JP2015199049A - Method and apparatus for biological treatment of organic waste water - Google Patents
Method and apparatus for biological treatment of organic waste water Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 37
- 239000010815 organic waste Substances 0.000 title claims abstract description 7
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
-
- 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
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- Biological Treatment Of Waste Water (AREA)
- Treatment Of Biological Wastes In General (AREA)
- Activated Sludge Processes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
Description
本発明は、生活排水、下水、食品工場やパルプ工場をはじめとした広い濃度範囲の有機性排水処理に利用することができる有機排水の生物処理方法及び装置に関するものであり、特に、第一生物処理槽及び該第一生物処理槽からの第一生物処理水が導入される第二生物処理槽を用いた有機性排水の生物処理方法及び装置に関する。 The present invention relates to a biological treatment method and apparatus for organic wastewater that can be used for organic wastewater treatment in a wide concentration range including domestic wastewater, sewage, food factories and pulp factories. The present invention relates to a biological treatment method and apparatus for organic wastewater using a second biological treatment tank into which a first biological treatment water from the treatment tank and the first biological treatment tank is introduced.
有機性排液の嫌気性処理方法として、高密度で沈降性の大きいグラニュール汚泥を形成し、溶解性ＢＯＤを含む有機性排液を上向流通液してスラッジブランケットを形成した状態で接触させて高負荷高速処理を行うＵＡＳＢ法（上向流スラッジブランケット法）、あるいは汚泥を粒状担体に高密度で付着させて、流動床を形成し、高負荷高速処理を行う流動床法などが採用されている。 As an anaerobic treatment method for organic drainage, granule sludge with high density and large sedimentation is formed, and organic drainage containing soluble BOD is flowed upward and brought into contact with sludge blanket formed. UASB method (upward flow sludge blanket method) that performs high-load high-speed treatment, or fluidized bed method that applies sludge to a granular carrier at high density to form a fluidized bed and perform high-load high-speed treatment, etc. ing.
これらの方法は、消化速度の遅い固形有機物を分離除去して得られた、消化速度の速い溶解性有機物主体の液を、嫌気性微生物密度の高いグラニュール汚泥、あるいは粒状担体に汚泥を担持した担持汚泥の流動床を用いる嫌気性処理によって高負荷で高速処理する方法である。 In these methods, liquids mainly composed of soluble organic substances having a high digestion rate obtained by separating and removing solid organic substances having a low digestion rate are supported on granular sludge having a high anaerobic microorganism density or on a granular carrier. This is a method of high-speed treatment with high load by anaerobic treatment using a fluidized bed of supported sludge.
しかし、単にＵＡＳＢのグラニュール汚泥を回分式嫌気処理法に用いても、被処理液にタンパク質、糖などの高分子の溶解性有機物が多く含まれていると、グラニュール汚泥の軽量化や崩壊、またメタン生成活性の悪化といった問題が生じる。これは被処理液中のタンパク質や糖を基質とする酸生成菌がグラニュール汚泥に付着して増殖するために生じる。すなわち酸生成菌はメタン生成菌に比べ増殖速度が速く、グラニュール汚泥に付着した酸生成菌は羽毛状に増殖するため、グラニュール汚泥の沈降性、メタン生成活性が低下し、処理効率が悪化する。 However, even if UASB granulated sludge is simply used for batch-type anaerobic treatment, if the liquid to be treated contains a large amount of soluble organic substances such as protein and sugar, the weight and disintegration of the granular sludge is reduced. In addition, problems such as deterioration of methanogenic activity occur. This occurs because acid-producing bacteria that use proteins and sugars in the liquid to be treated as substrates adhere to the granular sludge and grow. In other words, acid-producing bacteria grow faster than methanogens, and acid-producing bacteria attached to granule sludge grow in a feather shape, so the sedimentation and methanogenic activity of the granule sludge is reduced, and the processing efficiency deteriorates. To do.
粒状汚泥の活性および沈降性を高くして効率的よく嫌気性処理を行うことができる生物処理方法として、特許文献１に、有機性排液を酸生成槽に導入し、酸生成菌を含む汚泥と嫌気性下に接触させて有機酸生成反応を行う酸生成工程と、酸生成工程の処理液をメタン生成槽に導入し、メタン生成菌を含む粒状汚泥を流動させた状態で嫌気性下に接触させて回分式にメタン生成反応を行い、反応後静置分離して分離液を排出するメタン生成工程と、を有する生物処理方法が記載されている。 As a biological treatment method capable of efficiently performing anaerobic treatment by increasing the activity and sedimentation of granular sludge, Patent Document 1 introduces an organic drainage liquid into an acid production tank and contains sludge containing acid producing bacteria. And anaerobic contact in an anaerobic condition, and an acid generation process in which the organic acid generation reaction is conducted, and the treatment liquid of the acid generation process is introduced into the methane generation tank, and the granular sludge containing the methane generating bacteria is fluidized under anaerobic conditions. A biological treatment method is described in which a methane production reaction is carried out in a batch-wise manner, and a methane production step is carried out in which the separation liquid is discharged after standing and separating after the reaction.
この特許文献１では、酸生成槽で酸生成菌により有機物をメタン生成細菌が利用可能な形のアルコールや有機酸まで低分子化するとともに、酸生成菌を増殖させ、メタン生成を安定化させる。 In Patent Document 1, an organic substance is reduced in molecular weight to an alcohol or organic acid in a form that can be used by methanogenic bacteria in an acid producing tank, and the acid producing bacteria are grown to stabilize methane production.
