JP2001314890A - Wastewater treatment method - Google Patents
Wastewater treatment methodInfo
- Publication number
- JP2001314890A JP2001314890A JP2000137559A JP2000137559A JP2001314890A JP 2001314890 A JP2001314890 A JP 2001314890A JP 2000137559 A JP2000137559 A JP 2000137559A JP 2000137559 A JP2000137559 A JP 2000137559A JP 2001314890 A JP2001314890 A JP 2001314890A
- Authority
- JP
- Japan
- Prior art keywords
- tank
- denitrification
- aeration
- sludge
- returned
- 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.)
- Granted
Links
Classifications
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Activated Sludge Processes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は廃水の処理方法に係
り、特に、廃水を活性汚泥の存在下にリン放出工程、脱
窒工程及び曝気工程の順に通水し、該曝気工程の混合液
中に浸漬された分離膜により処理水を分離する廃水の処
理方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for treating wastewater, and more particularly, to passing wastewater in the order of a phosphorus release step, a denitrification step and an aeration step in the presence of activated sludge, and The present invention relates to a method for treating wastewater in which treated water is separated by a separation membrane immersed in water.
【０００２】[0002]
【従来の技術】従来、廃水中のＢＯＤ、窒素及びリンを
除去する方法として、嫌気槽と好気槽とを組み合せ、廃
水を嫌気槽、脱窒槽、好気槽及び沈殿槽の順に通水する
と共に、沈殿槽で分離された汚泥の一部を嫌気槽に返送
し、かつ好気槽処理液の一部を脱窒槽に返送して、廃水
中のＢＯＤ成分、窒素成分及びリン成分を生物学的に除
去する方法が知られている。2. Description of the Related Art Conventionally, as a method for removing BOD, nitrogen and phosphorus in wastewater, an anaerobic tank and an aerobic tank are combined, and the wastewater is passed through an anaerobic tank, a denitrification tank, an aerobic tank, and a sedimentation tank in this order. At the same time, a part of the sludge separated in the sedimentation tank is returned to the anaerobic tank, and a part of the aerobic tank treatment liquid is returned to the denitrification tank, and the BOD component, nitrogen component and phosphorus component in the wastewater are biologically analyzed. There is known a method of removing the water.
【０００３】この方法において、廃水は、まず嫌気槽に
て嫌気処理され、ＢＯＤ成分が微生物に取り込まれると
共に、リン化合物が加水分解されてリン（正リン酸）が
放出される。嫌気槽の処理液は次いで脱窒槽で脱窒処理
（硝酸イオン及び亜硝酸イオンの窒素ガスへの還元処
理）される。更に、脱窒槽処理液は、好気槽において好
気処理され、微生物によるアンモニアの硝化と正リン酸
の取り込みが行われる。その後、好気槽処理液は沈殿槽
にてリンを含む汚泥と、処理水とに分離される。In this method, wastewater is first anaerobically treated in an anaerobic tank, BOD components are taken in by microorganisms, and phosphorus compounds are hydrolyzed to release phosphorus (orthophosphoric acid). The treatment liquid in the anaerobic tank is then subjected to a denitrification treatment (reduction treatment of nitrate ions and nitrite ions to nitrogen gas) in a denitrification tank. Further, the denitrification tank treatment liquid is subjected to aerobic treatment in an aerobic tank, and nitrification of ammonia and uptake of orthophosphoric acid by microorganisms are performed. Thereafter, the aerobic tank treatment liquid is separated in the sedimentation tank into sludge containing phosphorus and treated water.
【０００４】しかし、この固液分離に沈殿槽を採用した
ものでは、好気槽の汚泥濃度を高くすることができな
い；汚泥の沈降不良で処理水側への汚泥のリークの問題
がある；装置の小型化が図れない；といった欠点があ
る。このため、特開平９−４７７８１号公報には、沈殿
槽の代りに浸漬膜を用いて固液分離を行う方法として、
廃水を嫌気槽に導入し、嫌気槽処理液を曝気槽に導入
し、曝気槽内に浸漬された分離膜により処理水を分離す
ると共に、この曝気槽内液を嫌気槽に返送する方法が記
載されている。この方法では、沈殿槽を不要とし、曝気
槽の汚泥を高く維持して効率的な処理を行うと共に、汚
泥を確実に分離することができる。However, in the case where a sedimentation tank is employed for the solid-liquid separation, the sludge concentration in the aerobic tank cannot be increased; there is a problem of sludge leakage to the treated water side due to poor sedimentation of the sludge; Cannot be miniaturized; For this reason, Japanese Patent Application Laid-Open No. 9-47781 discloses a method of performing solid-liquid separation using an immersion membrane instead of a precipitation tank.
A method is described in which wastewater is introduced into an anaerobic tank, anaerobic tank treatment liquid is introduced into an aeration tank, treated water is separated by a separation membrane immersed in the aeration tank, and the liquid in the aeration tank is returned to the anaerobic tank. Have been. According to this method, the sludge in the aeration tank can be maintained at a high level, and the sludge can be surely separated while eliminating the need for the sedimentation tank.
【０００５】[0005]
【発明が解決しようとする課題】しかしながら、特開平
９−４７７８１号公報に記載される方法では、酸素と硝
酸及び亜硝酸性窒素を含む曝気槽内液を嫌気槽に返送す
るため、嫌気槽をリン放出条件、即ち、無酸素、無ＮＯ
ｘ状態に維持することができず、この結果、嫌気槽にお
いて脱窒は起こるが、リンの放出は期待できないという
問題がある。However, in the method described in Japanese Patent Application Laid-Open No. 9-47781, the anaerobic tank is required to return the liquid in the aeration tank containing oxygen, nitric acid and nitrite nitrogen to the anaerobic tank. Phosphorus release conditions, i.e., no oxygen, no NO
x state cannot be maintained, and as a result, denitrification occurs in the anaerobic tank, but there is a problem that release of phosphorus cannot be expected.
