JP4609989B2 - Wastewater treatment equipment - Google Patents

Wastewater treatment equipment Download PDF

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JP4609989B2
JP4609989B2 JP2004274386A JP2004274386A JP4609989B2 JP 4609989 B2 JP4609989 B2 JP 4609989B2 JP 2004274386 A JP2004274386 A JP 2004274386A JP 2004274386 A JP2004274386 A JP 2004274386A JP 4609989 B2 JP4609989 B2 JP 4609989B2
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waste water
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phosphorus
wastewater
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聡 常田
彰 平田
昭彦 寺田
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Waseda University
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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、排水処理装置に係り、更に詳しくは、脱窒性リン蓄積細菌を用いて排水処理を行う際に、嫌気工程後に添加する有機物を不要にできる排水処理装置に関する。 The present invention relates to a waste water treatment equipment, and more particularly, in performing the wastewater treatment using a denitrifying phosphorus accumulating bacteria relates to waste water treatment equipment that can be made unnecessary organic matter added after anaerobic step.

湖沼、内湾、内海等の停滞的な閉鎖性水域においては、窒素やリンがアオコや赤潮の発生を引き起こすことから、前記閉塞性水域の健全な水環境を創出するには、当該水域に流入する生活排水から窒素及びリンを十分に除去する必要がある。そこで、排水から窒素及びリンを除去する排水処理技術として、所定の細菌を用いた種々の生物学的処理が知られており、この生物学的処理として、嫌気／無酸素／好気法（Ａ２Ｏ法）が知られている（特許文献１参照）。このＡ２Ｏ法は、硝化細菌及び脱窒細菌を使って排水中から窒素成分を除去するとともに、リン蓄積細菌を使って排水中からリンを除去する方法である。ここで、脱窒細菌及びリン蓄積細菌による反応を進行させるには、排水中の有機物が必要不可欠である。 In stagnant closed water areas such as lakes, inner bays, inland seas, etc., nitrogen and phosphorus cause the occurrence of blue sea bream and red tide. Nitrogen and phosphorus must be sufficiently removed from domestic wastewater. Therefore, various biological treatments using predetermined bacteria are known as wastewater treatment techniques for removing nitrogen and phosphorus from wastewater. As this biological treatment, anaerobic / anoxic / aerobic methods (A 2 O method) is known (see Patent Document 1). The A 2 O method is a method of removing nitrogen components from wastewater using nitrifying bacteria and denitrifying bacteria and removing phosphorus from wastewater using phosphorus accumulating bacteria. Here, in order to advance the reaction by denitrifying bacteria and phosphorus accumulating bacteria, organic substances in the wastewater are indispensable.

しかしながら、前記Ａ２Ｏ法では、雨水等の流入により有機物濃度が低くなった排水の場合、脱窒及び脱リンのための有機炭素源を十分に確保することができず、窒素及びリンの効率的な除去は見込めないという問題がある。 However, in the A 2 O method, in the case of wastewater whose organic matter concentration has become low due to the inflow of rainwater or the like, it is not possible to sufficiently secure an organic carbon source for denitrification and phosphorus removal, and the efficiency of nitrogen and phosphorus There is a problem that it cannot be expected to be removed.

