法として、例えば、特開平9−308892号公報には、微生物を担持した流動担体を保持した生物処理槽の流出液を沈殿槽で固液分離して処理水を得る方法が開示されている。 Conventionally, as a method for removing organic matter from wastewater containing high-concentration organic matter by biological treatment, there is known a fluidized bed carrier biological treatment method in which a carrier on which microorganisms are attached flows in treated water and the microorganisms consume or absorb organic matter. It has been. This method can take a higher organic substance load per treatment tank volume than a general activated sludge method, and is excellent in treatment efficiency. As a specific technique of such a fluidized bed carrier biological treatment method, for example, Japanese Patent Laid-Open No. 9-308992 discloses that the effluent of a biological treatment tank holding a fluid carrier carrying microorganisms is solid-liquid separated in a sedimentation tank. A method for obtaining treated water is disclosed.
また、有機物を含む水を活性汚泥と混合して生物処理した後、分離膜を用いて濾過を行うことで活性汚泥と処理水を分離する膜分離活性汚泥法も広く用いられており、この膜分離活性汚泥法を、生物膜を形成した濾材の充填層を形成した生物膜処理槽と組み合わせた方法として、特開平6−47399号公報には、生物膜処理槽の流出水を浸漬膜型好気性処理槽で処理して膜透過水を処理水として抜き出し、該処理槽内の汚泥を前段の生物膜処理槽に返送する方法が開示されている。
しかし、流動床担体生物処理法では、分解性の良い有機物は微生物により高速で吸収分解できる反面、分解性の悪い有機物の除去能力は一般的な活性汚泥処理法と殆ど変わらないため、高濃度の有機物を含む排水を処理して一般的な活性汚泥法と同等の処理水を得ようとすると、処理槽の必要容量が過大になるという欠点があった。また、微生物が増殖し、余剰汚泥として処理水に混じって流出するが、この余剰汚泥はフロック化し難いため、これを除去するには凝集剤の使用が不可欠であるという欠点もあった。 However, in the fluidized bed biological treatment method, organic substances with good degradability can be absorbed and decomposed at high speed by microorganisms, but the removal ability of organic substances with poor degradability is almost the same as general activated sludge treatment methods. When wastewater containing organic matter is treated to obtain treated water equivalent to a general activated sludge method, there is a disadvantage that the required capacity of the treatment tank becomes excessive. In addition, microorganisms grow and flow out as surplus sludge mixed with the treated water. However, since this surplus sludge is difficult to flock, there is a disadvantage that the use of a flocculant is indispensable to remove this sludge.
一方、膜分離活性汚泥法では、高濃度の有機物を処理しようとすると活性汚泥を高濃度に保つ必要があるため、活性汚泥内に直接浸漬した分離膜に目詰まりを生じやすいという欠点がある。 On the other hand, the membrane-separated activated sludge method has a drawback that clogging is likely to occur in the separation membrane directly immersed in the activated sludge because it is necessary to keep the activated sludge at a high concentration when trying to treat a high concentration organic matter.
本発明は上記従来の流動床担体生物処理法と膜分離活性汚泥法の問題点を解決し、高濃度の有機物を含む排水を、処理槽の必要容量を抑え、また、余剰汚泥除去のための凝集剤を必要とすることなく、更には、浸漬膜の目詰まりを防止して効率的に処理して高水質の処理水を得ることができる生物処理装置を提供することを目的とする。 The present invention solves the problems of the above-described conventional fluidized bed carrier biological treatment method and membrane separation activated sludge method, reduces wastewater containing high-concentration organic matter, reduces the required capacity of the treatment tank, and removes excess sludge. It is another object of the present invention to provide a biological treatment apparatus that does not require a flocculant and that can be efficiently treated by preventing clogging of the immersion membrane and obtaining high-quality treated water.
本発明の生物処理装置は、有機性排水を受け入れる、微生物を担持した流動担体を保持する第1の好気性生物処理槽と、該第1の好気性生物処理槽の流出水を受け入れる、微生物を担持した流動担体と浮遊活性汚泥とを保持する第2の好気性生物処理槽と、該第2の好気性生物処理槽の流出水を受け入れ、該流出水を上澄水と沈殿汚泥とに分離する沈殿槽と、該沈殿槽の上澄水を受け入れ、該上澄水に同伴される汚泥を分離すると共に処理水を排出する分離膜浸漬槽であって、槽内に浸漬された分離膜モジュールと該分離膜モジュールの下方に設けられた散気手段とを備える分離膜浸漬槽と、前記沈殿槽の沈殿汚泥を前記第2の好気性生物処理槽に返送する第1の汚泥返送手段と、前記分離膜浸漬槽の汚泥を前記第2の好気性生物処理槽に返送する第2の汚泥返送手段と、を具備する生物処理装置であって、該有機性排水が、BOD2000mg/L以上の排水であり、該分離浸漬膜槽内の汚泥濃度が1000〜6000mg/Lであることを特徴とする。 The biological treatment apparatus of the present invention includes a first aerobic biological treatment tank that holds a fluid carrier carrying microorganisms and that accepts organic waste water, and a microorganism that accepts effluent water from the first aerobic biological treatment tank. A second aerobic biological treatment tank holding the supported fluid carrier and suspended activated sludge, and the effluent water of the second aerobic biological treatment tank is received, and the effluent water is separated into supernatant water and precipitated sludge. A separation membrane immersion tank that receives the supernatant water of the precipitation tank, separates sludge entrained in the supernatant water, and discharges treated water, the separation membrane module immersed in the tank and the separation A separation membrane immersion tank provided with a diffuser provided below the membrane module, a first sludge return means for returning the sedimented sludge of the settling tank to the second aerobic biological treatment tank, and the separation membrane Return sludge from the immersion tank to the second aerobic biological treatment tank A second sludge return means for, a biological treatment device having a, said organic waste water is a BOD2000mg / L or more drainage, sludge concentration in the separation submerged membrane tank is at 1000~6000mg / L characterized in that there.