特許文献２には、有機性排水を第一生物処理槽で細菌により処理し、排水に含まれる有機物を酸化分解して非凝集性の細菌の菌体に変換した後、原生動物の担体を有した第二処理槽で固着性原生動物に捕食除去させる有機性排水の生物処理方法が記載されている。
In
この特許文献２の第一生物処理槽では、一過式で分散状態の細菌により有機物の大部分を処理し、第二生物処理槽でこの分散菌を微小動物により捕食させ、汚泥減量を行う。
In the first biological treatment tank of
特許文献１の酸生成槽や特許文献２の分散菌槽は、浮遊状態で細菌を維持するため、ある程度の滞留時間が必要となり、排水の性状によっては必要な滞留時間が長くなり、槽の容積が大きくなり、大きな設置面積が必要となる。また、装置施工後に原水負荷が設計値より大きくなると、分散菌槽や酸生成槽の槽容積が不足してしまう。
The acid generation tank of Patent Document 1 and the dispersion bacteria tank of
本発明は、第一生物処理槽と、その処理水が導入される第二生物処理槽とを有する有機性排水の生物処理方法及び装置において、生物処理槽の容積を減少可能とすることを目的とする。 An object of the present invention is to reduce the volume of a biological treatment tank in an organic wastewater biological treatment method and apparatus having a first biological treatment tank and a second biological treatment tank into which the treated water is introduced. And
本発明の有機性排水の生物処理装置は、有機性排水が貯留される原水槽と、該原水槽から有機性排水が導入され、細菌により生物処理されて第一生物処理水が生成する第一生物処理槽と、第一生物処理水が導入され、生物処理されて第二生物処理水が生成する第二生物処理槽とを有する有機性排水の生物処理装置において、第二生物処理槽又はその下流側から第一生物処理槽又はその上流側への汚泥混合液及び／又は分離汚泥の返送手段を具備せず、第一生物処理槽内容液又は第一生物処理水を原水流量に対し２０％以下の割合で原水槽に返送する返送ラインを具備したことを特徴とするものである。 The biological wastewater treatment apparatus according to the present invention includes a raw water tank in which organic wastewater is stored, an organic wastewater introduced from the raw water tank, and biologically treated with bacteria to produce a first biologically treated water. In a biological treatment apparatus for organic wastewater having a biological treatment tank and a second biological treatment tank into which the first biological treated water is introduced and biologically treated to produce the second biological treated water, the second biological treatment tank or its Without the means for returning the sludge mixed liquid and / or separated sludge from the downstream side to the first biological treatment tank or its upstream side, the content of the first biological treatment tank or the first biological treatment water is 20% of the raw water flow rate. It is characterized by having a return line that returns to the raw water tank at the following ratio.
本発明の有機性排水の生物処理方法は、本発明の有機性排水の生物処理装置によって有機性排水を処理するものである。 The organic wastewater biological treatment method of the present invention treats organic wastewater with the organic wastewater biological treatment apparatus of the present invention.
本発明の有機性排水の生物処理方法では、有機物分解に必要な栄養源を原水槽に添加するとともに、原水槽のｐＨを５．５〜８．５に調整することが好ましい。 In the biological treatment method for organic wastewater of the present invention, it is preferable to add a nutrient source necessary for organic matter decomposition to the raw water tank and adjust the pH of the raw water tank to 5.5 to 8.5.
本発明の有機性排水の生物処理方法では、原水槽の水位を、ＨＲＴを１時間以上に維持するように設定することが好ましい。 In the organic wastewater biological treatment method of the present invention, it is preferable to set the water level of the raw water tank so that the HRT is maintained for 1 hour or more.
本発明の有機性排水の生物処理方法では、原水槽に、高さが原水槽の最大水深の５０％以下の固定床を設置し、固定床が水面下にあるように水位を維持することが好ましい。 In the biological treatment method for organic wastewater of the present invention, a fixed floor having a height of 50% or less of the maximum depth of the raw water tank is installed in the raw water tank, and the water level is maintained so that the fixed floor is below the water surface. preferable.
本発明の有機性排水の生物処理方法の一態様では、第一生物処理槽で分散状態の細菌により有機物処理を行い、分散状態の細菌を含む第一生物処理水を第二生物処理槽に導入し、第二生物処理槽で分散状態の細菌と残存する有機物の処理を行う。 In one aspect of the organic wastewater biological treatment method of the present invention, organic matter treatment is performed with dispersed bacteria in the first biological treatment tank, and the first biological treatment water containing the dispersed bacteria is introduced into the second biological treatment tank. In the second biological treatment tank, the dispersed bacteria and the remaining organic matter are treated.
本発明の有機性排水の生物処理方法の別の一態様では、第一生物処理槽が酸生成槽であり、第二生物処理槽がメタン生成を行う嫌気処理である。 In another one aspect | mode of the biological treatment method of the organic waste_water | drain of this invention, a 1st biological treatment tank is an acid production tank, and a 2nd biological treatment tank is the anaerobic process which produces | generates methane.
