JP2008086863A - Out-tank type membrane separation activated sludge process - Google Patents
Out-tank type membrane separation activated sludge process Download PDFInfo
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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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Abstract
Description
本発明は、下水、返流水、工場排水、ゴミ浸出水、し尿、農業廃水、畜産排水、養殖排水などの各種有機性排水の処理に用いられる槽外設置型膜分離活性汚泥法に関するものであり、特に槽外設置型の分離膜を逆洗した際に発生する逆洗排水の取り扱いに関するものである。 The present invention relates to an outside tank type membrane separation activated sludge method used for treating various organic wastewater such as sewage, return water, industrial wastewater, waste leachate, human waste, agricultural wastewater, livestock wastewater and aquaculture wastewater. In particular, the present invention relates to the handling of backwash wastewater generated when backwashing a separation membrane installed outside the tank.
上記のような有機性排水の処理法としては、生物処理槽内において微生物による処理を行わせる活性汚泥法が一般的である。生物処理槽の槽内水は最終沈殿池において重力沈降による固液分離が行われ、上澄水が処理水として取り出される。しかしこの方法は重力沈降に長時間を要するために広い最終沈殿池を設置しなければならない。そこで最終沈殿池を分離膜に置き換えた膜分離活性汚泥法が普及しつつある。 As an organic wastewater treatment method as described above, an activated sludge method in which treatment with microorganisms is performed in a biological treatment tank is common. The water in the biological treatment tank is subjected to solid-liquid separation by gravity sedimentation in the final sedimentation tank, and the supernatant water is taken out as treated water. However, since this method requires a long time for gravity sedimentation, a wide final sedimentation basin must be installed. Therefore, a membrane separation activated sludge method in which the final sedimentation basin is replaced with a separation membrane is becoming widespread.
この膜分離活性汚泥法は、槽内に分離膜を浸漬させて槽内水を直接ろ過させる槽内設置型膜分離活性汚泥法と、槽外に分離膜を設置し、槽内水を循環させながらろ過する槽外設置型膜分離活性汚泥法に大別される。このうち槽内設置型膜分離活性汚泥法では、分離膜が生物槽内に浸漬されているので、膜面に捕捉された膜孔径近傍の粒子(膜面閉塞物質)を生物反応槽から槽外に除去することができない。このため、膜ろ過性能の安定性を確保することが困難であるという問題があった。 This membrane separation activated sludge method has a membrane installed activated sludge method in which the separation membrane is immersed in the tank and the water in the tank is directly filtered, and a separation membrane is installed outside the tank to circulate the water in the tank. It is roughly classified into an outside tank type activated membrane separation activated sludge method. Among these, in the membrane separation activated sludge method installed in the tank, since the separation membrane is immersed in the biological tank, particles near the membrane pore diameter (membrane surface blocking substance) trapped on the membrane surface are removed from the biological reaction tank to the outside of the tank. Can not be removed. For this reason, there existed a problem that it was difficult to ensure the stability of membrane filtration performance.
一方、槽外設置型膜分離活性汚泥法では、分離膜に膜面閉塞物質が堆積してきた際に逆洗により取り除くことができるが、この逆洗排水は生物反応槽に返送して再処理するのが普通である。逆洗排水中の膜面閉塞物質はペレット状となっている場合があるが、生物反応槽に返送されると曝気撹拌により解体し、元の粒子に戻ってしまう。 On the other hand, in the membrane separation activated sludge method installed outside the tank, when the membrane surface clogging material accumulates on the separation membrane, it can be removed by backwashing, but this backwash wastewater is returned to the biological reaction tank for reprocessing. Is normal. The membrane surface blocking substance in the backwash drainage may be in the form of pellets, but when it is returned to the biological reaction tank, it is disassembled by aeration and agitation and returns to the original particles.
また、生物反応槽に返送された膜面閉塞物質の一部は活性汚泥フロックに取り込まれるが、汚泥活性の低下する冬季には活性汚泥フロックに取り込まれる膜面閉塞物質量は減少するため、生物反応槽中の膜面閉塞物質量が増加する。これらの理由により、逆洗排水を生物反応槽に返送すると、槽内設置型膜分離活性汚泥法と同様に膜ろ過性能の安定性を確保することが困難となる。 Part of the membrane surface clogging material returned to the biological reaction tank is taken up by the activated sludge floc, but the amount of membrane surface clogging material taken up by the activated sludge floc decreases during the winter when sludge activity decreases. The amount of membrane surface blocking substance in the reaction vessel increases. For these reasons, when the backwash wastewater is returned to the biological reaction tank, it is difficult to ensure the stability of the membrane filtration performance as in the case of the in-tank membrane separation activated sludge method.