請求項2の生物処理装置は、請求項1において、前記第1の好気性生物処理槽の槽負荷が0.8〜8.0kg−BOD/m3・dであることを特徴とする。 The biological treatment apparatus according to claim 2 is characterized in that, in claim 1, the tank load of the first aerobic biological treatment tank is 0.8 to 8.0 kg-BOD / m 3 · d.
請求項3の生物処理装置は、請求項1又は2において、前記第2の好気性生物処理槽の実効容量が前記第1の好気性生物処理槽の実効容量の1〜10倍であることを特徴とする。 The biological treatment apparatus according to claim 3 is the biological treatment apparatus according to claim 1 or 2, wherein the effective capacity of the second aerobic biological treatment tank is 1 to 10 times the effective capacity of the first aerobic biological treatment tank. Features.
請求項4の生物処理装置は、請求項1ないし3のいずれか1項において、前記沈殿槽の水面積負荷が5〜30m/dで、滞留時間が1〜18時間であることを特徴とする。 A biological treatment apparatus according to a fourth aspect is characterized in that, in any one of the first to third aspects, the water area load of the settling tank is 5 to 30 m / d and the residence time is 1 to 18 hours. .
請求項5の生物処理装置は、請求項1ないし4のいずれか1項において、前記分離膜浸漬槽の滞留時間が1〜18時間であることを特徴とする。 Biological treatment apparatus according to claim 5, in any one of claims 1 to 4, residence distillation time of the separation membrane immersion tank is characterized in that 1 to 18 hours.
即ち、本発明では、上記課題を解決すべく、第1及び第2の好気性生物処理槽を設けて流動床担体生物処理を2段に分けて行い、その後、汚泥を沈降させて引き抜くことができる沈殿槽を設けることにより余剰汚泥の大部分を凝集剤を使わずにフロック化させて除去し、残った僅かな余剰汚泥を更に後段の分離膜浸漬槽で分離する。この分離膜浸漬槽には、予め沈殿槽で余剰汚泥の大部分を除去した後の比較的低濃度の汚泥が流入するため、膜濾過における目詰まりの問題は少なく、この分離膜浸漬槽内で残留する有機物の分解除去と、浸漬膜による汚泥の膜濾過とを効率的に行うことができる。この分離膜浸漬槽の浸漬膜の透過水として得られる処理水は、精密濾過(MF)膜等を透過した高水質の処理水である。そして、沈殿槽の分離汚泥と分離膜浸漬槽の分離汚泥を第2の好気性生物処理槽に返送することにより、この第2の好気性生物処理槽において、流動床担体生物処理における分解性の悪い有機物の除去能力を向上させ、これを効率的に分解除去することが可能となる。 That is, in the present invention, in order to solve the above-mentioned problems, the first and second aerobic biological treatment tanks are provided and the fluidized bed carrier biological treatment is performed in two stages, and then the sludge is settled and extracted. By providing a settling tank that can be used, most of the excess sludge is removed by flocculation without using a flocculant, and the remaining surplus sludge is further separated in a subsequent separation membrane immersion tank. In this separation membrane immersion tank, a relatively low concentration of sludge after removing most of the excess sludge in the precipitation tank flows in advance, so there are few problems of clogging in membrane filtration. The remaining organic matter can be decomposed and removed, and sludge membrane filtration with an immersion membrane can be performed efficiently. The treated water obtained as the permeated water of the submerged membrane in the separation membrane soaking tank is a high quality treated water that has permeated through a microfiltration (MF) membrane or the like. Then, by returning the separated sludge in the settling tank and the separated sludge in the separation membrane soaking tank to the second aerobic biological treatment tank, in this second aerobic biological treatment tank, the degradability in the fluidized bed carrier biological treatment It is possible to improve the ability to remove bad organic substances and efficiently decompose and remove them.
本発明の生物処理装置によれば、高濃度有機性排水を、比較的小容量の装置により、凝集剤を必要とすることなく、また、浸漬膜の目詰まりを防止して、効率的に処理して高水質の処理水を得ることができる。 According to the biological treatment apparatus of the present invention, high-concentration organic wastewater can be efficiently treated by using a relatively small-capacity apparatus without requiring a flocculant and preventing clogging of the immersion film. As a result, high-quality treated water can be obtained.