【０００６】即ち、生物学的リン除去において、嫌気槽
で十分なリン放出が行われることが必要であり、このた
めに、嫌気槽のＭＬＳＳ濃度は十分高くする必要があ
る。従って、浸漬膜を用いた活性汚泥法では、嫌気槽の
ＭＬＳＳを高くするためには、浸漬膜槽からの汚泥返送
率を十分高くしなければならない。例えば、浸漬膜槽の
ＭＬＳＳが１００００ｍｇ／Ｌと仮定すると、汚泥返送
率５０％では、嫌気槽のＭＬＳＳは３３００ｍｇ／Ｌに
しかならない。この汚泥返送率を３００％に上げること
ができれば、ＭＬＳＳは７５００ｍｇ／Ｌとなり、その
分、嫌気槽は小型化できるが、このように汚泥返送率を
上げると、返送汚泥中に含まれるＮＯＸの影響で嫌気槽
においてリンの放出が起こらなくなる。[0006] That is, in biological phosphorus removal, it is necessary to sufficiently release phosphorus in an anaerobic tank, and for this purpose, the MLSS concentration in the anaerobic tank needs to be sufficiently high. Therefore, in the activated sludge method using a submerged membrane, the sludge return rate from the submerged membrane tank must be sufficiently high in order to increase the MLSS in the anaerobic tank. For example, assuming that the MLSS of the immersion membrane tank is 10,000 mg / L, the MLSS of the anaerobic tank is only 3300 mg / L at a sludge return rate of 50%. If it is possible to increase the sludge return rate 300%, MLSS is 7500 mg / L, and the correspondingly, although anaerobic tank can be downsized, in this way increase the sludge return rate, of the NO X contained in the return sludge As a result, phosphorus release does not occur in the anaerobic tank.
【０００７】本発明は上記従来の問題点を解決し、廃水
を活性汚泥の存在下にリン放出工程、脱窒工程及び曝気
工程の順に通水し、浸漬膜による固液分離で処理水を得
る方法において、効率的な脱窒、脱リン、脱ＢＯＤを行
って高水質の処理水を得ることができる廃水の処理方法
を提供することを目的とする。The present invention solves the above-mentioned conventional problems, and passes wastewater in the order of a phosphorus release step, a denitrification step, and an aeration step in the presence of activated sludge to obtain treated water by solid-liquid separation using an immersion membrane. It is an object of the present invention to provide a method for treating wastewater capable of obtaining high-quality treated water by performing efficient denitrification, dephosphorization, and BOD removal.
【０００８】[0008]
【課題を解決するための手段】本発明の廃水の処理方法
は、廃水を活性汚泥の存在下にリン放出工程、脱窒工程
及び曝気工程の順に通水し、該曝気工程の混合液中に浸
漬された分離膜により処理水を分離する廃水の処理方法
であって、該曝気工程の混合液の一部を前記脱窒工程へ
返送すると共に、前記脱窒工程の混合液をリン放出工程
へ返送することを特徴とする。According to the method for treating wastewater of the present invention, the wastewater is passed in the order of a phosphorus release step, a denitrification step, and an aeration step in the presence of activated sludge, and the wastewater is mixed with the mixture in the aeration step. A method of treating wastewater in which treated water is separated by a immersed separation membrane, wherein a part of the mixed solution in the aeration step is returned to the denitrification step, and the mixed solution in the denitrification step is transferred to a phosphorus release step. It will be returned.
【０００９】本発明では、曝気工程の混合液を脱窒工程
に、脱窒工程の混合液をリン放出工程にそれぞれ返送す
ることにより汚泥の返送を行うため、リン放出工程に
は、脱窒工程において脱窒処理され硝酸性窒素、亜硝酸
性窒素を含まず、酸素が消費された混合液が導入される
こととなり、リン放出工程をリンの放出条件である無Ｎ
Ｏｘ及び無酸素状態に保つことが可能となる。このた
め、このリン放出工程において、リン化合物が正リン酸
として効率的に放出され、この正リン酸が後段の曝気工
程において汚泥に取り込まれることにより、リンを高度
に除去することが可能となる。In the present invention, the sludge is returned by returning the mixture in the aeration step to the denitrification step and the mixture in the denitrification step to the phosphorus release step. In this case, a mixed solution denitrified and containing no nitrate nitrogen and nitrite nitrogen and consuming oxygen is introduced.
Ox and anoxic conditions can be maintained. Therefore, in this phosphorus releasing step, the phosphorus compound is efficiently released as orthophosphoric acid, and this orthophosphoric acid is taken into sludge in the subsequent aeration step, whereby phosphorus can be highly removed. .
【００１０】本発明においては、特に、脱窒工程を前段
とそれに続く後続段とで構成し、曝気工程の混合液の一
部を脱窒工程の前段へ返送し、かつ脱窒工程の後段の混
合液を嫌気工程へ返送することが好ましく、また、曝気
工程も前段とそれに続く後続段とで構成し、分離膜を曝
気工程の最終段に浸漬し、最終段の混合液の一部を、脱
窒工程の前段へ返送することが好ましい。In the present invention, in particular, the denitrification step is constituted by a former stage and a succeeding stage, and a part of the mixed solution in the aeration process is returned to the former stage of the denitrification process, and the second stage is provided in the latter stage of the denitrification process. It is preferable that the mixed solution is returned to the anaerobic step, and the aeration step also includes a former stage and a succeeding stage, and the separation membrane is immersed in the last stage of the aeration process, and a part of the mixed solution in the final stage is It is preferable to return to the preceding stage of the denitrification step.