そこで、本発明者らは、前記Ａ２Ｏ法の問題を解決するべく、無炭素、無酸素条件下で脱窒及びリンの取り込みを同時に行える脱窒性リン蓄積細菌を利用した嫌気／好気／無酸素法（ＡＯＡ法）を既提案した（特許文献１参照）。このＡＯＡ法では、先ず、嫌気工程で、脱窒性リン蓄積細菌により、有機物の摂取及びリンの放出が行われる。次に、好気工程で、硝化細菌を使ってアンモニア等を硝酸態窒素に変える硝化反応が行われる。そして、無酸素工程で、脱窒性リン蓄積細菌により、硝酸態窒素の窒素ガスへの変換及びリンの取り込みが行われる。このＡＯＡ法では、嫌気工程後、好気工程前に、有機物を排水に添加することで、好気工程時の脱窒性リン蓄積細菌によるリン取り込みを制限する。これは、有機物を添加しないと、好気工程時に、酸素の存在によって脱窒性リン蓄積細菌にリンが取り込まれてしまい、その分、後の無酸素工程で、リンと同時に取り込まれる硝酸態窒素の取り込み量が少なくなるからである。
特開２００３−２８５０９６号公報 In order to solve the problem of the A 2 O method, the present inventors have made anaerobic / aerobic using denitrifying phosphorus accumulating bacteria that can simultaneously perform denitrification and phosphorus uptake under carbon-free and oxygen-free conditions. / An oxygen-free method (AOA method) has already been proposed (see Patent Document 1). In this AOA method, first, ingestion of organic matter and release of phosphorus are performed by denitrifying phosphorus accumulating bacteria in an anaerobic process. Next, in the aerobic process, a nitrification reaction is performed in which ammonia or the like is converted into nitrate nitrogen using nitrifying bacteria. In the oxygen-free process, conversion of nitrate nitrogen to nitrogen gas and phosphorus uptake are performed by denitrifying phosphorus accumulating bacteria. In this AOA method, the organic matter is added to the waste water after the anaerobic process and before the aerobic process, thereby limiting phosphorus uptake by denitrifying phosphorus accumulating bacteria during the aerobic process. This is because if no organic matter is added, phosphorus is taken into the denitrifying phosphorus-accumulating bacteria during the aerobic process due to the presence of oxygen, and nitrate nitrogen that is taken up simultaneously with phosphorus in the subsequent anaerobic process. This is because the amount of uptake is reduced.
JP 2003-285096 A

しかしながら、前記ＡＯＡ法にあっては、嫌気工程後、好気工程前に、有機物を排水に別途添加する必要があるという問題がある。しかも、当該有機物の添加量は、好気工程時における脱窒性リン蓄積細菌のリン取り込みを阻害し、且つ、硝化細菌による硝化反応を阻害しない程度に調整しなければならず、有機物の添加制御が非常に困難になるという問題もある。   However, the AOA method has a problem that it is necessary to separately add organic matter to the waste water after the anaerobic process and before the aerobic process. In addition, the amount of organic matter added must be adjusted to such an extent that it inhibits the uptake of denitrifying phosphorus-accumulating bacteria during the aerobic process and does not inhibit the nitrification reaction by nitrifying bacteria. There is also a problem that becomes very difficult.

本発明は、このような問題に着目して案出されたものであり、その目的は、脱窒性リン蓄積細菌を用いて排水処理を行う際に、嫌気工程後に有機物を添加せずに排水処理を行うことができる排水処理装置を提供することにある。 The present invention has been devised by paying attention to such a problem. The purpose of the present invention is to perform drainage without adding organic matter after the anaerobic process when wastewater treatment is performed using denitrifying phosphorus-accumulating bacteria. and to provide a wastewater treatment equipment which can perform processing.

前記目的を達成するため、本発明は、脱窒性リン蓄積細菌を含む排水が供給される排水領域と、この排水領域に対して隔壁で区分された酸素領域と、この酸素領域に酸素を供給する酸素供給手段とを備えた排水処理装置において、
前記隔壁は、前記酸素領域に供給された酸素を前記排水領域に透過可能にする構造をなすとともに、前記排水領域側の面に硝化細菌が担持され、
前記酸素供給手段は、前記隔壁を透過した酸素のうち前記硝化細菌で消費されずに前記排水領域内の排水中に溶存する酸素の濃度が０．５ｇ／ｍ ３ 以下になるように酸素を供給する、という構成を採っている。 To achieve the pre-Symbol object, the present invention includes a drainage area effluent containing denitrifying phosphorus accumulating bacteria are supplied, and oxygen regions partitioned by the partition wall against the drainage area, the oxygen in this oxygen region In a wastewater treatment apparatus comprising an oxygen supply means for supplying,
The septum oxygen supplied to the oxygen region with forming a structure that transparently available to the drainage area, nitrifying bacteria is carried on the surface of the drainage area side,
The oxygen supply means supplies oxygen so that a concentration of oxygen dissolved in the wastewater in the drainage region is 0.5 g / m 3 or less without being consumed by the nitrifying bacteria among oxygen permeated through the partition wall. It has a configuration of “Yes”.