本発明では、第一生物処理槽内容液又は第一生物処理水の一部を原水槽に返送するところから、原水槽でも第一生物処理槽と同様の生物処理が進行する。これにより、生物処理装置全体の処理効率が向上し、生物処理槽特に第一生物処理槽の容積削減を図ることができる。
特に装置施工後や既設装置において、第一生物処理槽の容積を大きくすることなく高負荷に対応する運転を行うことが可能になる。
In the present invention, since a part of the first biological treatment tank contents liquid or a part of the first biological treatment water is returned to the raw water tank, the same biological treatment as in the first biological treatment tank proceeds in the raw water tank. Thereby, the processing efficiency of the whole biological treatment apparatus improves, and the volume reduction of a biological treatment tank, especially a 1st biological treatment tank can be aimed at.
In particular, it is possible to perform operation corresponding to a high load without increasing the volume of the first biological treatment tank after the apparatus construction or in the existing apparatus.
また、本発明では、第二生物処理槽又はその下流側から第一生物処理槽又はその上流側への汚泥混合液や分離汚泥の返送を行わないので、第一生物処理槽での分散菌生成効率が向上する。なお、第二生物処理槽やその下流側から汚泥混合液や分離汚泥を原水槽や第一生物処理槽に返送すると、好気処理ではワムシなど分散菌を捕食する微小動物が第一生物処理に供給されるため、濾過捕食性分散菌が捕食されてしまい、分散菌生成の制御が困難になる。また、嫌気処理では、原水槽や第一生物処理槽においてメタンガスが発生し、ガス処理など第二生物処理槽と同様の付帯設備が必要となる。 Further, in the present invention, since the sludge mixed solution and the separated sludge are not returned from the second biological treatment tank or the downstream side thereof to the first biological treatment tank or the upstream side thereof, the dispersal bacteria are generated in the first biological treatment tank. Efficiency is improved. If the sludge mixture or separated sludge is returned from the second biological treatment tank or its downstream side to the raw water tank or the first biological treatment tank, the micro-animals that prey on dispersal bacteria such as rotifers will be used for the first biological treatment. Since it is supplied, the filter-predatory dispersal bacteria are preyed on, and it becomes difficult to control the production of the dispersal bacteria. In the anaerobic treatment, methane gas is generated in the raw water tank and the first biological treatment tank, and the same incidental facilities as the second biological treatment tank such as gas treatment are required.
以下、図面を参照して本発明についてさらに詳細に説明する。 Hereinafter, the present invention will be described in more detail with reference to the drawings.
図１は本発明方法及び装置の基本的な形態を示すフロー図である。本発明では、有機性排水を原水槽１に導入し、好ましくは撹拌を行う。この攪拌は機械攪拌、曝気攪拌のいずれでも良い。原水槽１及び第一生物処理槽１０内で嫌気処理を行う場合は、連続通水中は原水槽１でＤＯが検出されないように攪拌するのが好ましい。原水槽１で好気処理を行う場合でも、臭気が発生しない程度であるならば、原水槽１のＤＯは検出されなくても良い。 FIG. 1 is a flow diagram showing the basic form of the method and apparatus of the present invention. In this invention, organic waste_water | drain is introduce | transduced into the raw | natural water tank 1, Preferably stirring is performed. This stirring may be either mechanical stirring or aeration stirring. When anaerobic treatment is performed in the raw water tank 1 and the first biological treatment tank 10, it is preferable to stir the continuous water so that DO is not detected in the raw water tank 1. Even when the aerobic treatment is performed in the raw water tank 1, the DO of the raw water tank 1 may not be detected as long as the odor is not generated.
原水槽１で反応を進めるため、栄養剤を原水槽１に添加するのが好ましい。この栄養剤とは、Ｎ、Ｐ、Ｓ、Ｃａ、Ｍｇ、Ｋ、Ｚｎ、Ｃｕ、アミノ酸、ビタミン等、微生物の増殖に必要な、無機物、有機物、ミネラル、微量金属など、対象原水で不足しているものを示す。また、原水槽１のｐＨは５．５〜８．５となるように酸又はアルカリで調整するのが好ましい。油分を含有する排水の場合は、油分の固化を防ぐため、ｐＨを８〜８．５とすることが望ましい。 In order to advance the reaction in the raw water tank 1, it is preferable to add a nutrient to the raw water tank 1. These nutrients are insufficient in the target raw water such as N, P, S, Ca, Mg, K, Zn, Cu, amino acids, vitamins, etc., which are necessary for the growth of microorganisms, such as inorganic substances, organic substances, minerals, and trace metals. Indicates what is. Moreover, it is preferable to adjust with the acid or alkali so that pH of the raw | natural water tank 1 may be set to 5.5-8.5. In the case of wastewater containing oil, it is desirable to adjust the pH to 8 to 8.5 in order to prevent solidification of the oil.
なお、原水槽１でのＨＲＴが１時間以上、例えば１〜１２時間となるように原水槽１内の水位を維持するのが好ましい。 In addition, it is preferable to maintain the water level in the raw | natural water tank 1 so that HRT in the raw | natural water tank 1 may be 1 hour or more, for example, 1 to 12 hours.