【００１１】即ち、脱窒工程を２段以上の複数段に設
け、前段の脱窒工程に曝気工程から返送される混合液を
導入することにより、好気条件の曝気工程からの返送液
の導入による影響を前段の脱窒工程で緩和して、後続段
の脱窒工程で良好な嫌気条件のもとに、脱窒を効率的に
進行させることが可能となる。In other words, the denitrification step is provided in two or more stages, and the mixed liquid returned from the aeration step is introduced into the preceding denitrification step, thereby introducing the return liquid from the aeration step under aerobic conditions. In the subsequent denitrification step, the effect of the denitrification can be mitigated in the preceding denitrification step, and denitrification can proceed efficiently under favorable anaerobic conditions.
【００１２】また、更に、曝気工程を２段以上の複数段
に設け、最終段の曝気工程に分離膜を浸漬し、この最終
段の混合液を脱窒工程に返送することにより、高い窒素
除去率を得ることができる。Further, a high aeration removal step is provided in two or more stages, a separation membrane is immersed in the last stage aeration process, and the final mixed solution is returned to the denitrification process. Rate can be obtained.
【００１３】[0013]
【発明の実施の形態】以下に図面を参照して本発明の実
施の形態を詳細に説明する。Embodiments of the present invention will be described below in detail with reference to the drawings.
【００１４】図１〜３は本発明の廃水の処理方法の実施
の形態を示す系統図である。図１〜３において同一機能
を奏する部材には同一符号を付してある。1 to 3 are system diagrams showing an embodiment of the method for treating wastewater of the present invention. In FIGS. 1 to 3, members having the same function are denoted by the same reference numerals.
【００１５】図１の廃水の処理方法では、原水を配管１
１より嫌気槽（リン放出槽）１、脱窒槽２及び曝気管５
を備える曝気槽３に順次通水して処理し、曝気槽３内に
浸漬された分離膜４で分離された透過水を配管１２より
処理水として系外へ排出する。曝気槽３内の液は、ポン
プＰ２により配管１３を経て脱窒槽２に返送する。ま
た、脱窒槽２内の液はポンプＰ１により配管１４を経て
嫌気槽１に返送する。曝気槽３からは、配管１５より適
宜余剰汚泥として槽内液が引き抜かれる。In the method for treating wastewater shown in FIG.
Anaerobic tank (phosphorus release tank) 1, denitrification tank 2, and aeration tube 5
The permeated water separated by the separation membrane 4 immersed in the aeration tank 3 is discharged out of the system as a treated water from a pipe 12. The liquid in the aeration tank 3 is returned to the denitrification tank 2 via the pipe 13 by the pump P2. The liquid in the denitrification tank 2 through the pipe 14 to return to the anaerobic tank 1 by the pump P 1. From the aeration tank 3, the liquid in the tank is withdrawn as appropriate from the pipe 15 as excess sludge.
【００１６】この方法では、原水は、まず、嫌気槽１で
脱窒槽２からの返送汚泥を受けて、効率的に嫌気処理さ
れ、ＢＯＤ成分が除去されると共に、リン（正リン酸）
の放出が行われる。この嫌気処理液は、次いで脱窒槽２
内で曝気槽３からの返送汚泥を受けて効率的に脱窒処理
され窒素が除去される。この脱窒処理液は更に曝気槽３
で好気処理され、ＢＯＤの好気分解と、アンモニア性窒
素の硝化とリンの汚泥中への取り込みが行われる。従っ
て、この曝気槽３内の液を分離膜４で膜分離することに
より、ＢＯＤ成分、窒素成分及びリン成分が高度に除去
された処理水を得ることができる。また、曝気槽３から
は、リンを高濃度に取り込んだ汚泥を引き抜くことがで
きる。In this method, the raw water is first subjected to the sludge returned from the denitrification tank 2 in the anaerobic tank 1 and is efficiently subjected to anaerobic treatment to remove the BOD component and to remove phosphorus (normal phosphoric acid).
Is released. This anaerobic treatment liquid is then supplied to the denitrification tank 2
Inside, the sludge returned from the aeration tank 3 is efficiently denitrified and nitrogen is removed. This denitrification treatment liquid is further supplied to the aeration tank 3
And aerobic decomposition of BOD, nitrification of ammonia nitrogen, and incorporation of phosphorus into sludge. Therefore, by subjecting the liquid in the aeration tank 3 to membrane separation by the separation membrane 4, it is possible to obtain treated water from which the BOD component, the nitrogen component and the phosphorus component have been highly removed. Further, sludge containing phosphorus at a high concentration can be extracted from the aeration tank 3.
【００１７】このような処理において、本発明では処理
水の固液分離を分離膜４で行うため、大面積を要する沈
殿槽が不要となり、また、曝気槽３内の汚泥濃度を高く
維持して好気処理効率を高めることができる。また曝気
槽３内の汚泥混合液を脱窒槽２に返送することで脱窒槽
２内の汚泥濃度を高く維持すると共に、脱窒槽２におい
て、曝気槽３で硝化された硝酸性窒素、亜硝酸性窒素を
効率的に脱窒処理することができる。更に、脱窒槽２内
の汚泥混合液を嫌気槽１に返送することで嫌気槽１内の
汚泥濃度を高く維持して効率的な嫌気処理を行えるが、
この際、返送される汚泥混合液は、脱窒槽２内で硝酸性
窒素、亜硝酸性窒素が除去されると共に酸素が消費され
た液であるため、嫌気処理におけるリン放出阻害を受け
ることなく、効率的なリンの加水分解を行える。In such a treatment, in the present invention, since the solid-liquid separation of the treated water is performed by the separation membrane 4, a sedimentation tank requiring a large area becomes unnecessary, and the sludge concentration in the aeration tank 3 is maintained at a high level. Aerobic treatment efficiency can be increased. In addition, the sludge mixture in the aeration tank 3 is returned to the denitrification tank 2 to maintain the sludge concentration in the denitrification tank 2 high. Nitrogen can be efficiently denitrified. Further, by returning the sludge mixture in the denitrification tank 2 to the anaerobic tank 1, the sludge concentration in the anaerobic tank 1 can be maintained at a high level, and efficient anaerobic treatment can be performed.