なお、本明細書において、「硝酸態窒素」とは、ＮＯ３−Ｎ及びＮＯ２−Ｎの総称を意味する。 In the present specification, “nitrate nitrogen” means a generic name of NO 3 —N and NO 2 —N.

本発明によれば、脱窒性リン蓄積細菌により有機物の摂取及びリンの放出が行われる嫌気工程後に、酸素領域に酸素を供給すると、当該酸素が隔壁を通じて排水領域側に放出される。このとき、隔壁の排水領域側の面に存在する硝化細菌が酸素を消費することで、排水中のアンモニア成分を硝酸態窒素に変える硝化反応が行われる。そして、隔壁から放出された直後の酸素が優先的に硝化細菌によって消費され、残った僅かの酸素が排水中に溶存することになる。このため、排水中の脱窒性リン蓄積細菌には殆ど酸素が供給されなくなり、それによるリン取り込みが殆ど行われず、このリン取り込みを阻害する有機物の添加を行わなくてもよく、当該有機物の添加量の複雑な制御も不要となる。 According to the present invention , when oxygen is supplied to the oxygen region after an anaerobic process in which organic matter is ingested and phosphorus is released by denitrifying phosphorus accumulating bacteria, the oxygen is released to the drain region through the partition wall. At this time, the nitrifying bacteria present on the surface of the partition wall on the side of the drainage region consume oxygen, whereby a nitrification reaction is performed to convert the ammonia component in the drainage into nitrate nitrogen. Then, the oxygen immediately after being released from the partition wall is preferentially consumed by the nitrifying bacteria, and the remaining little oxygen is dissolved in the waste water. For this reason, almost no oxygen is supplied to the denitrifying phosphorus accumulating bacteria in the waste water, so that the phosphorus uptake is hardly performed, and it is not necessary to add an organic substance that inhibits this phosphorus uptake. Complex control of quantity is also unnecessary.

また、リン取り込みを阻害する有機物の添加を行わずに、しかも、排水処理に要する時間をＡＯＡ法で排水処理を行った場合とほほ同程度にすることができる。
 Further , without adding an organic substance that inhibits phosphorus uptake, the time required for the wastewater treatment can be made substantially the same as when the wastewater treatment is performed by the AOA method.

以下、本発明の実施例について図面を参照しながら説明する。   Embodiments of the present invention will be described below with reference to the drawings.

図１には、本実施例に係る排水処理装置の概略構成図が示されており、図２には、図１中Ａ部の拡大断面図が示されている。これらの図において、排水処理装置１０は、脱窒性リン蓄積細菌及び硝化細菌を使って排水処理を行う排水処理槽１２と、この排水処理槽１２に酸素を供給する酸素供給手段としてのエアーポンプ１３とを備えて構成されている。   FIG. 1 shows a schematic configuration diagram of a wastewater treatment apparatus according to the present embodiment, and FIG. 2 shows an enlarged sectional view of a portion A in FIG. In these figures, a wastewater treatment apparatus 10 includes a wastewater treatment tank 12 that performs wastewater treatment using denitrifying phosphorus accumulating bacteria and nitrifying bacteria, and an air pump as an oxygen supply means that supplies oxygen to the wastewater treatment tank 12. 13.

前記排水処理槽１２は、脱窒性リン蓄積細菌を含む排水Ｈが供給管１４から内部に供給される槽本体１５と、この槽本体１５の内部に配置され、硝化細菌Ｎが担持された細菌担持装置１６と、槽本体１５内の排水を攪拌する攪拌手段１７とを備えている。   The waste water treatment tank 12 includes a tank body 15 into which waste water H containing denitrifying phosphorus-accumulating bacteria is supplied from a supply pipe 14, and bacteria that are arranged inside the tank body 15 and carry nitrifying bacteria N. A supporting device 16 and stirring means 17 for stirring the waste water in the tank body 15 are provided.