原水槽１に固定床担体を設置し、原水槽１内の菌体保持能を高めても良い。この場合、固定床の高さが高いと、原水槽１の水位が低い場合に、固定床が水面から出てしまうため、固定床の高さは原水槽１の最大水深の５０％程度、望ましくは３０％以下、例えば１０〜３０％とするのが好ましい。固定床担体は充填型でも可能だが、板状、紐状、短冊状等の揺動型が好ましい。なお、流動床は制御が困難であり固定床が好ましい。 A fixed bed carrier may be installed in the raw water tank 1 to enhance the ability to retain cells in the raw water tank 1. In this case, if the height of the fixed floor is high, the fixed floor will come out of the water surface when the water level of the raw water tank 1 is low. Therefore, the height of the fixed floor is preferably about 50% of the maximum water depth of the raw water tank 1. Is preferably 30% or less, for example, 10 to 30%. The fixed bed carrier can be a filling type, but is preferably a rocking type such as a plate, string or strip. The fluidized bed is difficult to control and a fixed bed is preferable.
原水槽１内の有機性排水は第一生物処理槽１０に導入され、好気的又は嫌気的に生物処理される。この第一生物処理槽１０の処理水（第一生物処理水）又は内容液を返送ライン２によって原水槽１に返送する。このように第一生物処理槽内容液又は第一生物処理水を原水槽１に返送すると、原水槽１に種菌を接種することとなり、原水槽１でも、第一生物処理槽１０と同様の生物処理が行われる。返送ライン２による返送は第一生物処理槽１０の処理水移送ライン又は第一生物処理槽１０の出口付近から行うことが望ましい。
The organic waste water in the raw water tank 1 is introduced into the first biological treatment tank 10 and biologically treated aerobically or anaerobically. The treated water (first biological treated water) or the content liquid in the first biological treatment tank 10 is returned to the raw water tank 1 through the
第一生物処理槽１０での処理は一過式とし、第二生物処理槽２０又はそれよりも下流側からの汚泥混合液や分離汚泥の返送は行わない。第一生物処理槽１０のＢＯＤ容積負荷は１ｋｇ／ｍ３／ｄａｙ以上例えば１〜２０ｋｇ／ｍ３／ｄａｙとし、ＨＲＴは２４時間以下、特に０．５〜８時間とするのが好ましい。 The treatment in the first biological treatment tank 10 is made transient, and the sludge mixed liquid and separated sludge from the second biological treatment tank 20 or the downstream side thereof are not returned. The BOD volume load of the first biological treatment tank 10 is preferably 1 kg / m 3 / day or more, for example 1 to 20 kg / m 3 / day, and the HRT is preferably 24 hours or less, particularly 0.5 to 8 hours.
第一生物処理槽１０に担体を添加し、汚泥保持量を増やし、負荷変動に対応できるようにしても良い。担体は流動床担体、固定床担体（充填型担体、揺動性担体）のいずれでも良い。第一生物処理槽１０に流動床を形成する場合、図１に示すように、スクリーンやストレーナなどの担体分離手段１１を設け、担体１２と内容液を分離後、内容液を返送するのが好ましい。
A carrier may be added to the first biological treatment tank 10 to increase the sludge retention amount so as to cope with load fluctuations. The carrier may be either a fluidized bed carrier or a fixed bed carrier (filled carrier, rocking carrier). When forming a fluidized bed in the first biological treatment tank 10, it is preferable to provide carrier separation means 11 such as a screen or a strainer as shown in FIG. 1 and to return the content liquid after separating the
また、第二生物処理槽２０にも担体を添加し、汚泥保持量を増やし、負荷変動に対応できるようにしても良い。担体は流動床担体、固定床担体（充填型担体、揺動性担体）のいずれでも良い。第二生物処理槽２０に流動床を形成する場合、図１に示すように、スクリーンやストレーナなどの担体分離手段２１を設け、担体２２と内容液を分離後、処理水を取り出すのが好ましい。
Further, a carrier may be added to the second biological treatment tank 20 to increase the sludge retention amount so as to cope with load fluctuations. The carrier may be either a fluidized bed carrier or a fixed bed carrier (filled carrier, rocking carrier). When the fluidized bed is formed in the second biological treatment tank 20, it is preferable to provide a carrier separation means 21 such as a screen or a strainer as shown in FIG. 1, and to remove the treated water after separating the
第一生物処理槽１０の処理水又は内容液の返送量は、原水流量Ｑの２０％以下、望ましくは１〜１０％、さらに望ましくは１〜５％とする。内容液又は第一生物処理水の返送は、この返送量となるならば、連続でも間欠でもよい。 The return amount of the treated water or the content liquid in the first biological treatment tank 10 is 20% or less of the raw water flow rate Q, desirably 1 to 10%, and more desirably 1 to 5%. The return of the content liquid or the first biological treatment water may be continuous or intermittent as long as this return amount is reached.
内容液又は第一生物処理槽処理水の返送量は負荷変動（水量、原水濃度）に応じて変更するのが好ましい。時間当たりの変動比（１時間中の最大負荷）／（１時間中の最低負荷）に対する返送量を表１の通りとするのが好ましい。 It is preferable to change the return amount of the content liquid or the first biological treatment tank treated water according to the load fluctuation (water amount, raw water concentration). It is preferable that the return amount with respect to the fluctuation ratio per hour (maximum load during one hour) / (minimum load during one hour) is as shown in Table 1.