At this time, the returned sludge mixed liquid is a liquid from which nitrate nitrogen and nitrite nitrogen are removed and oxygen is consumed in the denitrification tank 2, so that the sludge mixture is not hindered by the phosphorus release in the anaerobic treatment. Efficient phosphorus hydrolysis can be performed.
【００１８】図２の方法は、脱窒槽を第１脱窒槽２Ａと
第２脱窒槽２Ｂとに２段に設け、曝気槽３からの汚泥混
合液を第１脱窒槽２Ａに返送し、第２脱窒槽２Ｂ内の汚
泥混合液を嫌気槽１に返送した点が図１に示す方法と異
なり、その他は同様に処理が行われる。In the method shown in FIG. 2, a denitrification tank is provided in two stages, a first denitrification tank 2A and a second denitrification tank 2B, and the mixed sludge from the aeration tank 3 is returned to the first denitrification tank 2A, The point that the mixed sludge liquid in the denitrification tank 2B is returned to the anaerobic tank 1 is different from the method shown in FIG.
【００１９】この方法では、脱窒槽を２段階とし、曝気
槽３からの汚泥混合液を前段の第１脱窒槽２Ａに返送す
ることで、曝気槽３からの汚泥混合液の好気条件が第１
脱窒槽２Ａで緩和され、第２脱窒槽２Ｂにおいてより一
層高度な脱窒処理を行うことができるため、処理水質の
向上を図ることができる。また、この場合において、脱
窒が進行した第２脱窒槽２Ｂ内の汚泥混合液を嫌気槽１
に返送することで、嫌気槽１内への硝酸性窒素、亜硝酸
性窒素や酸素の流入を確実に防止して、より一層効率的
なリンの放出を行える。In this method, the denitrification tank is divided into two stages, and the sludge mixed liquid from the aeration tank 3 is returned to the first denitrification tank 2A in the preceding stage, whereby the aerobic condition of the sludge mixed liquid from the aeration tank 3 is changed. 1
Since the denitrification is alleviated in the denitrification tank 2A and the denitrification treatment can be performed in the second denitrification tank 2B, the quality of the treated water can be improved. Further, in this case, the sludge mixed liquid in the second denitrification tank 2B in which the denitrification has progressed is transferred to the anaerobic tank 1
In this way, the inflow of nitrate nitrogen, nitrite nitrogen and oxygen into the anaerobic tank 1 is reliably prevented, and phosphorus can be more efficiently released.
【００２０】図３の方法は、曝気槽を曝気管５Ａを備え
る第１曝気槽３Ａと曝気管５Ｂを備える第２曝気槽３Ｂ
とに２段に設け、後段の第２曝気槽３Ｂ内に分離膜４を
浸漬して処理水を取り出し、この第２曝気槽３Ｂ内の汚
泥混合液を第１脱窒槽２Ａに返送すると共に、第２曝気
槽３Ｂから余剰汚泥を引き出すようにした点が図２に示
す方法と異なり、その他は同様に処理が行われる。The method shown in FIG. 3 includes a first aeration tank 3A having an aeration tube 5A and a second aeration tank 3B having an aeration tube 5B.
The separation membrane 4 is immersed in the second aeration tank 3B at the subsequent stage, and the treated water is taken out. The sludge mixture in the second aeration tank 3B is returned to the first denitrification tank 2A. The method differs from the method shown in FIG. 2 in that excess sludge is drawn out from the second aeration tank 3B, and the other processes are performed similarly.
【００２１】この方法では曝気槽を２段階とし、前段の
第１曝気槽３Ａを主にＢＯＤ分解槽として機能させ、後
段の第２曝気槽３Ｂを主に硝化槽として機能させ、後段
の第２曝気槽３Ｂ内の汚泥混合液を第１脱窒槽２Ａに返
送することにより高い硝化率を得ることができる。ま
た、このように好気処理が進行した第２曝気槽３Ｂ内の
液を膜分離して処理水を取り出すことにより、高水質の
処理水を得ることができる。更に、この第２曝気槽３Ｂ
からは、余剰汚泥として、十分にリンを取り込んだ汚泥
を抜き出すことができる。In this method, the aeration tank has two stages, the first aeration tank 3A in the former stage mainly functions as a BOD decomposition tank, the second aeration tank 3B in the latter stage mainly functions as a nitrification tank, and the second stage in the second stage. By returning the sludge mixture in the aeration tank 3B to the first denitrification tank 2A, a high nitrification rate can be obtained. In addition, high-quality treated water can be obtained by membrane-separating the liquid in the second aeration tank 3B that has undergone the aerobic treatment as described above and extracting treated water. Further, the second aeration tank 3B
Can extract sludge that has sufficiently taken in phosphorus as surplus sludge.
【００２２】本発明において、曝気槽から脱窒槽への混
合液の返送量には、特に制限はないが、脱窒槽の混合液
を嫌気槽（リン放出槽）に返送するに当り、十分なリン
放出が起こるように、脱窒反応が進行し液中のリンを十
分に摂取した後の混合液とすることが望ましい。このた
め、曝気液（硝化液）の脱窒槽への返送率は１００％以
上、好ましくは１５０％以上とする。In the present invention, the amount of the mixed solution returned from the aeration tank to the denitrification tank is not particularly limited. However, when the mixed solution in the denitrification tank is returned to the anaerobic tank (phosphorus release tank), sufficient phosphorus is returned. It is desirable to prepare a mixed solution after the denitrification reaction has progressed and phosphorus in the solution has been sufficiently ingested so that release occurs. For this reason, the rate of returning the aerated liquid (nitrified liquid) to the denitrification tank is 100% or more, and preferably 150% or more.