前記細菌担持装置１６は、シリコン製のチューブ１９を多数本結束することで構成される。   The bacteria carrier 16 is configured by bundling a large number of silicon tubes 19.

前記各チューブ１９は、上下方向に延出する向きでそれぞれ配置されており、それらの一端側から、エアーポンプ１３に繋がる供給路２０を通じて内部空間Ｓ１（図２参照）に酸素が導入され、当該導入酸素が、各チューブ１９の他端側に繋がる排出路２１から外部に排出される構造となっている。また、各チューブ１９の周壁１９Ａは、内部空間Ｓ１に供給された酸素をその外側に向かって透過可能にする構造をしているとともに、その外周面を覆うように硝化細菌Ｎが担持されている。ここで、硝化細菌Ｎの担持は、チューブ１９の外周面に沿って硝化細菌Ｎを保持できる限り、種々の手法を採ることができる。本実施例では、チューブ１９の外周面に、硝化細菌Ｎが付いたスラグウールＷを巻きつけることで、硝化細菌Ｎを担持している。その他、硝化細菌Ｎが入ったゲルをチューブ１９の外周面側に固定化してもよい。また、チューブ１９の外周面に糸等を巻くことによって、当該外周面の摩擦係数を高くし、その状態で硝化細菌Ｎを付けるようにしてもよい。更に、グラフト重合等を使って、チューブ１９の外周面に対し、化学的に表面修飾を施し硝化細菌Ｎを固定化することも可能である。   Each tube 19 is arranged in a direction extending in the vertical direction, and oxygen is introduced from one end side thereof into the internal space S1 (see FIG. 2) through the supply path 20 connected to the air pump 13, Introduced oxygen is discharged to the outside from a discharge path 21 connected to the other end of each tube 19. The peripheral wall 19A of each tube 19 has a structure that allows oxygen supplied to the internal space S1 to permeate outwardly, and nitrifying bacteria N are supported so as to cover the outer peripheral surface thereof. . Here, as long as the nitrifying bacteria N can be held along the outer peripheral surface of the tube 19, various methods can be used to carry the nitrifying bacteria N. In this embodiment, the nitrifying bacteria N are carried by winding the slag wool W with the nitrifying bacteria N around the outer peripheral surface of the tube 19. In addition, a gel containing nitrifying bacteria N may be immobilized on the outer peripheral surface side of the tube 19. Further, by winding a thread or the like around the outer peripheral surface of the tube 19, the friction coefficient of the outer peripheral surface may be increased, and the nitrifying bacteria N may be attached in that state. Furthermore, it is also possible to immobilize the nitrifying bacteria N by chemically modifying the outer peripheral surface of the tube 19 using graft polymerization or the like.

チューブ１９の内部空間Ｓ１に供給された酸素は、前記排出路２１から外部に排出される他に、周壁１９Ａを透過し、その外側に担持された硝化細菌Ｎに向かって放出される。そして、硝化細菌Ｎが放出酸素を消費し、消費されなかった残りの酸素が、細菌担持装置１６を除く槽本体１５の排水受容空間Ｓ２に放出される。   The oxygen supplied to the internal space S1 of the tube 19 is discharged from the discharge passage 21 to the outside, passes through the peripheral wall 19A, and is released toward the nitrifying bacteria N carried on the outside. The nitrifying bacteria N consumes the released oxygen, and the remaining oxygen that has not been consumed is released into the drainage receiving space S2 of the tank body 15 excluding the bacteria carrying device 16.

従って、チューブ１９の内部空間Ｓ１は、エアーポンプ１３から酸素が供給される酸素領域を構成し、槽本体１５の排水受容空間Ｓ２は、脱窒性リン蓄積細菌を含む排水が供給される排水領域を構成する。そして、周壁１９Ａは、酸素領域と排水領域とを区分する隔壁を構成する。   Therefore, the internal space S1 of the tube 19 constitutes an oxygen region to which oxygen is supplied from the air pump 13, and the drainage receiving space S2 of the tank body 15 is a drainage region to which wastewater containing denitrifying phosphorus accumulating bacteria is supplied. Configure. The peripheral wall 19A constitutes a partition that separates the oxygen region and the drainage region.