本発明は、第一生物処理槽１０で分散菌を生成させ、第二生物処理槽２０でこれを捕食する処理、又は第一生物処理槽１０で酸を生成させ、第二生物処理槽２０でメタンを生成させる処理を行う方法に適用するのに好適である。 In the first biological treatment tank 10, dispersed bacteria are generated in the first biological treatment tank 20, and in the second biological treatment tank 20, acid is generated in the second biological treatment tank 20. It is suitable for applying to a method for performing a process for producing methane.
図２は、本発明を微小動物の捕食を利用した生物処理に適用したフローを示している。有機性排水は原水槽１から第一生物処理槽１０に導入され、散気管１３で曝気される。これにより、分散菌が増殖し、有機成分（溶解性ＢＯＤ）の７０％以上、望ましくは８０％以上さらに望ましくは９０％以上が酸化分解される。第一生物処理槽１０のｐＨは６〜８．５とするのが好ましい。ただし、原水中に油分を多く含む場合は分解速度を上げるため、ｐＨを８．０〜９．０としても良い。 FIG. 2 shows a flow in which the present invention is applied to biological treatment using predation of micro animals. Organic wastewater is introduced from the raw water tank 1 to the first biological treatment tank 10 and aerated by the air diffuser 13. As a result, the dispersal bacteria grow and 70% or more, desirably 80% or more, more desirably 90% or more of the organic component (soluble BOD) is oxidatively decomposed. The pH of the first biological treatment tank 10 is preferably 6 to 8.5. However, when the raw water contains a large amount of oil, the pH may be adjusted to 8.0 to 9.0 in order to increase the decomposition rate.
第一生物処理槽１０での通水は一過式を基本とし、ＢＯＤ容積負荷は１ｋｇ／ｍ３／ｄａｙ以上、ＨＲＴ２４時間以下、望ましくは０．５〜８時間とすることで、非凝集性細菌が優占化した処理水を得ることが出来る。また、ＨＲＴを短くすることでＢＯＤ濃度の薄い排水を高負荷で処理することが出来る。二槽以上の多段化や各種の担体の添加によりＢＯＤ容積負荷は５ｋｇ／ｍ３／ｄａｙ以上の高負荷化が可能になる。 The water flow in the first biological treatment tank 10 is basically a transient type, and the BOD volumetric load is 1 kg / m 3 / day or more, HRT 24 hours or less, preferably 0.5 to 8 hours, and is non-aggregating. Treated water that is dominated by bacteria can be obtained. Also, by shortening the HRT, wastewater with a low BOD concentration can be treated with a high load. The BOD volumetric load can be increased to 5 kg / m 3 / day or higher by adding two or more tanks or adding various carriers.
担体として流動床担体を添加する場合、流動床担体は球状、ペレット状、中空筒状等、任意であり、大きさも０．１〜１０ｍｍ程度の径である。材料は天然素材、無機素材、高分子素材等任意で、ゲル状物質を用いても良い。流動床担体を添加する場合は、図１のように槽内液の排出部に担体を分離するためのスクリーンなどの担体分離手段１１を設ける。 When a fluidized bed carrier is added as a carrier, the fluidized bed carrier may be any shape such as a spherical shape, a pellet shape, or a hollow cylindrical shape, and the size is about 0.1 to 10 mm. The material may be any natural material, inorganic material, polymer material, etc., and a gel material may be used. In the case of adding a fluidized bed carrier, carrier separating means 11 such as a screen for separating the carrier is provided in the discharge portion of the liquid in the tank as shown in FIG.
担体は流動床担体に限らず、固定床担体（充填型担体、揺動性担体）でも良い。図２の符号１５は固定床担体を示している。揺動性固定床担体の形状は糸状、板状、短冊状など任意であり、材料は天然素材、無機素材、高分子素材等任意である。
The carrier is not limited to a fluidized bed carrier, but may be a fixed bed carrier (filled carrier, rocking carrier).
第一生物処理槽１０に添加する担体の充填率が過度に高い場合、分散菌は生成せず、細菌は担体に付着するか、糸状性細菌が増殖する。そこで、第一生物処理槽１０の担体の充填率を２０％以下、望ましくは１０％以下、例えば流動床の場合は５〜１０％、揺動性固定床の場合は０．１〜２％とすることで、濃度変動に影響されず、捕食しやすい分散菌の生成が可能になる。また、第一生物処理槽１０内のＤＯを１ｍｇ／Ｌ以下、望ましくは０．５ｍｇ／Ｌ以下とし、糸状性細菌の増殖を抑制しても良い。 When the filling rate of the carrier added to the first biological treatment tank 10 is excessively high, dispersed bacteria are not generated, and bacteria adhere to the carrier or filamentous bacteria grow. Therefore, the filling rate of the carrier in the first biological treatment tank 10 is 20% or less, desirably 10% or less, for example, 5 to 10% in the case of a fluidized bed and 0.1 to 2% in the case of a rocking fixed bed. By doing so, it becomes possible to produce dispersal bacteria that are not affected by concentration fluctuations and are easy to prey. Further, DO in the first biological treatment tank 10 may be 1 mg / L or less, preferably 0.5 mg / L or less to suppress the growth of filamentous bacteria.