【００２３】また、本発明において、脱窒槽から嫌気槽
への汚泥混合液の返送量にも特に制限はないが、一般的
には原水流量に対して１５０％以上が処理効率の面で好
ましい。In the present invention, the amount of the sludge mixed solution returned from the denitrification tank to the anaerobic tank is not particularly limited, but generally 150% or more of the raw water flow rate is preferable in terms of treatment efficiency.
【００２４】なお、曝気槽に浸漬する分離膜としては特
に制限はなく、形状は中空糸膜でも平膜でもよく、精密
濾過（ＭＦ）膜や限外濾過（ＵＦ）膜等を用いることが
できる。The separation membrane immersed in the aeration tank is not particularly limited, and may be a hollow fiber membrane or a flat membrane, and may be a microfiltration (MF) membrane or an ultrafiltration (UF) membrane. .
【００２５】図示の方法はいずれも本発明の一実施例で
あって、本発明はその要旨を超えない限り、何ら図示の
方法に限定されるものではない。The illustrated methods are all examples of the present invention, and the present invention is not limited to the illustrated methods unless it exceeds the gist.
【００２６】例えば、脱窒槽や曝気槽は２槽に限らず３
層以上設け、これを直列に配設したものであっても良
い。また、曝気槽のみを複数槽とし、脱窒槽を単槽とし
ても良い。いずれの場合においても、最終段の曝気槽の
汚泥混合液を脱窒槽に返送し、この最終段の曝気槽に分
離膜を浸漬して処理水を分離すると共に余剰汚泥を引き
抜くのが好ましい。また、曝気槽から返送される汚泥混
合液は、最前段の脱窒槽に導入し、最終段の脱窒槽の汚
泥混合液を嫌気槽に返送するのが好ましい。更に、嫌気
槽についても２槽又は３槽以上の槽を直列に配設しても
良い。この場合には、脱窒槽から返送される汚泥混合液
は最前段の嫌気槽に導入するのが好ましい。For example, the number of denitrification tanks and aeration tanks is not limited to two but three.
Layers or more may be provided and these may be arranged in series. Alternatively, the aeration tank alone may be a plurality of tanks, and the denitrification tank may be a single tank. In any case, it is preferable to return the sludge mixture in the final aeration tank to the denitrification tank, immerse the separation membrane in the final aeration tank to separate the treated water, and to pull out excess sludge. Further, it is preferable that the sludge mixed liquid returned from the aeration tank is introduced into the foremost denitrification tank, and the sludge mixed liquid from the final denitrification tank is returned to the anaerobic tank. Further, as for the anaerobic tank, two tanks or three or more tanks may be arranged in series. In this case, it is preferable that the sludge mixed liquid returned from the denitrification tank is introduced into the forefront anaerobic tank.
【００２７】このような本発明の廃水の処理方法は、各
種産業廃水の処理に極めて有効である。The wastewater treatment method of the present invention is extremely effective for treating various industrial wastewaters.
【００２８】[0028]
【実施例】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。The present invention will be described more specifically below with reference to examples and comparative examples.
【００２９】実施例１ 下記水質の廃水を原水として図１に示す方法に従って処
理し、得られた処理水の水質を表１に示した。 （原水水質） ＢＯＤ ：２５０ｍｇ／Ｌ リン ： ５ｍｇ／Ｌ アンモニア： ４０ｍｇ／Ｌ 原水流量、各槽の滞留時間、汚泥混合液返送量等の処理
条件は下記の通りとした。 ［処理条件］ 原水流量 ：１．０Ｌ／ｈｒ 嫌気槽滞留時間：１．０ｈｒ 脱窒槽滞留時間：３．０ｈｒ 曝気槽滞留時間：３．０ｈｒ 曝気槽内汚泥混合液の脱窒槽への返送量：４．０Ｌ／ｈ
ｒ 脱窒槽内汚泥混合液の嫌気槽への返送量：４．０Ｌ／ｈ
ｒ 曝気槽からの余剰汚泥引抜き量：１００ｍＬ／ｄａｙExample 1 Wastewater having the following water quality was treated as raw water in accordance with the method shown in FIG. 1, and the quality of the obtained treated water is shown in Table 1. (Raw water quality) BOD: 250 mg / L Phosphorus: 5 mg / L Ammonia: 40 mg / L Treatment conditions such as the flow rate of raw water, the residence time in each tank, and the amount of sludge mixed solution returned are as follows. [Treatment conditions] Raw water flow rate: 1.0 L / hr Anaerobic tank residence time: 1.0 hr Denitrification tank residence time: 3.0 hr Aeration tank residence time: 3.0 hr Return amount of sludge mixed solution in the aeration tank to the denitrification tank: 4.0L / h
r Return amount of the sludge mixture in the denitrification tank to the anaerobic tank: 4.0 L / h
r Excess sludge withdrawn from the aeration tank: 100 mL / day
【００３０】実施例２ 図２に示す如く、脱窒槽を２段に設け、曝気槽内汚泥混
合液を第１脱窒槽へ返送し、第２脱窒槽内汚泥混合液を
嫌気槽に返送したこと以外は実施例１と同様にして処理
を行い、得られた処理水の水質を表１に示した。なお、
第１脱窒槽の滞留時間は１．５ｈｒ，第２脱窒槽の滞留
時間は１．５ｈｒとした。Example 2 As shown in FIG. 2, a denitrification tank was provided in two stages, the sludge mixture in the aeration tank was returned to the first denitrification tank, and the sludge mixture in the second denitrification tank was returned to the anaerobic tank. Other than the above, the treatment was carried out in the same manner as in Example 1, and the quality of the obtained treated water is shown in Table 1. In addition,
The residence time in the first denitrification tank was 1.5 hr, and the residence time in the second denitrification tank was 1.5 hr.