前記攪拌手段１７は、排水受容空間Ｓ２に配置された翼体１７Ａを図示しないモータ等で回転させることで、排水Ｈを攪拌可能とする構成となっているが、排水Ｈを攪拌可能な構成であれば何でも良い。   The stirring means 17 is configured to allow the drainage H to be stirred by rotating the wing body 17A disposed in the drainage receiving space S2 with a motor or the like (not shown). Anything is fine.

前記エアーポンプ１３は、酸素がチューブ１９から排水受容空間Ｓ２内に放出されたときに、排水Ｈ中の残存酸素濃度が０．５ｇ／ｍ３以下になるように、供給流量等が調整される。この調整は、排出管路２１中に設けた図示しない流量計等の流量に基づいてエアーポンプ１３の駆動が制御される。その他、溶存酸素濃度を測定可能なＤＯメータユニットを使って、排水中の溶存酸素濃度の計測値を基にして、エアーポンプ１３の駆動を制御してもよい。 The air pump 13 adjusts the supply flow rate and the like so that the residual oxygen concentration in the waste water H becomes 0.5 g / m 3 or less when oxygen is released from the tube 19 into the waste water receiving space S2. . In this adjustment, the driving of the air pump 13 is controlled based on the flow rate of a flow meter (not shown) provided in the discharge pipe 21. In addition, the driving of the air pump 13 may be controlled based on the measured value of the dissolved oxygen concentration in the waste water using a DO meter unit capable of measuring the dissolved oxygen concentration.

次に、排水処理装置１２を使った排水処理手順について説明する。なお、ここでは、排水処理装置１２を回分式の排水処理システムに適用している。   Next, a wastewater treatment procedure using the wastewater treatment device 12 will be described. Here, the waste water treatment device 12 is applied to a batch-type waste water treatment system.

有機物が含まれている排水Ｈが槽本体１５内に供給される。そして、先ず、嫌気工程が行われる。すなわち、エアーポンプ１３から細菌担持装置１６側への酸素の供給を停止した状態で、攪拌手段１７によって槽本体１５内の排水Ｈが所定時間攪拌される。この過程で、排水Ｈに含まれる脱窒性リン蓄積細菌により、有機物の取り込み及びリンの放出が行われる。   Waste water H containing organic matter is supplied into the tank body 15. First, an anaerobic process is performed. That is, the waste water H in the tank body 15 is stirred for a predetermined time by the stirring means 17 in a state where the supply of oxygen from the air pump 13 to the bacteria carrying device 16 side is stopped. In this process, organic matter is taken up and phosphorus is released by denitrifying phosphorus accumulating bacteria contained in the waste water H.

そして、エアーポンプ１３が作動し、各チューブ１９内に酸素が供給される。この酸素は、各チューブ１９の周壁１９Ａを透過し、その外周面側に担持された硝化細菌Ｎに優先的に供給され、当該硝化細菌Ｎの作用により、排水Ｈのアンモニア成分を硝酸態窒素に変える硝化反応が行われる。また、排水Ｈに含まれる脱窒性リン蓄積細菌によって、排水Ｈ中のリンが摂取され、同時に前述の硝化反応により生じた硝酸態窒素が窒素ガスに変換される。このとき、エアーポンプ１３から供給された酸素は、チューブ１９内の外側の硝化細菌Ｎに優先的に供給されて消費されるため、その僅かな残り分が、排水Ｈ中に溶存することになる。従って、脱窒性リン蓄積細菌は酸素に殆どさらされることがなく、酸素の存在による脱窒性リン蓄積細菌のリンの過剰吸収を抑制する有機物の添加が不要となり、当該有機物を添加しなくても、脱窒性リン蓄積細菌によって、リンの摂取と硝酸態窒素の変換とをバランス良く行うことができる。   Then, the air pump 13 is operated and oxygen is supplied into each tube 19. This oxygen permeates through the peripheral wall 19A of each tube 19 and is preferentially supplied to the nitrifying bacteria N carried on the outer peripheral surface side. By the action of the nitrifying bacteria N, the ammonia component of the waste water H is converted into nitrate nitrogen. A changing nitrification reaction takes place. Further, phosphorus in the wastewater H is ingested by the denitrifying phosphorus accumulating bacteria contained in the wastewater H, and at the same time, nitrate nitrogen generated by the nitrification reaction is converted into nitrogen gas. At this time, oxygen supplied from the air pump 13 is preferentially supplied to and consumed by the nitrifying bacteria N outside the tube 19, so that a small remaining amount is dissolved in the waste water H. . Therefore, denitrifying phosphorus accumulating bacteria are hardly exposed to oxygen, and it is not necessary to add an organic substance that suppresses excessive absorption of phosphorus in the denitrifying phosphorus accumulating bacteria due to the presence of oxygen. In addition, the denitrifying phosphorus accumulating bacteria can balance the intake of phosphorus and the conversion of nitrate nitrogen.