以下に図面を参照して本発明の生物処理装置の実施の形態を詳細に説明する。 Hereinafter, embodiments of a biological treatment apparatus of the present invention will be described in detail with reference to the drawings.
図1は本発明の生物処理装置の実施の形態を示す系統図である。図1において、1は第1の好気性生物処理槽であり、内部に微生物を担持した流動担体が保持されており、処理水流出部に設けられたスクリーン1Aと、槽内下部に設けられた散気装置1Bとを備える。2は第2の好気性生物処理槽であり、内部に微生物を担持した流動担体と浮遊活性汚泥とが保持されており、処理水流出部に設けられたスクリーン2Aと、槽内下部に設けられた散気装置2Bとを備える。3は沈殿槽である。4は分離膜浸漬槽であり、内部に分離膜モジュール4Aが浸漬されており、この分離膜モジュールの下方に散気装置4Bが設けられている。5はポンプである。 FIG. 1 is a system diagram showing an embodiment of a biological treatment apparatus of the present invention. In FIG. 1, reference numeral 1 denotes a first aerobic biological treatment tank, in which a fluid carrier carrying microorganisms is held, and is provided at a screen 1A provided at a treated water outflow part and at a lower part in the tank. A diffuser 1B is provided. Reference numeral 2 denotes a second aerobic biological treatment tank, in which a fluid carrier carrying microorganisms and suspended activated sludge are held, and is provided at a screen 2A provided at the treated water outflow part and at a lower part in the tank. A diffuser 2B. 3 is a settling tank. Reference numeral 4 denotes a separation membrane immersion tank, in which a separation membrane module 4A is immersed, and an air diffuser 4B is provided below the separation membrane module. 5 is a pump.
第1,第2の好気性生物処理槽1,2の形状には特に制限はなく、円筒形、直方体形状などいずれでも良く、内部に澱みを生じさせないためのバッフル板などが設けられていても良い。 The shape of the first and second aerobic biological treatment tanks 1 and 2 is not particularly limited, and may be any of a cylindrical shape, a rectangular parallelepiped shape, and a baffle plate for preventing stagnation inside. good.
第1,第2の好気性生物処理槽1,2に保持される担体は、微生物を固定化させかつ水中を流動する素材よりなり、比重が水と同等で微生物が付着しやすい、例えばスポンジ状の樹脂など、多孔質或いは多くの隙間を有する構造体であることが好ましく、その大きさは、直径ないしは2枚の平行板で挟んだときの最大距離として0.5〜200mmの範囲であることが好ましい。ただし、槽内に保持される担体は、その形状、大きさ、材質等において均一であっても良く、異なるものが混在していても良い。また、第1,第2好気性生物処理槽1,2内の担体保持量は、担体を槽内水中におけると同じ状態のまま陸上で乱雑に積んだ際の容積が、各好気生物処理槽1,2の有効容量の10〜60%となるようにすることが好ましい。 The carriers held in the first and second aerobic biological treatment tanks 1 and 2 are made of a material that immobilizes microorganisms and flows in water, and has a specific gravity equivalent to that of water and easily adheres to microorganisms. It is preferable that the structure is porous or has a large number of gaps, such as resin, and the size is in the range of 0.5 to 200 mm as the maximum distance when sandwiched between two diameters or two parallel plates. Is preferred. However, the carrier held in the tank may be uniform in shape, size, material, or the like, or different ones may be mixed. In addition, the amount of carrier retained in the first and second aerobic biological treatment tanks 1 and 2 is the volume when the carrier is randomly stacked on land with the same state as in the water in the tank. It is preferable to be 10 to 60% of the effective capacity of 1 and 2.
スクリーン1A,2Aは、担体と流出水とを分離するためのものであり、目開きが担体の大きさより小さく、流動する担体から流出水を分離し得るものであれば良く、その形状や材質は特に限定されないが、例えばステンレス製のスクリーン、プラスチック製の網状物などを用いることができる。スクリーン1A,2Aの水中部分の表面積は流出水1m3/d当り0.5m2以上、例えば1〜1.5m2となるようにするのが、水の流出効率の面で好ましい。また、スクリーン1A,2Aの担体による目詰まりを防ぐために、必要に応じてスクリーン1A,2A下側に散気管などを設けるなどしてスクリーン1A,2Aの表面と平行な向きの水流が十分に当たるようにしても良い。 The screens 1A and 2A are for separating the carrier and the effluent water, as long as the openings are smaller than the size of the carrier and the effluent water can be separated from the flowing carrier. Although not particularly limited, for example, a stainless steel screen, a plastic mesh or the like can be used. Screen 1A, the surface area of the water portion of the 2A outflow water 1 m 3 / d per 0.5 m 2 or more, for example, to such a 1~1.5M 2 is preferred from the viewpoint of water outflow efficiency. Further, in order to prevent clogging of the screens 1A and 2A by the carrier, a water flow in a direction parallel to the surfaces of the screens 1A and 2A is sufficiently applied by providing an air diffuser or the like below the screens 1A and 2A as necessary. Anyway.