そこで特許文献1に示すように、槽外に設置された分離膜の逆洗排水を外部に排出することが提案されているが、この方法では生物反応槽中のMLSS濃度が低下し過ぎて生物活性が低下するおそれがあるうえ、外部に排出された逆洗排水を処理するために別の排水処理設備が必要になり、実用性に欠けるという問題がある。
本発明は上記した従来の問題点を解決し、生物反応槽中のMLSS濃度を過度に低下させることがなく、また逆洗排水のために別の排水処理設備を必要とせず、しかも分離膜の膜ろ過性能の安定性を確保することができる槽外設置型膜分離活性汚泥法を提供するためになされたものである。 The present invention solves the above-described conventional problems, does not excessively reduce the MLSS concentration in the biological reaction tank, does not require a separate wastewater treatment facility for backwash wastewater, and further does not require a separation membrane. It was made in order to provide the outside tank installation type membrane separation activated sludge method which can ensure the stability of membrane filtration performance.
上記の課題を解決するためになされた本発明は、生物反応槽の槽内水を槽外に設置した分離膜に循環させてろ過水を取り出す槽外設置型膜分離活性汚泥法において、分離膜を逆洗することによって生じた膜面閉塞物質を含む逆洗排水をオゾン処理し、膜面閉塞物質を微細化、あるいは、活性汚泥フロックに取り込まれやすい状態にしたうえで生物反応槽に返送することを特徴とするものである。 The present invention made in order to solve the above-mentioned problem is a separation membrane in an outside tank type membrane separation activated sludge method in which the in-vessel water of a biological reaction tank is circulated through a separation membrane installed outside the tank and filtrate is taken out. Backwash wastewater containing membrane surface clogging material generated by backwashing is treated with ozone to make the membrane surface clogging material fine or easy to be taken into activated sludge flocs and returned to the biological reaction tank. It is characterized by this.
本発明によれば、逆洗排水をオゾン処理し、膜面閉塞物質を微細化するので、生物反応槽に返送された膜面閉塞物質は膜面を閉塞しない微粒子となり、再び膜面を閉塞することはない。従って従来のように生物反応槽中の膜面閉塞物質量が増加することがなく、分離膜の膜ろ過性能の安定性を確保することができる。しかも逆洗排水は全量を生物反応槽に返送できるので、逆洗排水のための別の排水処理設備を必要とせず、また逆洗排水を外部に排出しないため、生物反応槽中のMLSS濃度を過度に低下させることがなく、生物活性を維持することができる。また、生物反応槽に、嫌気無酸素好気法など、生物学的脱りんを含む処理工程を選定した場合には、オゾン処理した排水を嫌気槽に返送することにより、生物学的脱りんに必要な有機物を供給でき、生物学的脱りんの安定化も可能となる。 According to the present invention, the backwash wastewater is treated with ozone to refine the membrane surface blocking substance, so that the membrane surface blocking material returned to the biological reaction tank becomes fine particles that do not block the membrane surface and again blocks the membrane surface. There is nothing. Therefore, the membrane surface blocking substance amount in the biological reaction tank does not increase as in the conventional case, and the stability of the membrane filtration performance of the separation membrane can be ensured. In addition, since the entire amount of backwash wastewater can be returned to the biological reaction tank, no separate wastewater treatment facility is required for backwash wastewater, and the backwash wastewater is not discharged to the outside. Biological activity can be maintained without being excessively reduced. In addition, when a treatment process that includes biological dephosphorization, such as anaerobic anaerobic anaerobic method, is selected for the biological reaction tank, the wastewater treated with ozone is returned to the anaerobic tank for biological dephosphorization. Necessary organic substances can be supplied, and biological dephosphorization can be stabilized.
以下に本発明の好ましい実施形態を示す。
図1において1は生物反応槽であり、従来と同様に有機性排水である原水、例えば下水が好気性微生物によって活性汚泥処理されている。2は生物反応槽1の外部に設置された分離膜であり、その一次側に生物反応槽1の槽内水が循環ポンプ3によって供給され、膜ろ過される。この実施形態ではクロスフロー方式のろ過が行われており、膜面を二次側に透過した膜ろ過水は処理水として処理水タンク4に取り出され、濃縮水は一次側の端部から返流管路5を通じて生物反応槽1に返送される。
Preferred embodiments of the present invention are shown below.
In FIG. 1, reference numeral 1 denotes a biological reaction tank, in which raw water, for example, sewage, which is organic wastewater, is treated with activated sludge by aerobic microorganisms.