なお、前記排水処理装置１０を使って、上述のように排水Ｈからリンや硝酸態窒素を除去するのに要する時間は、従来のＡＯＡ法での所要時間と同程度になることが、実験の結果、立証されている。   It should be noted that the time required to remove phosphorus and nitrate nitrogen from the waste water H as described above using the waste water treatment apparatus 10 is about the same as the time required for the conventional AOA method. The result is proven.

次に、排水Ｈの溶存酸素が脱窒性リン蓄積細菌の窒素除去速度に与える影響を検証するための実験を行った。   Next, an experiment was conducted to verify the effect of dissolved oxygen in wastewater H on the nitrogen removal rate of denitrifying phosphorus accumulating bacteria.

図３に示されるように、本実験装置３０は、実験排水Ｈが入れられるビーカ３２と、このビーカ３２内の底壁３２Ａに設置され、磁性を帯びた攪拌子３３と、ビーカ３２の下に置かれ、攪拌子３３を磁力で回転させるスターラー３５と、ビーカ３２の外側に配置されたエアーポンプ３７と、ビーカ３２内に設置され、エアーポンプ３７からの酸素を実験排水Ｈに溶存する状態で曝気させる噴出ノズル３８と、実験排水Ｈの溶存酸素濃度を測定するＤＯメータユニット３９とを備えている。   As shown in FIG. 3, the present experimental apparatus 30 includes a beaker 32 into which experimental waste water H is put, a bottom wall 32 </ b> A in the beaker 32, a magnetic stir bar 33, and a beaker 32. A stirrer 35 that rotates the stirrer 33 by magnetic force, an air pump 37 disposed outside the beaker 32, and is installed in the beaker 32 so that oxygen from the air pump 37 is dissolved in the experimental waste water H. A jet nozzle 38 for aeration and a DO meter unit 39 for measuring the dissolved oxygen concentration of the experimental waste water H are provided.

前記実験装置３０に対して、次の手順で実験を行った。   An experiment was performed on the experimental apparatus 30 according to the following procedure.