第1,第2好気性生物処理槽1,2の槽下部に設けられる散気装置1B,2Bは、好気性生物処理槽1,2の内部全体に必要かつ十分な流動を起こし、かつ微生物に溶存酸素を行き渡らせることができるものであれば良く、その形式や設置数には特に制限はないが、例えば、ディフューザー、エアレーター、孔開き散気管などを用いることができる。 The air diffusers 1B and 2B provided at the lower part of the first and second aerobic biological treatment tanks 1 and 2 cause necessary and sufficient flow throughout the aerobic biological treatment tanks 1 and 2 and There is no particular limitation on the type and the number of installations as long as the dissolved oxygen can be distributed. For example, a diffuser, an aerator, a perforated diffuser tube, or the like can be used.
第1,第2好気性生物処理槽1,2は、基本的には同等の仕様のものが用いられるが、双方で異なる構成を採用しても良い。ただし、第2の好気性生物処理槽2にのみ後段の沈殿槽3及び分離膜浸漬槽4からの汚泥が返送されるため、第1の好気性生物処理槽1と第2の好気性生物処理槽2とは、第1の好気性生物処理槽1から第2の好気性生物処理槽2への水の供給がない場合であっても、第2の好気性生物処理槽2から第1の好気性生物処理槽1への逆流が起こることがないように接続されていることが好ましい。 The first and second aerobic biological treatment tanks 1 and 2 basically have the same specifications, but may have different configurations. However, since the sludge from the subsequent settling tank 3 and the separation membrane immersion tank 4 is returned only to the second aerobic biological treatment tank 2, the first aerobic biological treatment tank 1 and the second aerobic biological treatment are performed. Even if there is no supply of water from the first aerobic biological treatment tank 1 to the second aerobic biological treatment tank 2, the tank 2 refers to the first aerobic biological treatment tank 2 from the first aerobic biological treatment tank 2. It is preferable to be connected so that no backflow to the aerobic biological treatment tank 1 occurs.
第1,第2の好気性生物処理槽1,2の実効容量(有効容積)については、第1の好気性生物処理槽1の実効容量は流入する有機物をBODで表したとき、槽負荷が0.8〜8.0kg−BOD/m3・dとなるように設計することが好ましい。槽負荷がこの範囲よりも大きいと十分な有機物除去を行えず、この範囲よりも小さいと徒に装置容量が大きくなり好ましくない。また、第2の好気性生物処理槽2の実効容量は、第1の好気性生物処理槽1の実効容量よりも大きいことが好ましく、例えば第1の好気性生物処理槽1の実効容量の5〜8倍であることが好ましい。第2の好気性生物処理槽2の実効容量がこの範囲よりも小さいと、難分解性の有機物を十分に除去し得ず、この範囲よりも大きいと徒に装置容量が大きくなり好ましい。 Regarding the effective capacity (effective volume) of the first and second aerobic biological treatment tanks 1 and 2, the effective capacity of the first aerobic biological treatment tank 1 is the tank load when the inflowing organic matter is represented by BOD. It is preferable to design so that it may become 0.8-8.0kg-BOD / m < 3 > * d. If the tank load is larger than this range, sufficient organic matter removal cannot be performed, and if it is smaller than this range, the capacity of the apparatus is undesirably increased. In addition, the effective capacity of the second aerobic biological treatment tank 2 is preferably larger than the effective capacity of the first aerobic biological treatment tank 1, for example, the effective capacity of the first aerobic biological treatment tank 1 is 5 It is preferably ˜8 times. When the effective capacity of the second aerobic biological treatment tank 2 is smaller than this range, it is not possible to sufficiently remove the hardly decomposable organic matter.
沈殿槽3の形状には特に制限はなく、円筒形、直方体形状などいずれでも良く、内部に澱みを生じさせないためのバッフル板などが設けられていても良い。また、余剰汚泥を効率よく沈降させるための攪拌装置などが設けられていてもよいが、全体が上昇流となるような導入部と流出部とを有し、被処理水(流入水)量に対して水平面の面積速度(水面積負荷)が30m/d以下、例えば6〜10m/dであって滞留時間が2時間以上、例えば10〜12時間となるように設計することが好ましい。 There is no restriction | limiting in particular in the shape of the sedimentation tank 3, Any, such as cylindrical shape and a rectangular parallelepiped shape, may be sufficient, and the baffle plate etc. for preventing a starch from being produced inside may be provided. In addition, a stirrer or the like for efficiently sinking excess sludge may be provided, but it has an introduction part and an outflow part so that the whole becomes an upward flow, and the amount of treated water (inflow water) is reduced. On the other hand, it is preferable that the area velocity (water area load) of the horizontal plane is 30 m / d or less, for example, 6 to 10 m / d, and the residence time is 2 hours or more, for example, 10 to 12 hours.