この第一生物処理槽１０の処理水を第二生物処理槽２０に導入し、散気管２３で曝気し、残存している有機成分の酸化分解、分散性細菌の自己分解および微小動物による補食による余剰汚泥の減量化を行う。
The treated water of the first biological treatment tank 10 is introduced into the second biological treatment tank 20 and aerated by an
第二生物処理槽２０では、細菌に比べ増殖速度の遅い微小動物の働きと細菌の自己分解を利用するため、微小動物と細菌が系内に留まるような運転条件および処理装置を用いなければならない。そこで、第二生物処理槽２０には、流動床担体や固定床、揺動性担体を添加することで微小動物の槽内保持量を高めることが好ましい。図２の符号２５は第二生物処理槽２０内の固定床担体を示している。流動床担体は球状、ペレット状、中空筒状、糸状など任意であり、大きさも０．１〜１０ｍｍ程度の径である。材料は天然素材、無機素材、高分子素材等任意である。揺動性固定床担体は、担体の少なくとも一部が、第二生物処理槽２０の底面、側面、上部のいずれかに固定される。形状は糸状、板状、短冊状の任意で、材料は天然素材、無機素材、高分子素材等任意である。
In the second biological treatment tank 20, in order to utilize the action of a micro animal whose growth rate is slower than that of bacteria and the self-degradation of the bacteria, it is necessary to use an operation condition and a treatment device that allow the micro animals and bacteria to stay in the system. . Therefore, it is preferable to increase the amount of micro-animal retained in the second biological treatment tank 20 by adding a fluidized bed carrier, a fixed bed, or a rocking carrier.
第二生物処理槽２０の後段に固液分離装置３０を設け、第二生物処理液を固液分離し、分離した汚泥の少なくとも一部を第二生物処理槽２０内に返送しても良い。この固液分離は、沈殿池、膜分離、上向流分離いずれでも良い。
A solid-
図３〜５は本発明を嫌気処理に適用したフローである。このフローでも、有機性排水は原水槽１を介して第一生物処理槽１０に供給される。第一生物処理槽１０は酸生成槽となり、メタン生成細菌が直接利用できない有機物を有機酸やアルコール等に低分子化する。 3 to 5 are flows in which the present invention is applied to anaerobic processing. Even in this flow, the organic waste water is supplied to the first biological treatment tank 10 through the raw water tank 1. The first biological treatment tank 10 becomes an acid generation tank, and lowers the organic matter that cannot be directly used by the methanogenic bacteria to an organic acid, alcohol, or the like.
第一生物処理槽（酸生成槽）１０の条件は、空気や酸素で曝気せず、第一生物処理槽１０内を非曝気式の撹拌手段で撹拌する点を除いては上記図２のフローの第一生物処理槽（分散菌槽）１０と同様である。非曝気式の攪拌手段としては、槽内液の循環、槽内ガスの循環、機械攪拌、原水の上向流添加等、任意である。図３〜５では、第一生物処理槽１０内の底部に水中ポンプ１６を設置し、その吐出水の一部を配管１７によって第一生物処理槽１０の上部に流出させて槽内を撹拌している。ポンプ吐出水の残部は、返送ライン２を介して原水槽１に返送される。
The conditions of the first biological treatment tank (acid generation tank) 10 are the flow of FIG. 2 except that the first biological treatment tank 10 is not aerated with air or oxygen, and the first biological treatment tank 10 is stirred with a non-aeration type stirring means. This is the same as the first biological treatment tank (dispersed bacteria tank) 10. As the non-aeration type stirring means, circulation of the liquid in the tank, circulation of the gas in the tank, mechanical stirring, upward addition of raw water, etc. are optional. 3-5, the
第一生物処理槽（酸生成槽）１０で生成した有機酸やアルコール等を含む第一生物処理水は、第二生物処理槽（メタン生成槽）２０に導入され、有機酸、アルコール等がメタンに変換される。メタン生成細菌は、酸生成細菌より増殖速度が遅いため、第二生物処理槽２０では高濃度で菌体を維持する必要がある。そのため、第二生物処理槽２０では、グラニュール法、担体法（流動床、固定床いずれでも可）など生物膜法を採用するのが好ましい。これらの処理法の場合、図３〜５の通り、第一生物処理水は第二生物処理槽２０の下部又は中継槽４０に導入される。
即ち、図３においては、第一生物処理水は中継槽４０を経て第二生物処理槽２０の下部に導入される。第二生物処理槽２０内の上部にはＧＳＳ（気固液分離装置）２６が設けられており、分離ガスが系外へ排出されると共に、分離水の一部が処理水として取り出され、残部は中継槽４０に循環される。また、第二生物処理槽２０の下部からは余剰汚泥が引き抜かれる。
図４においては、第二生物処理槽２０は流動床担体２２を有する。また、流動床担体２２を分離するためのスクリーンやストレーナなどの担体分離手段２１が設けられており、上部からガスが排出されると共に、担体分離手段２１で担体２２と分離された分離水の一部が処理水として取り出され、残部は中継槽４０に循環される。
図５においては、第二生物処理槽２０の処理水を処理する膜分離装置５０が設けられている。第二生物処理槽２０で発生したガスは上部から排出されると共に、第二生物処理槽２０の処理水は膜分離装置５０で膜分離処理され、分離汚泥は第二生物処理槽２０に返送され、分離水が処理水として取り出される。
The first biological treatment water containing the organic acid and alcohol produced in the first biological treatment tank (acid production tank) 10 is introduced into the second biological treatment tank (methane production tank) 20, and the organic acid, alcohol and the like are methane. Is converted to Since the methanogenic bacteria have a slower growth rate than the acid producing bacteria, it is necessary to maintain the cells at a high concentration in the second biological treatment tank 20. Therefore, in the second biological treatment tank 20, it is preferable to employ a biofilm method such as a granule method or a carrier method (either a fluidized bed or a fixed bed is acceptable). In the case of these treatment methods, the first biological treatment water is introduced into the lower part of the second biological treatment tank 20 or the relay tank 40 as shown in FIGS.