分離膜2の種類はMF膜またはUF膜であり、その材質はセラミック、高分子の何れでもよい。また膜形状はモノリス膜、チューブラー膜、平膜、中空糸膜のいずれでもよく、加圧方式は内圧式、外圧式の何れでも良い。モノリス膜やチューブラー膜の場合には、一次側の流路は断面が円形であるか、四角形以上の多角形であることが好ましい。この実施形態では、分離膜2として出願人会社製のセラミック製モノリス膜を用いている。この膜は、セラミック多孔体の内部に断面が円形の流路を多数形成し、各流路の周面を膜孔径が0.1μmの膜面としたMF膜である。
The type of the
このような槽外設置型の分離膜2を用いれば生物反応槽1の槽内水の固液分離を容易に行うことができ、従来の最終沈殿池に比較して装置全体の小型化を図ることができる。しかし活性汚泥及び槽内水中の固形分は分離膜2の膜面に堆積するため、定期的に、あるいは膜差圧が上昇したときに循環ポンプ3を停止し、処理水タンク4から処理水を逆洗ポンプ6によって分離膜2の二次側に打込み、膜面の逆洗を行う。この逆洗の頻度は原水の性状によって大きく異なるが、原水の汚濁度が高い場合には10分間に1回程度、低い場合には3時間に1回程度とすることが好ましい。
If such a
この逆洗により生じた逆洗排水は、逆洗排水タンク7に排出される。この逆洗排水中には、膜面から剥離された活性汚泥及び膜面閉塞物質が含まれている。従来はこの逆洗排水をそのまま生物反応槽1に戻していたが、本発明ではオゾン供給装置8から逆洗排水中にオゾンを供給し、オゾン処理を行う。
The backwash drainage generated by this backwash is discharged to the
オゾンは強い酸化力を有する気体であり、有機物を破壊・分解する作用を持つ。このため逆洗排水中の膜面閉塞物質を微細化し、分離膜2の膜孔径よりも小さい微粒子とすることができる。この目的のためのオゾン処理には、殺菌や汚泥減量を目的とするオゾン処理に比較して少量のオゾンを供給すればよく、ランニングコストは安価である。具体的にはオゾンの供給量は逆洗排水量あたり20〜100mgO3/L程度とすることが好ましい。なお、この実施形態では逆洗排水タンク7に直接オゾンを供給したが、別にオゾン処理手段を設けてもよいことはいうまでもない。
Ozone is a gas with strong oxidizing power and has the effect of destroying and decomposing organic matter. For this reason, the membrane surface blocking substance in the backwash waste water can be refined to make fine particles smaller than the membrane pore diameter of the
オゾン処理された逆洗排水は、返送用ポンプ9によって生物反応槽1に返送される。オゾン処理によって膜孔径近傍の膜面閉塞物質は、膜孔径よりも小さい微粒子となったり、表面改質により活性汚泥フロックに取り込まれやすい物質となっているので、この返送によって生物反応槽1内の膜孔径近傍の粒子からなる膜面閉塞物質量が増加することはない。従って本発明によれば分離膜2の膜ろ過性能は急速に低下することがなく、長期間にわたって安定したろ過が可能である。
The ozone-washed backwash waste water is returned to the biological reaction tank 1 by the return pump 9. The membrane surface blocking substance in the vicinity of the membrane pore diameter by ozone treatment becomes fine particles smaller than the membrane pore diameter or becomes a substance that is easily taken into the activated sludge floc by surface modification. The amount of the membrane surface blocking substance composed of particles in the vicinity of the membrane pore diameter does not increase. Therefore, according to the present invention, the membrane filtration performance of the
しかも本発明によれば、逆洗排水を系外に排出することなく生物反応槽1に返送するので、生物反応槽1のMLSS濃度が低下せず、生物反応槽1の生物活性を安定に維持することができる。さらに逆洗排水を処理するために別の処理装置を設ける必要もない。
以下に本発明の実施例を示す。
Moreover, according to the present invention, the backwash waste water is returned to the biological reaction tank 1 without being discharged out of the system, so that the MLSS concentration in the biological reaction tank 1 is not lowered, and the biological activity of the biological reaction tank 1 is stably maintained. can do. Further, it is not necessary to provide a separate processing device for processing the backwash waste water.
Examples of the present invention are shown below.
図1に示した処理装置を用いて、下水の活性汚泥処理を行った。生物反応槽のMLSS濃度は10,000mg/Lとした。分離膜は出願人会社製のモノリス型セラミック膜であり、膜孔径は0.1μmである。生物反応槽の槽内水を循環させてクロスフローろ過を行い、膜ろ過水を処理水として取り出した。 Using the treatment apparatus shown in FIG. 1, the activated sludge treatment of sewage was performed. The MLSS concentration in the biological reaction tank was 10,000 mg / L. The separation membrane is a monolithic ceramic membrane manufactured by the applicant company, and the membrane pore diameter is 0.1 μm. Cross flow filtration was performed by circulating water in the biological reaction tank, and membrane filtrate was taken out as treated water.