【００３１】実施例３ 図３に示す如く、曝気槽を２段に設け、第２曝気槽内汚
泥混合液を第１脱窒槽に返送し、この第２曝気槽から処
理水、余剰汚泥を取り出したこと以外は実施例２と同様
にして処理を行い、得られた処理水の水質を表１に示し
た。なお、第１曝気槽の滞留時間は１．５ｈｒ，第２曝
気槽の滞留時間は１．５ｈｒとした。Example 3 As shown in FIG. 3, an aeration tank was provided in two stages, and the sludge mixture in the second aeration tank was returned to the first denitrification tank, and treated water and excess sludge were taken out of the second aeration tank. The treatment was carried out in the same manner as in Example 2 except for this, and the quality of the obtained treated water is shown in Table 1. The residence time in the first aeration tank was 1.5 hr, and the residence time in the second aeration tank was 1.5 hr.
【００３２】比較例１ 実施例１において、曝気槽内汚泥混合液を脱窒槽ではな
く、嫌気槽に返送し、脱窒槽から嫌気槽への汚泥混合液
の返送を行わなかったこと以外は同様にして処理を行
い、得られた処理水の水質を表１に示した。Comparative Example 1 In Example 1, the sludge mixture in the aeration tank was returned to the anaerobic tank instead of the denitrification tank, and the sludge mixture was not returned from the denitrification tank to the anaerobic tank. Table 1 shows the quality of the obtained treated water.
【００３３】[0033]
【表１】 [Table 1]
【００３４】表１より明らかなように、曝気槽内汚泥混
合液を嫌気槽に返送する比較例１では、嫌気槽において
リンの放出が行われないために、リンが十分に除去し得
ず、またＢＯＤも劣るものとなる。As is clear from Table 1, in Comparative Example 1 in which the sludge mixture in the aeration tank was returned to the anaerobic tank, phosphorus was not released in the anaerobic tank, so that phosphorus could not be sufficiently removed. Also, the BOD will be inferior.
【００３５】これに対して、曝気槽内汚泥混合液を脱窒
槽に返送し、脱窒槽内汚泥混合液を嫌気槽に返送する実
施例１であれば良好な処理水が得られる。特に、脱窒槽
を２段に設けた実施例２では、リン除去が良好である。
更に、曝気槽をも２段に設けた実施例３ではリン除去も
窒素除去も良好である。On the other hand, in Example 1, where the sludge mixture in the aeration tank is returned to the denitrification tank and the sludge mixture in the denitrification tank is returned to the anaerobic tank, good treated water can be obtained. In particular, in Example 2 in which the denitrification tanks were provided in two stages, the phosphorus removal was good.
Furthermore, in Example 3 in which the aeration tank was also provided in two stages, both phosphorus removal and nitrogen removal were good.
【００３６】[0036]
【発明の効果】以上詳述した通り、本発明の廃水の処理
方法によれば、各種産業廃水から、ＢＯＤ成分、リン成
分及び窒素成分を効率的に除去して高水質の処理水を得
ることができる。As described above in detail, according to the method for treating wastewater of the present invention, high-quality treated water can be obtained by efficiently removing BOD components, phosphorus components and nitrogen components from various industrial wastewaters. Can be.
【図１】本発明の廃水の処理方法の実施の形態を示す系
統図である。FIG. 1 is a system diagram showing an embodiment of a method for treating wastewater of the present invention.
【図２】本発明の廃水の処理方法の他の実施の形態を示
す系統図である。FIG. 2 is a system diagram showing another embodiment of the wastewater treatment method of the present invention.
【図３】本発明の廃水の処理方法の別の実施の形態を示
す系統図である。FIG. 3 is a system diagram showing another embodiment of the method for treating wastewater of the present invention.
１ 嫌気槽 ２ 脱窒槽 ２Ａ 第１脱窒槽 ２Ｂ 第２脱窒槽 ３ 曝気槽 ３Ａ 第１曝気槽 ３Ｂ 第２曝気槽 ４ 分離膜 ５，５Ａ，５Ｂ 曝気管 DESCRIPTION OF SYMBOLS 1 Anaerobic tank 2 Denitrification tank 2A 1st denitrification tank 2B 2nd denitrification tank 3 Aeration tank 3A 1st aeration tank 3B 2nd aeration tank 4 Separation membrane 5,5A, 5B Aeration tube
Claims (3)
程、脱窒工程及び曝気工程の順に通水し、該曝気工程の
混合液中に浸漬された分離膜により処理水を分離する廃
水の処理方法であって、 該曝気工程の混合液の一部を前記脱窒工程へ返送すると
共に、前記脱窒工程の混合液をリン放出工程へ返送する
ことを特徴とする廃水の処理方法。Claims: 1. A wastewater in which wastewater is passed in the order of a phosphorus release step, a denitrification step, and an aeration step in the presence of activated sludge, and treated water is separated by a separation membrane immersed in a mixed solution in the aeration step. A method for treating wastewater, comprising: returning a part of the mixed solution in the aeration step to the denitrification step, and returning the mixed solution in the denitrification step to the phosphorus release step.
とそれに続く後続段とからなり、前記曝気工程の混合液
の一部を該脱窒工程の前段へ返送することを特徴とする
廃水の処理方法。2. The wastewater according to claim 1, wherein the denitrification step comprises a former stage and a succeeding stage, and a part of the mixed solution in the aeration step is returned to the former stage of the denitrification step. Processing method.