分離膜浸漬槽4の形状には特に制限はなく、円筒形、直方体形状などいずれでも良く、内部に澱みを生じさせないためのバッフル板などが設けられていても良い。分離膜浸漬槽4の実効容積は被処理水(流入水)量に対して滞留時間が2時間以上、例えば10〜12時間で、分離膜モジュールの分離膜部分が十分に水中に浸漬し得る大きさ以上とする。また、槽内の汚泥濃度は概ね20000mg/L以下、例えば3,000〜5,000mg/Lで、分離膜モジュールが高い膜フラックスを維持することができるような汚泥濃度となるように、後述のポンプ5による汚泥の引き抜き量を調節することが好ましい。 There is no restriction | limiting in particular in the shape of the separation membrane immersion tank 4, Any, such as a cylindrical shape and a rectangular parallelepiped shape, may be provided, and the baffle plate etc. for preventing a stagnation inside may be provided. The effective volume of the separation membrane immersion tank 4 is such that the residence time is 2 hours or more, for example, 10 to 12 hours with respect to the amount of treated water (inflow water), and the separation membrane portion of the separation membrane module can be sufficiently immersed in water. More than that. In addition, the sludge concentration in the tank is about 20000 mg / L or less, for example, 3,000 to 5,000 mg / L, and is described later so that the separation membrane module can maintain a high membrane flux. It is preferable to adjust the amount of sludge drawn by the pump 5.
分離膜浸漬槽4内に浸漬される分離膜モジュール4Aの分離膜は、MF膜以下の細孔径のものであれば良く、その形状は中空状でも平面状でも良く、材質も特に定めない。分離膜モジュール4Aは、固液分離に関わる部分が槽内水中に完全に浸漬するように配置する。この分離膜モジュール4Aは、必要に応じて下方に設けられた散気装置4Bから散気を行うことで、膜面を振動させて微生物の固着を防いだり、クロスフロー状の流れによって膜フラックスの向上を図ったりしても良い。分離膜モジュール4Aの膜フラックスは特に定めないが、これが最大となるように分離膜浸漬槽4の汚泥濃度を定めることができるため、本来の膜式活性汚泥法に於けるフラックスよりは高くすることができる。例えば、ポリエチレン製の中空糸MF膜の場合、通常の膜式活性汚泥法で汚泥濃度10000mg/Lの条件下で膜フラックス0.25m/dで使用していたものを、本発明を適用した装置では汚泥濃度5000mg/Lの条件下で膜フラックス約0.4m/dの高い膜フラックスで処理を行うことができる。 The separation membrane of the separation membrane module 4A immersed in the separation membrane immersion tank 4 only needs to have a pore diameter equal to or smaller than that of the MF membrane, and the shape thereof may be hollow or planar, and the material is not particularly defined. The separation membrane module 4A is arranged so that the part related to solid-liquid separation is completely immersed in the water in the tank. This separation membrane module 4A performs aeration from the aeration device 4B provided below as needed, thereby vibrating the membrane surface to prevent microorganisms from sticking, and the cross-flow flow causes the membrane flux to flow. Improvements may be made. The membrane flux of the separation membrane module 4A is not particularly defined, but the sludge concentration in the separation membrane immersion tank 4 can be determined so that this is maximized, so it should be higher than the flux in the original membrane activated sludge method. Can do. For example, in the case of a hollow fiber MF membrane made of polyethylene, an apparatus to which the present invention is applied is used with a membrane flux of 0.25 m / d under the condition of a sludge concentration of 10000 mg / L by a normal membrane activated sludge method. Then, the treatment can be performed with a high membrane flux having a membrane flux of about 0.4 m / d under a sludge concentration of 5000 mg / L.
分離膜モジュール4Aの下方に設けられる散気装置4Bは、分離膜浸漬槽4の内部全体に必要かつ十分な流動を起こし、かつ微生物に溶存酸素を行き渡らせることができるものであれば良く、その形式や設置数には特に制限はないが、例えば、ディフューザー、エアレーター、孔開き散気管などを用いることができる。この散気は、上述の分離膜モジュール4Aの膜面振動のための散気を兼ねて行っても良く、各々別々に行っても良い。 The diffuser 4B provided below the separation membrane module 4A may be any device as long as it causes necessary and sufficient flow throughout the separation membrane immersion tank 4 and can distribute dissolved oxygen to microorganisms. There are no particular restrictions on the type or number of installations, but for example, a diffuser, an aerator, a perforated diffuser tube, or the like can be used. This aeration may be performed as an aeration for the membrane vibration of the separation membrane module 4A described above, or may be performed separately.