分離膜は1時間ごとにろ過運転を停止して逆洗を行った。膜面閉塞物質を含む逆洗排水を逆洗排水タンクに集め、オゾンを吹き込んでオゾン処理を行った。オゾン供給量は逆洗排水量あたり100mgO3/Lである。オゾン処理された逆洗排水は全量を生物反応槽に返送した。 The separation membrane was backwashed with the filtration operation stopped every hour. Backwash drainage containing membrane surface blocking substances was collected in a backwash drainage tank, and ozone treatment was performed by blowing ozone. The ozone supply amount is 100 mg O 3 / L per backwash waste water amount. The entire amount of ozone-washed backwash wastewater was returned to the biological reactor.
オゾン処理を行わない場合(従来例)とオゾン処理を行った場合(実施例)とを比較すると、処理水の性状はともに同一であるが、従来例では分離膜の膜ろ過流束が2.0m/日であったのに対し、実施例では2.4m/日であり、オゾン処理によって膜ろ過性能が大幅に改善されたことを確認できた。また、生物反応槽のMLSS濃度は10000mg/Lのままで、減少しなかった。 When the ozone treatment is not performed (conventional example) and the ozone treatment is performed (example), the properties of the treated water are the same, but in the conventional example, the membrane filtration flux of the separation membrane is 2. While it was 0 m / day, it was 2.4 m / day in the examples, and it was confirmed that the membrane filtration performance was greatly improved by the ozone treatment. In addition, the MLSS concentration in the bioreactor remained at 10000 mg / L and did not decrease.
次に逆洗排水へのオゾン供給量を変化させて、分離膜の膜ろ過流束に与える影響を調べた。オゾン供給量は逆洗排水量あたり20mgO3/Lである。オゾン処理された逆洗排水は全量を生物反応槽に返送した。従来例では分離膜の膜ろ過流束が2.0m/日であったのに対し、実施例では2.4m/日であり、オゾン処理によって膜ろ過性能が大幅に改善されたことを確認できた。上記のように、微量のオゾンによって膜ろ過性能の改善を図れることを確認した。 Next, the influence of the separation membrane on the membrane filtration flux was examined by changing the amount of ozone supplied to the backwash wastewater. The amount of ozone supply is 20 mg O 3 / L per backwash waste water amount. The entire amount of ozone-washed backwash wastewater was returned to the biological reactor. In the conventional example, the membrane filtration flux of the separation membrane was 2.0 m / day, whereas in the example, it was 2.4 m / day, confirming that the membrane filtration performance was greatly improved by ozone treatment. It was. As described above, it was confirmed that the membrane filtration performance could be improved with a small amount of ozone.
1 生物反応槽
2 分離膜
3 循環ポンプ
4 処理水タンク
5 返流管路
6 逆洗ポンプ
7 逆洗排水タンク
8 オゾン供給装置
DESCRIPTION OF SYMBOLS 1
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JP2014061506A (en) * | 2012-09-24 | 2014-04-10 | Hitachi Ltd | Liquid treatment facility |
CN110167889A (en) * | 2016-12-06 | 2019-08-23 | 格兰富控股联合股份公司 | Biomass selection and the consumption of selectivity organism matter enhance the multi-parameter of Membrane Bioreactor for Wastewater Treatment efficiency |
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JPH0474584A (en) * | 1990-07-16 | 1992-03-09 | Kuraray Co Ltd | Treatment of waste water |
JPH0496718A (en) * | 1990-08-10 | 1992-03-30 | Matsushita Electric Ind Co Ltd | Cord fitting hook |
JPH06182338A (en) * | 1992-12-16 | 1994-07-05 | Kurita Water Ind Ltd | Membrane separating device |
JPH11128920A (en) * | 1997-10-30 | 1999-05-18 | Kubota Corp | Operation of organic wastewater treatment apparatus |
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JPH0474584A (en) * | 1990-07-16 | 1992-03-09 | Kuraray Co Ltd | Treatment of waste water |
JPH0496718A (en) * | 1990-08-10 | 1992-03-30 | Matsushita Electric Ind Co Ltd | Cord fitting hook |
JPH06182338A (en) * | 1992-12-16 | 1994-07-05 | Kurita Water Ind Ltd | Membrane separating device |
JPH11128920A (en) * | 1997-10-30 | 1999-05-18 | Kubota Corp | Operation of organic wastewater treatment apparatus |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
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JP2014061506A (en) * | 2012-09-24 | 2014-04-10 | Hitachi Ltd | Liquid treatment facility |
CN110167889A (en) * | 2016-12-06 | 2019-08-23 | 格兰富控股联合股份公司 | Biomass selection and the consumption of selectivity organism matter enhance the multi-parameter of Membrane Bioreactor for Wastewater Treatment efficiency |
CN110167889B (en) * | 2016-12-06 | 2022-12-30 | 格兰富控股联合股份公司 | Multi-parameter enhancement of membrane bioreactor treatment efficiency by biomass selection and selective biomass consumption |
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