That is, in FIG. 3, the first biological treatment water is introduced into the lower part of the second biological treatment tank 20 through the relay tank 40. A GSS (gas-solid-liquid separator) 26 is provided in the upper part of the second biological treatment tank 20, and the separation gas is discharged out of the system, and part of the separated water is taken out as treated water, and the remainder Is circulated to the relay tank 40. Further, excess sludge is drawn from the lower part of the second biological treatment tank 20.
In FIG. 4, the second biological treatment tank 20 has a
In FIG. 5, the
本発明では、第二生物処理槽２０の後段にさらに生物処理槽やその他の処理手段を設けてもよい。
また、嫌気処理の場合、酸生成槽でのｐＨ調整剤の使用量削減のため、ＧＳＳや膜分離の処理液（図３の処理水又は図５の処理水）、担体を用いる場合はスクリーンにより担体が分離された処理液（図４の処理水）を第一生物処理槽に返送してもよい。
In the present invention, a biological treatment tank and other treatment means may be further provided in the subsequent stage of the second biological treatment tank 20.
In the case of anaerobic treatment, in order to reduce the amount of pH adjuster used in the acid generation tank, a GSS or membrane separation treatment liquid (treated water in FIG. 3 or treated water in FIG. 5) or a carrier is used. The treatment liquid (treated water in FIG. 4) from which the carrier has been separated may be returned to the first biological treatment tank.
以下、実施例及び比較例について説明する。 Hereinafter, examples and comparative examples will be described.
［実施例１（フロー：図２）］
図２のフローにより、飲料水系排水（ＣＯＤｃｒ＝８００ｍｇ／Ｌ、ＳＳ＝０ｍｇ／Ｌ）を処理した。
[Example 1 (flow: FIG. 2)]
The drinking water drainage (CODcr = 800 mg / L, SS = 0 mg / L) was treated by the flow of FIG.
容量５０Ｌの原水槽１と、容量２５Ｌの第一生物処理槽（分散菌槽：汚泥返送なし）と、容量１５０Ｌの第二生物処理槽（活性汚泥槽）２０と沈殿槽３０を図２の通り接続した。ＣＯＤｃｒ容積負荷２．３ｋｇ／ｍ３／ｄａｙ、水量５００Ｌ／ｄａｙ、第一生物処理槽ＨＲＴ１．２時間の条件で運転した。第一生物処理槽１０及び第二生物処理槽２０に板状の固定床担体１５，２５を充填率１体積％にて充填した。第一生物処理槽１０から槽内液を１０Ｌ／ｄａｙにて原水槽１へ返送した。原水槽１では、曝気攪拌を行った。
The raw water tank 1 with a capacity of 50 L, the first biological treatment tank with a capacity of 25 L (dispersed bacteria tank: no sludge return), the second biological treatment tank (active sludge tank) 20 with a capacity of 150 L and the
その結果、第一生物処理槽１０出口の溶解性ＣＯＤｃｒ濃度は１００ｍｇ／Ｌとなり、溶解性ＣＯＤｃｒ除去率は８７．５％に達し、良好な分散菌が生成した。汚泥転換率は０．１ｋｇ−ＳＳ／ｋｇ−ＣＯＤｃｒと非常に低い汚泥発生量となった。 As a result, the soluble CODcr concentration at the outlet of the first biological treatment tank 10 was 100 mg / L, the soluble CODcr removal rate reached 87.5%, and good dispersal bacteria were produced. The sludge conversion rate was 0.1 kg-SS / kg-CODcr and a very low sludge generation amount.
［比較例１］
第一生物処理槽内容液の原水槽１への返送を行わないこと以外は実施例１と同様にして試験を行った。その結果、第一生物処理槽１０出口の溶解性ＣＯＤｃｒ濃度は５００ｍｇ／Ｌで、溶解性ＣＯＤｃｒ除去率は３７．５％に留まり、多量の糸状性細菌が生成した。そのため、沈殿槽３０では沈降不良を起こし、安定して処理することが出来なかった。汚泥は大量に引き抜く必要があり、汚泥転換率は０．３５ｋｇ−ＳＳ／ｋｇ−ＣＯＤｃｒと非常に高い汚泥発生量となった。
[Comparative Example 1]
The test was performed in the same manner as in Example 1 except that the liquid in the first biological treatment tank was not returned to the raw water tank 1. As a result, the soluble CODcr concentration at the outlet of the first biological treatment tank 10 was 500 mg / L, the soluble CODcr removal rate remained at 37.5%, and a large amount of filamentous bacteria were produced. Therefore, the
［実施例２（フロー：図３）］
図３のフローにより、飲料水系排水（ＣＯＤｃｒ＝１５００ｍｇ／Ｌ、ＳＳ＝０ｍｇ／Ｌ）の処理を行った。
[Example 2 (flow: FIG. 3)]
According to the flow of FIG. 3, drinking water drainage (CODcr = 1500 mg / L, SS = 0 mg / L) was processed.