ポンプ5は、沈殿槽3で沈降させた余剰汚泥、及び分離膜浸漬槽4内の汚泥の一部を第2の好気性生物処理槽2に戻し、かつこれら各槽の汚泥濃度を一定に保つべく汚泥を引き抜くために設けられる。ポンプ5による沈殿槽3及び分離膜浸漬槽4からの汚泥の引き抜きは連続的に行っても良く、間欠的に行っても良い。また、沈殿槽3からの汚泥の引き抜きと分離膜浸漬槽4からの汚泥の引き抜きとを交互に行っても良く、両槽3,4からの汚泥の引き抜きを同時に行ってこれらを混合しながら第2の好気性生物処理槽2に返送しても良い。また、各槽の汚泥濃度を好適な濃度に一定に保つために、人手による各槽の汚泥濃度の分析結果、汚泥濃度計の検出値、或いは経験上または過去の実績上発生すると予測される余剰汚泥量によって、ポンプ5の吐出側を適宜外部へ切り換えて引き抜き汚泥を系外へ排出するようにしても良い。このポンプ5としては、活性汚泥を移送することができるものであれば良く、その形式等は特に定めない。沈殿槽3の汚泥引き抜き用ポンプと分離膜浸漬槽4の汚泥引き抜き用ポンプとを別々に設けても良く、両槽の汚泥流路に切り換え弁や流量調節弁を設けても良い。 The pump 5 returns the excess sludge settled in the settling tank 3 and a part of the sludge in the separation membrane immersion tank 4 to the second aerobic biological treatment tank 2 and keeps the sludge concentration in each tank constant. It is provided to extract sludge as much as possible. The sludge extraction from the sedimentation tank 3 and the separation membrane immersion tank 4 by the pump 5 may be performed continuously or intermittently. Alternatively, the sludge extraction from the settling tank 3 and the sludge extraction from the separation membrane immersion tank 4 may be performed alternately, and the sludge extraction from both tanks 3 and 4 may be performed simultaneously while mixing them. You may return to the aerobic biological treatment tank 2 of 2. In addition, in order to keep the sludge concentration in each tank at a suitable level, surplus that is expected to be generated from the results of manual analysis of sludge concentration in each tank, the detected value of the sludge concentration meter, or from experience or past performance. Depending on the amount of sludge, the discharge side of the pump 5 may be appropriately switched to the outside so that the extracted sludge is discharged out of the system. The pump 5 is not particularly limited as long as it can transfer activated sludge. The sludge extraction pump of the sedimentation tank 3 and the sludge extraction pump of the separation membrane immersion tank 4 may be provided separately, and a switching valve and a flow rate control valve may be provided in the sludge flow paths of both tanks.
このような本発明の生物処理装置において、原水(有機性排水)は、第1の好気性生物処理槽1及び第2の好気性生物処理槽2に順次に導入され、2段流動床担体生物処理された後沈殿槽3で固液分離され、分離汚泥はポンプ5により第2の好気性生物処理槽2に返送される。なお、沈殿槽3の分離汚泥は、必要に応じてその一部が系外に排出されても良い。沈殿槽3の上澄水は次いで分離膜浸漬槽4に導入され、槽内の微生物で好気性生物処理された後分離膜モジュール4Aで膜濾過され、膜透過水が処理水として系外へ排出される。分離膜浸漬槽4の槽内汚泥はポンプ5により第2の好気性生物処理槽2に返送される。この返送汚泥もまた、必要に応じて一部系外へ排出しても良い。 In such a biological treatment apparatus of the present invention, raw water (organic waste water) is sequentially introduced into the first aerobic biological treatment tank 1 and the second aerobic biological treatment tank 2, and is then supplied to the two-stage fluidized bed carrier organism. After the treatment, solid-liquid separation is performed in the sedimentation tank 3, and the separated sludge is returned to the second aerobic biological treatment tank 2 by the pump 5. A part of the separated sludge in the settling tank 3 may be discharged out of the system as necessary. The supernatant water of the sedimentation tank 3 is then introduced into the separation membrane immersion tank 4, subjected to aerobic biological treatment with microorganisms in the tank, and then filtered through the separation membrane module 4 </ b> A, and the membrane permeate is discharged out of the system as treated water. The The sludge in the separation membrane immersion tank 4 is returned to the second aerobic biological treatment tank 2 by the pump 5. This return sludge may also be partially discharged outside the system as necessary.
本発明によれば、第1,第2好気性生物処理槽1,2を経た2段流動床担体生物処理水を沈殿槽3で固液分離することにより、流動床担体生物処理で生じる余剰汚泥の大部分を凝集剤を用いることなくフロック化させて沈降分離することができる。そして、沈殿槽3の上澄水に含まれる僅かな余剰汚泥を分離膜浸漬槽4で膜濾過して分離する。この分離膜浸漬槽4には、予め沈殿槽3で余剰汚泥の大部分を除去した後の比較的低濃度の汚泥が流入するため、膜濾過における目詰まりの問題は少なく、この分離膜浸漬槽4内で残留する有機物の分解除去と、浸漬膜による汚泥の膜濾過とを効率的に行うことができる。この分離膜浸漬槽4の分離膜モジュール4Aの透過水として得られる処理水は、精密濾過(MF)膜等を透過した高水質の処理水である。しかも、本発明では、沈殿槽3の分離汚泥と分離膜浸漬槽4の分離汚泥を第2の好気性生物処理槽2に返送することにより、この第2の好気性生物処理槽2における分解性の悪い有機物の除去能力を向上させることができる。このため、第2の好気性生物処理槽2の実効容量は比較的小さなもので足り、この結果、全体の装置容量の低減を図ることができる。 According to the present invention, surplus sludge generated by fluidized bed carrier biological treatment by solid-liquid separation of the two-stage fluidized bed carrier biologically treated water that has passed through the first and second aerobic biological treatment tanks 1 and 2 in the sedimentation tank 3. Most of this can be flocculated and separated by sedimentation without using a flocculant. Then, a slight excess sludge contained in the supernatant water of the sedimentation tank 3 is separated by membrane filtration in the separation membrane immersion tank 4. Since relatively low concentration sludge after removing most of the excess sludge in the sedimentation tank 3 flows into the separation membrane immersion tank 4 in advance, there is little problem of clogging in membrane filtration. The organic matter remaining in 4 can be decomposed and removed, and sludge membrane filtration with an immersion membrane can be performed efficiently. The treated water obtained as the permeated water of the separation membrane module 4A of the separation membrane immersion tank 4 is a high quality treated water that has permeated through a microfiltration (MF) membrane or the like. Moreover, in the present invention, the separation sludge in the sedimentation tank 3 and the separation sludge in the separation membrane immersion tank 4 are returned to the second aerobic biological treatment tank 2, so that the degradability in the second aerobic biological treatment tank 2 is achieved. The ability to remove bad organic substances can be improved. For this reason, the effective capacity of the second aerobic biological treatment tank 2 may be relatively small, and as a result, the overall apparatus capacity can be reduced.