が前段とそれに続く後続段とからなり、前記分離膜は該
曝気工程の最終段に浸漬されており、該最終段の混合液
の一部を、前記脱窒工程へ返送することを特徴とする廃
水の処理方法。3. The aeration step according to claim 1, wherein the aeration step includes a preceding step and a succeeding step, wherein the separation membrane is immersed in a last step of the aeration step, A wastewater treatment unit, wherein the wastewater is returned to the denitrification step.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000137559A JP4742403B2 (en) | 2000-05-10 | 2000-05-10 | Wastewater treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000137559A JP4742403B2 (en) | 2000-05-10 | 2000-05-10 | Wastewater treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2001314890A true JP2001314890A (en) | 2001-11-13 |
| JP4742403B2 JP4742403B2 (en) | 2011-08-10 |
Family
ID=18645315
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2000137559A Expired - Fee Related JP4742403B2 (en) | 2000-05-10 | 2000-05-10 | Wastewater treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP4742403B2 (en) |
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004066030A (en) * | 2002-08-02 | 2004-03-04 | Mitsubishi Heavy Ind Ltd | Method and equipment for removing nitrogen compound from wastewater |
| JP2008036514A (en) * | 2006-08-04 | 2008-02-21 | Fuji Electric Systems Co Ltd | Wastewater treating method |
| JP2008155080A (en) * | 2006-12-21 | 2008-07-10 | Hitachi Ltd | Sewage treatment apparatus and its method |
| JP2008221163A (en) * | 2007-03-14 | 2008-09-25 | Toshiba Corp | Wastewater treatment system |
| JP2009131854A (en) * | 2009-03-23 | 2009-06-18 | Maezawa Ind Inc | Sewage treatment apparatus |
| JP2009285582A (en) * | 2008-05-29 | 2009-12-10 | Hitachi Plant Technologies Ltd | Membrane separation activated sludge treatment apparatus and its method |
| JP2010253428A (en) * | 2009-04-28 | 2010-11-11 | Asahi Kasei Chemicals Corp | Wastewater treatment apparatus and wastewater treatment method |
| JP2011067727A (en) * | 2009-09-24 | 2011-04-07 | Sumiju Kankyo Engineering Kk | Method and apparatus for treating wastewater |
| JP2011200767A (en) * | 2010-03-24 | 2011-10-13 | Kubota Corp | Wastewater treating method and wastewater treatment system |
| JP2012076081A (en) * | 2011-12-12 | 2012-04-19 | Hitachi Plant Technologies Ltd | Membrane separation type activated sludge treatment apparatus and method thereof |
| JP2013501617A (en) * | 2010-02-05 | 2013-01-17 | ホソ ユニバーシティ アカデミック コーオペレーション ファンデーション | Advanced wastewater treatment system equipped with a plasma discharge tank |
| JP2013537107A (en) * | 2010-09-20 | 2013-09-30 | アメリカン・ウォーター・ワークス・カンパニー，インコーポレーテッド | Optimized nutrient removal from wastewater |
| WO2013168680A1 (en) * | 2012-05-07 | 2013-11-14 | 大成企業株式会社 | Wastewater treatment system and treatment method therefor |
| CN104045154A (en) * | 2013-03-12 | 2014-09-17 | 江苏瑞盛水处理有限公司 | Wastewater biological treatment system based on bio-contact oxidation process |
| JP2016002514A (en) * | 2014-06-16 | 2016-01-12 | 株式会社日立製作所 | Membrane separation activated sludge treatment apparatus and method of operating the same |
| US9656893B2 (en) | 2010-09-20 | 2017-05-23 | American Water Works Company, Inc. | Simultaneous anoxic biological phosphorus and nitrogen removal with energy recovery |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS58183995A (en) * | 1982-04-20 | 1983-10-27 | Nishihara Environ Sanit Res Corp | Biological denitrification and dephosphorization of crude night soil |
| JPS60129194A (en) * | 1983-12-16 | 1985-07-10 | Kurita Water Ind Ltd | Treatment of sewage |
| JPH09225492A (en) * | 1996-02-22 | 1997-09-02 | Kubota Corp | Waste water treatment |
| JPH09290289A (en) * | 1996-04-19 | 1997-11-11 | Daewoo Co Ltd | Device for biologically removing nitrogen and phosphorus in sewage and method thereof |
-
2000
- 2000-05-10 JP JP2000137559A patent/JP4742403B2/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS58183995A (en) * | 1982-04-20 | 1983-10-27 | Nishihara Environ Sanit Res Corp | Biological denitrification and dephosphorization of crude night soil |
| JPS60129194A (en) * | 1983-12-16 | 1985-07-10 | Kurita Water Ind Ltd | Treatment of sewage |
| JPH09225492A (en) * | 1996-02-22 | 1997-09-02 | Kubota Corp | Waste water treatment |
| JPH09290289A (en) * | 1996-04-19 | 1997-11-11 | Daewoo Co Ltd | Device for biologically removing nitrogen and phosphorus in sewage and method thereof |
Cited By (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004066030A (en) * | 2002-08-02 | 2004-03-04 | Mitsubishi Heavy Ind Ltd | Method and equipment for removing nitrogen compound from wastewater |
| JP4690265B2 (en) * | 2006-08-04 | 2011-06-01 | メタウォーター株式会社 | Wastewater treatment method |
| JP2008036514A (en) * | 2006-08-04 | 2008-02-21 | Fuji Electric Systems Co Ltd | Wastewater treating method |
| JP2008155080A (en) * | 2006-12-21 | 2008-07-10 | Hitachi Ltd | Sewage treatment apparatus and its method |
| JP4709792B2 (en) * | 2007-03-14 | 2011-06-22 | 株式会社東芝 | Wastewater treatment system |
| JP2008221163A (en) * | 2007-03-14 | 2008-09-25 | Toshiba Corp | Wastewater treatment system |
| JP2009285582A (en) * | 2008-05-29 | 2009-12-10 | Hitachi Plant Technologies Ltd | Membrane separation activated sludge treatment apparatus and its method |
| JP2009131854A (en) * | 2009-03-23 | 2009-06-18 | Maezawa Ind Inc | Sewage treatment apparatus |