全有機炭素濃度が１２０ｇ／ｍ３、アンモニア態窒素が３０ｇ／ｍ３、リン酸態リン濃度が１５ｇ／ｍ３となる模擬排水２５０ｍｌをビーカに入れた状態で、脱窒性リン蓄積細菌を含む汚泥懸濁液２５０ｍｌを加え、ＭＬＳＳ濃度が２０００ｇ／ｍ３となる実験排水Ｈを作成した。
そして、スターラー３５の作動によって攪拌子３３を回転させ、実験排水Ｈを嫌気条件下で２時間攪拌し、脱窒性リン蓄積細菌による有機物の取り込み及びリンの吐き出しを行わせた。その後、硝酸ナトリウムを添加し、実験排水Ｈの硝酸態窒素濃度を３０ｇ／ｍ３とした。そして、ＤＯメータユニット３９で実験排水Ｈの溶存酸素濃度を計測しながら、エアーポンプ３７から実験排水Ｈに供給される空気の流量を調整し、実験排水Ｈの溶存酸素濃度が、０ｇ／ｍ３、０．１ｇ／ｍ３、０．５ｇ／ｍ３、１．２ｇ／ｍ３、２．０ｇ／ｍ３、６．０ｇ／ｍ３の６種類について、窒素除去速度を計測した。この窒素除去速度は、硝酸態窒素とアンモニア態窒素それぞれについて、経過時間と濃度の関係を求め、各濃度を加えた上で、それらの初期２時間分を１次近似し、その傾き（濃度差／経過時間）を計算することにより求めた。その結果を図４に示す。 Contains denitrifying phosphorus-accumulating bacteria in a beaker with 250 ml of simulated waste water with a total organic carbon concentration of 120 g / m 3 , ammonia nitrogen of 30 g / m 3 , and phosphate phosphorus concentration of 15 g / m 3 250 ml of sludge suspension was added, and an experimental waste water H having an MLSS concentration of 2000 g / m 3 was created.
Then, the stirrer 33 was rotated by the operation of the stirrer 35, and the experimental waste water H was stirred for 2 hours under anaerobic conditions, and organic substances were taken up and discharged by denitrifying phosphorus accumulating bacteria. Thereafter, sodium nitrate was added to adjust the nitrate nitrogen concentration of the experimental waste water H to 30 g / m 3 . And while measuring the dissolved oxygen concentration of the experimental waste water H with the DO meter unit 39, the flow rate of the air supplied from the air pump 37 to the experimental waste water H is adjusted, and the dissolved oxygen concentration of the experimental waste water H is 0 g / m 3. , 0.1 g / m 3 , 0.5 g / m 3 , 1.2 g / m 3 , 2.0 g / m 3 , 6.0 g / m 3 , nitrogen removal rates were measured. This nitrogen removal rate is obtained by calculating the relationship between elapsed time and concentration for each of nitrate nitrogen and ammonia nitrogen, adding each concentration, and firstly approximating the initial 2 hours, and the slope (concentration difference) / Elapsed time). The result is shown in FIG.

図４によれば、残存酸素濃度が０．５ｇ／ｍ３以下の場合は、それを超える場合に比べ、窒素除去速度が格段に増大することが理解されるであろう。従って、排水処理槽１２中で、チューブ１９の外側の硝化細菌Ｎが消費仕切らずに、排水Ｈに溶存した酸素の濃度が０．５ｇ／ｍ３以下になったときに、排水処理上有用となる。 According to FIG. 4, it will be understood that when the residual oxygen concentration is 0.5 g / m 3 or less, the nitrogen removal rate is remarkably increased as compared with the case where the residual oxygen concentration is more than 0.5 g / m 3 . Therefore, when the concentration of oxygen dissolved in the waste water H becomes 0.5 g / m 3 or less in the waste water treatment tank 12 without the nitrifying bacteria N outside the tube 19 being consumed, it is useful for waste water treatment. Become.

なお、前記実施例では、排水処理装置１０を回分式の排水処理システムに適用した例を説明したが、排水処理装置１０を連続式の排水処理システムに適用することもできる。この場合は、嫌気工程を行う槽を別途設け、当該槽にて嫌気工程による処理終了後、その排水を排水処理槽１２に供給する構成となる。   In addition, although the example which applied the waste water treatment apparatus 10 to the batch type waste water treatment system was demonstrated in the said Example, the waste water treatment apparatus 10 can also be applied to a continuous waste water treatment system. In this case, the tank which performs an anaerobic process is provided separately, and it becomes the structure which supplies the wastewater to the waste water treatment tank 12 after the process by an anaerobic process is complete | finished in the said tank.

また、前記実施例では、上下方向に延びるチューブ１９を使っているが、本発明はこれに限らず、酸素を透過する隔壁を使って、酸素領域と排水領域を区分し、排水領域側の隔壁の面に硝化細菌を担持させる構成である限り、種々の構成を採用することができる。   Moreover, in the said Example, although the tube 19 extended in an up-down direction is used, this invention is not restricted to this, The oxygen area | region and the drainage area are divided using the partition which permeate | transmits oxygen, and the partition by the side of a drainage area As long as the nitrifying bacteria are supported on the surface, various configurations can be adopted.