このような本発明の生物処理装置は、調理ゴミ等の厨芥含有排水や、食品製造排水、酒類製造排水等の有機性排水の生物処理に有効であり、特に、このような有機性排水のうち有機物濃度が2,000mg−BOD/L以上であるような高濃度有機性排水の生物処理に有効である。 Such a biological treatment apparatus of the present invention is effective for biological treatment of organic wastewater such as food wastewater and liquor production wastewater such as cooking waste, and particularly among such organic wastewater. It is effective for biological treatment of high-concentration organic wastewater whose organic matter concentration is 2,000 mg-BOD / L or more.
以下に実施例及び比較例を挙げて本発明をより具体的に説明する。 Hereinafter, the present invention will be described more specifically with reference to Examples and Comparative Examples.
実施例1
図1に示す本発明の生物処理装置により、BOD濃度2,000mg/Lの豆腐製造排水の処理を100L/dの流量で行った。各槽の仕様は次の通りである。
第1の好気性生物処理槽1:実効容量=15L
BOD負荷=1.56kg−BOD/m3・d(第2の
好気性生物処理槽と合わせて)
担体種類=粒径3〜10mmの角型
材質:発泡ポリウレタン
担体保持量=槽有効容量の50%
第2の好気性生物処理槽2:実効容量=100L
担体種類=粒径3〜10mmの角型
材質:発泡ポリウレタン
担体保持量=槽有効容量の50%
沈殿槽3:実効容量=30L
水面積負荷=6.7m/d
滞留時間=7.2時間
分離膜浸漬槽4:実効容量=30L
滞留時間=7.2時間
分離膜モジュールの膜種=中空糸型ポリエチレン膜
Example 1
The tofu production waste water having a BOD concentration of 2,000 mg / L was processed at a flow rate of 100 L / d by the biological treatment apparatus of the present invention shown in FIG. The specifications of each tank are as follows.
First aerobic biological treatment tank 1: Effective capacity = 15L
BOD load = 1.56 kg−BOD / m 3 · d (second
Combined with aerobic biological treatment tank)
Carrier type = square shape with particle size of 3-10 mm
Material: Polyurethane foam
Carrier holding amount = 50% of tank effective capacity
Second aerobic biological treatment tank 2: Effective capacity = 100 L
Carrier type = square shape with particle size of 3-10 mm
Material: Polyurethane foam
Carrier holding amount = 50% of tank effective capacity
Sedimentation tank 3: Effective capacity = 30L
Water area load = 6.7 m / d
Residence time = 7.2 hours Separation membrane immersion tank 4: Effective capacity = 30L
Residence time = 7.2 hours
Membrane type of separation membrane module = hollow fiber type polyethylene membrane
沈殿槽3の分離汚泥は100L/dの流量で第2の好気性生物処理槽2に返送し、上澄水125L/dを分離膜浸漬槽4に導入した。また、分離膜浸漬槽4では槽内汚泥を25L/dの流量で第2の好気性生物処理槽2に返送し、膜濾過水100L/dを処理水として取り出した。この分離膜浸漬槽4の汚泥濃度は4,000〜6,000mg/Lに維持された。 The separated sludge in the settling tank 3 was returned to the second aerobic biological treatment tank 2 at a flow rate of 100 L / d, and the supernatant water 125 L / d was introduced into the separation membrane immersion tank 4. Moreover, in the separation membrane immersion tank 4, sludge in the tank was returned to the second aerobic biological treatment tank 2 at a flow rate of 25 L / d, and 100 L / d of membrane filtrate was taken out as treated water. The sludge concentration in the separation membrane immersion tank 4 was maintained at 4,000 to 6,000 mg / L.
その結果、BOD濃度2〜10mg/L、SSを含まない高水質処理水を分離膜モジュールの目詰まりを引き起こすことなく、0.4m/dの高い膜フラックスで2ヶ月間安定に得ることができた。 As a result, BOD concentration of 2 to 10 mg / L, high-quality treated water not containing SS can be stably obtained for 2 months with a high membrane flux of 0.4 m / d without causing clogging of the separation membrane module. It was.