| JP2010253428A (en) * | 2009-04-28 | 2010-11-11 | Asahi Kasei Chemicals Corp | Wastewater treatment apparatus and wastewater treatment method |
| JP2011067727A (en) * | 2009-09-24 | 2011-04-07 | Sumiju Kankyo Engineering Kk | Method and apparatus for treating wastewater |
| US8574435B2 (en) | 2010-02-05 | 2013-11-05 | Hoseo University Academic Cooperation Foundation | Advanced treatment system of wastewater having plasma discharging vessel |
| EP2531452A4 (en) * | 2010-02-05 | 2015-09-02 | Univ Hoseo Acad Coop Found | Advanced treatment system of wastewater having plasma discharging vessel |
| JP2013501617A (en) * | 2010-02-05 | 2013-01-17 | ホソ ユニバーシティ アカデミック コーオペレーション ファンデーション | Advanced wastewater treatment system equipped with a plasma discharge tank |
| JP2011200767A (en) * | 2010-03-24 | 2011-10-13 | Kubota Corp | Wastewater treating method and wastewater treatment system |
| JP2013537107A (en) * | 2010-09-20 | 2013-09-30 | アメリカン・ウォーター・ワークス・カンパニー，インコーポレーテッド | Optimized nutrient removal from wastewater |
| US9505644B2 (en) | 2010-09-20 | 2016-11-29 | American Water Works Company, Inc. | Simultaneous anoxic biological phosphorus and nitrogen removal |
| US9656893B2 (en) | 2010-09-20 | 2017-05-23 | American Water Works Company, Inc. | Simultaneous anoxic biological phosphorus and nitrogen removal with energy recovery |
| JP2012076081A (en) * | 2011-12-12 | 2012-04-19 | Hitachi Plant Technologies Ltd | Membrane separation type activated sludge treatment apparatus and method thereof |
| WO2013168680A1 (en) * | 2012-05-07 | 2013-11-14 | 大成企業株式会社 | Wastewater treatment system and treatment method therefor |
| CN104045154A (en) * | 2013-03-12 | 2014-09-17 | 江苏瑞盛水处理有限公司 | Wastewater biological treatment system based on bio-contact oxidation process |
| CN104045154B (en) * | 2013-03-12 | 2016-07-20 | 江苏瑞盛水处理有限公司 | Sewage biological treatment system based on Biological Contact Oxidation Process |
| JP2016002514A (en) * | 2014-06-16 | 2016-01-12 | 株式会社日立製作所 | Membrane separation activated sludge treatment apparatus and method of operating the same |
Also Published As
| Publication number | Publication date |
|---|---|
| JP4742403B2 (en) | 2011-08-10 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US6706185B2 (en) | Biological method of phosphorus removal and biological phosphorus-removing apparatus | |
| US7850851B2 (en) | Biological phosphorus removal | |
| US7172699B1 (en) | Energy efficient wastewater treatment for nitrogen and phosphorus removal | |
| JP4632356B2 (en) | Biological nitrogen removal method and system | |
| JP4742403B2 (en) | Wastewater treatment method | |
| JP2010253428A (en) | Wastewater treatment apparatus and wastewater treatment method | |
| CA2300719A1 (en) | Membrane supported biofilm process | |
| JP4570550B2 (en) | Nitrogen removal method and apparatus for high concentration organic wastewater | |
| JPH1157773A (en) | Biological dephosphorizing device | |
| JPS58210897A (en) | Biological dephosphorization method of waste water | |
| EP1260486A1 (en) | Method for treating organic wastewater | |
| JPS6254075B2 (en) | ||
| KR100709456B1 (en) | Waste water disposal plant and waste water disposal method | |
| JP3355121B2 (en) | Organic wastewater treatment method | |
| JP2000140886A (en) | Equipment for treatment of nitrogen-containing drainage | |
| JP3526140B2 (en) | Biological phosphorus removal method and apparatus for organic wastewater | |
| JP4547799B2 (en) | Biological phosphorus removal equipment | |
| JPH0819789A (en) | Method and apparatus for aerobic treatment of organic waste solution | |
| JP4882181B2 (en) | Denitrification method and apparatus | |
| JPH05104090A (en) | Method for treating sewage or sludge and apparatus therefor | |
| JP4380290B2 (en) | Nitrogen-containing organic wastewater treatment method and apparatus | |
| EP1555245A2 (en) | A biologial method of phosphorous removal and biological phosphorous-removing apparatus | |
| JP3919999B2 (en) | Organic wastewater treatment method and apparatus | |
| JPH0994596A (en) | Removal and recovery of phosphorus from organic sewage | |
| JPH0691292A (en) | Operation control method of aerobic-anaerobic active sludge treatment apparatus |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A621 | Written request for application examination |
Free format text: JAPANESE INTERMEDIATE CODE: A621 Effective date: 20070405 |
|
| A977 | Report on retrieval |
Free format text: JAPANESE INTERMEDIATE CODE: A971007 Effective date: 20081224 |
|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20100209 |
|
| A521 | Written amendment |
Free format text: JAPANESE INTERMEDIATE CODE: A523 Effective date: 20100407 |
|
| 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: 20110412 |
|
| A61 | First payment of annual fees (during grant procedure) |
Free format text: JAPANESE INTERMEDIATE CODE: A61 Effective date: 20110425 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20140520 Year of fee payment: 3 |
|
| R150 | Certificate of patent or registration of utility model |
Ref document number: 4742403 Country of ref document: JP Free format text: JAPANESE INTERMEDIATE CODE: R150 Free format text: JAPANESE INTERMEDIATE CODE: R150 |
|
| LAPS | Cancellation because of no payment of annual fees |