その他、本発明における各部の構成は図示構成例に限定されるものではなく、実質的に同様の作用を奏する限りにおいて、種々の変更が可能である。   In addition, the structure of each part in this invention is not limited to the example of illustration structure, A various change is possible as long as there exists a substantially similar effect | action.

本実施例に係る排水処理装置の概略構成図。The schematic block diagram of the waste water treatment equipment which concerns on a present Example. 図１中Ａ部の拡大断面図。The expanded sectional view of the A section in FIG. 実験装置を示す概念図。The conceptual diagram which shows an experimental apparatus. 溶存酸素濃度と窒素除去速度との関係を示す図表。The chart which shows the relationship between dissolved oxygen concentration and nitrogen removal rate.

符号の説明Explanation of symbols

１０ 排水処理装置
１２ 排水処理槽
１３ エアーポンプ（酸素供給手段）
１５ 槽本体
１９Ａ 周壁（隔壁）
Ｈ 排水
Ｎ 硝化細菌
Ｓ１ 内部空間（酸素領域）
Ｓ２ 排水受容空間（排水領域） 10 Wastewater treatment equipment 12 Wastewater treatment tank 13 Air pump (oxygen supply means)
15 Tank body 19A Perimeter wall (partition wall)
H Wastewater N Nitrifying bacteria S1 Internal space (oxygen region)
S2 Drainage receiving space (drainage area)

Claims (1)

脱窒性リン蓄積細菌を含む排水が供給される排水領域と、この排水領域に対して隔壁で区分された酸素領域と、この酸素領域に酸素を供給する酸素供給手段とを備えた排水処理装置において、
前記隔壁は、前記酸素領域に供給された酸素を前記排水領域に透過可能にする構造をなすとともに、前記排水領域側の面に硝化細菌が担持され、
前記酸素供給手段は、前記隔壁を透過した酸素のうち前記硝化細菌で消費されずに前記排水領域内の排水中に溶存する酸素の濃度が０．５ｇ／ｍ ３ 以下になるように酸素を供給することを特徴とする排水処理装置。 A wastewater treatment apparatus comprising a drainage region to which wastewater containing denitrifying phosphorus-accumulating bacteria is supplied, an oxygen region partitioned by a partition wall from the drainage region, and an oxygen supply means for supplying oxygen to the oxygen region In
The septum oxygen supplied to the oxygen region with forming a structure that transparently available to the drainage area, nitrifying bacteria is carried on the surface of the drainage area side,
The oxygen supply means supplies oxygen so that a concentration of oxygen dissolved in the wastewater in the drainage region is 0.5 g / m 3 or less without being consumed by the nitrifying bacteria among oxygen permeated through the partition wall. A wastewater treatment apparatus characterized by that.
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Publication number Priority date Publication date Assignee Title
JPH1085787A (en) * 1996-09-10 1998-04-07 Suido Kiko Kaisha Ltd Method and apparatus for nitrification-denitrification treatment.
JPH11333496A (en) * 1998-05-22 1999-12-07 Nissin Electric Co Ltd Microorganism carrier for denitrification
JP2000218290A (en) * 1999-02-01 2000-08-08 Kitakyushu City Sewage treatment and sewage treating device
JP2003211185A (en) * 2002-01-25 2003-07-29 Hiroshima Pref Gov Powerless wastewater treatment method
JP2003251381A (en) * 2002-02-28 2003-09-09 Asahi Kasei Corp Nitrogen removing method by membrane bioreactor
JP2003285096A (en) * 2002-03-28 2003-10-07 Univ Waseda Simultaneous denitrification and dephosphorization type treatment method for wastewater
JP2004130249A (en) * 2002-10-11 2004-04-30 Mitsubishi Rayon Co Ltd Biological dephosphorization accelerating method in anaerobic-aerobic circulation activated sludge treatment method
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