比較例1
実施例1において、沈殿槽を省略し、第2の好気性生物処理槽2の流出水を直接分離膜浸漬槽4に導入したこと以外は同様にして処理を行った。その結果、得られた処理水のBOD濃度は10〜20mg/L、SSは含まれず比較的高水質であったが、分離膜浸漬槽4内の汚泥濃度は25,000mg/Lとなり、3日間の運転により、分離膜モジュールの目詰まりで、膜フラックスは0.1m/d以下に低下し、運転を継続することが困難になった。
Comparative Example 1
In Example 1, the treatment was performed in the same manner except that the settling tank was omitted and the outflow water of the second aerobic biological treatment tank 2 was directly introduced into the separation membrane immersion tank 4. As a result, the BOD concentration of the treated water obtained was 10 to 20 mg / L and SS was not included, and the water quality was relatively high, but the sludge concentration in the separation membrane immersion tank 4 was 25,000 mg / L for 3 days. Due to the clogging of the separation membrane module, the membrane flux decreased to 0.1 m / d or less, making it difficult to continue the operation.
比較例2
実施例1において、分離膜浸漬槽を省略したこと以外は同様にして処理を行ったところ、得られた処理水のBOD濃度は100〜500mg/L、SSは1,000〜5,000mg/Lで高水質の処理水を得ることができなかった。
Comparative Example 2
In Example 1, when it processed similarly except having omitted the separation membrane immersion tank, the BOD density | concentration of the obtained treated water was 100-500 mg / L, SS was 1,000-5,000 mg / L. It was not possible to obtain high quality treated water.
比較例3
実施例1において、第1の好気性生物処理槽を省略し、有機性排水を直接第2の好気性生物処理槽に導入し、第2の好気性生物処理槽の実効容量を115Lとしたこと以外は同様にして処理を行ったところ、得られた処理水のBOD濃度は5〜30mg/Lで、高水質の処理水を得ることができなかった。
Comparative Example 3
In Example 1, the first aerobic biological treatment tank was omitted, the organic waste water was directly introduced into the second aerobic biological treatment tank, and the effective capacity of the second aerobic biological treatment tank was 115 L. When the treatment was performed in the same manner except that the BOD concentration of the obtained treated water was 5 to 30 mg / L, it was not possible to obtain treated water with high quality.
1 第1の好気性生物処理槽
2 第2の好気性生物処理槽
3 沈殿槽
4 分離膜浸漬槽
4A 分離膜モジュール
4B 散気装置
DESCRIPTION OF SYMBOLS 1 1st aerobic biological treatment tank 2 2nd aerobic biological treatment tank 3 Precipitation tank 4 Separation membrane immersion tank 4A Separation membrane module 4B Air diffuser
Claims (5)
該第1の好気性生物処理槽の流出水を受け入れる、微生物を担持した流動担体と浮遊活性汚泥とを保持する第2の好気性生物処理槽と、
該第2の好気性生物処理槽の流出水を受け入れ、該流出水を上澄水と沈殿汚泥とに分離する沈殿槽と、
該沈殿槽の上澄水を受け入れ、該上澄水に同伴される汚泥を分離すると共に処理水を排出する分離膜浸漬槽であって、槽内に浸漬された分離膜モジュールと該分離膜モジュールの下方に設けられた散気手段とを備える分離膜浸漬槽と、
前記沈殿槽の沈殿汚泥を前記第2の好気性生物処理槽に返送する第1の汚泥返送手段と、
前記分離膜浸漬槽の汚泥を前記第2の好気性生物処理槽に返送する第2の汚泥返送手段と、
を具備する生物処理装置であって、
該有機性排水が、BOD2000mg/L以上の排水であり、該分離浸漬膜槽内の汚泥濃度が1000〜6000mg/Lであることを特徴とする生物処理装置。 A first aerobic biological treatment tank that holds a fluid carrier carrying microorganisms and that accepts organic waste water;
A second aerobic biological treatment tank that retains a fluid carrier carrying microorganisms and suspended activated sludge that receives the effluent of the first aerobic biological treatment tank;
A settling tank that receives the effluent of the second aerobic biological treatment tank and separates the effluent into supernatant water and precipitated sludge;
A separation membrane immersion tank that receives the supernatant water of the sedimentation tank, separates sludge entrained in the supernatant water, and discharges treated water, the separation membrane module immersed in the tank, and the lower part of the separation membrane module A separation membrane immersion tank comprising a diffuser provided in
First sludge return means for returning the settling sludge in the settling tank to the second aerobic biological treatment tank;
A second sludge return means for returning the sludge of the separation membrane immersion tank to the second aerobic biological treatment tank;
A biological treatment apparatus comprising :
The biological treatment apparatus , wherein the organic waste water is waste water having a BOD of 2000 mg / L or more, and a sludge concentration in the separation / immersion membrane tank is 1000 to 6000 mg / L.
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