容量５０Ｌの原水槽１と、容量２５Ｌの第一生物処理槽（酸生成槽：汚泥返送なし）１０と、容量５０Ｌの第二生物処理槽（メタン生成槽（ＵＡＳＢ槽））２０とを図３の通り中継槽４０を介して接続した。ＣＯＤｃｒ容積負荷１０ｋｇ／ｍ３／ｄａｙ、水量５００Ｌ／ｄａｙ、第一生物処理槽ＨＲＴ１．２ｈの条件で運転した。第二生物処理槽（ＵＡＳＢ槽）２０にはグラニュールが槽容積で５０％維持されていた。第一生物処理槽１０から槽内液を２０Ｌ／ｄａｙとなるように原水槽１へ返送した。なお、原水槽１は機械攪拌とした。 FIG. 3 shows a raw water tank 1 with a capacity of 50 L, a first biological treatment tank with a capacity of 25 L (acid generation tank: no sludge return) 10 and a second biological treatment tank with a capacity of 50 L (methane production tank (UASB tank)). As shown in FIG. The operation was performed under the conditions of a CODcr volumetric load of 10 kg / m 3 / day, a water volume of 500 L / day, and a first biological treatment tank HRT1.2h. In the second biological treatment tank (UASB tank) 20, 50% of the granules were maintained in the tank volume. The liquid in the tank was returned from the first biological treatment tank 10 to the raw water tank 1 so as to be 20 L / day. The raw water tank 1 was mechanically stirred.
その結果、第一生物処理槽１０出口の溶解性ＣＯＤｃｒ濃度に占める有機酸の割合は１００ｍｇ／Ｌ（１５００ｍｇ／Ｌ中）から１０００ｍｇ／Ｌ（１３００ｍｇ／Ｌ中）に上昇し、酸生成が良好に進行した。第二生物処理槽（ＵＡＳＢ槽）２０では生成した有機酸の９５％がメタンに変換され、原水中の溶解性有機物の８０％が最終的にメタンに変換され、良好な処理が維持された。 As a result, the ratio of the organic acid in the soluble CODcr concentration at the outlet of the first biological treatment tank 10 increases from 100 mg / L (in 1500 mg / L) to 1000 mg / L (in 1300 mg / L), and the acid generation is good. Progressed. In the second biological treatment tank (UASB tank) 20, 95% of the generated organic acid was converted to methane, and 80% of the soluble organic matter in the raw water was finally converted to methane, and good treatment was maintained.
［比較例２］
第一生物処理槽１０内容液の原水槽１への返送を行わないこと以外は実施例２と同様の運転を行った。その結果、第一生物処理槽１０出口の溶解性ＣＯＤｃｒ濃度に占める有機酸の割合は１００ｍｇ／Ｌ（１５００ｍｇ／Ｌ中）から３００ｍｇ／Ｌ（１４００ｍｇ／Ｌ中）まで上昇しただけであり、酸生成が殆ど進行せず、後段のＵＡＳＢ槽２０ではグラニュールの浮上が頻発した。そのため、全体での溶解性有機物の除去率は４０％に留まった。
[Comparative Example 2]
The same operation as in Example 2 was performed, except that the content of the first biological treatment tank 10 was not returned to the raw water tank 1. As a result, the ratio of the organic acid in the soluble CODcr concentration at the outlet of the first biological treatment tank 10 only increased from 100 mg / L (in 1500 mg / L) to 300 mg / L (in 1400 mg / L), and acid generation Hardly progressed, and granule flotation frequently occurred in the UASB tank 20 in the subsequent stage. Therefore, the removal rate of soluble organic substances as a whole remained at 40%.
以上の実施例及び比較例より、本発明によると、有機性排水の効率的な生物処理が可能になり、槽容積削減の効果があることが認められた。 From the above Examples and Comparative Examples, it was confirmed that according to the present invention, an efficient biological treatment of organic wastewater is possible and there is an effect of reducing the tank volume.
１ 原水槽
１０ 第一生物処理槽
１１，２１ 担体分離手段
１２，２２ 流動床担体
１５，２５、 固定床担体
２６ ＧＳＳ
２０ 第二生物処理槽
３０ 固液分離装置
４０ 中継槽
５０ 膜分離装置
DESCRIPTION OF SYMBOLS 1 Raw water tank 10 1st
20 Second
Claims (7)
該原水槽から有機性排水が導入され、細菌により生物処理されて第一生物処理水が生成する第一生物処理槽と、
第一生物処理水が導入され、生物処理されて第二生物処理水が生成する第二生物処理槽と
を有する有機性排水の生物処理装置において、
第二生物処理槽又はその下流側から第一生物処理槽又はその上流側への汚泥混合液及び／又は分離汚泥の返送手段を具備せず、
第一生物処理槽内容液又は第一生物処理水を原水流量に対し２０％以下の割合で原水槽に返送する返送ラインを具備したことを特徴とする有機性排水の生物処理装置。 A raw water tank in which organic wastewater is stored;
A first biological treatment tank in which organic wastewater is introduced from the raw water tank and biologically treated by bacteria to produce first biological treated water;
In the biological treatment apparatus for organic wastewater having the second biological treatment tank into which the first biological treatment water is introduced and biologically treated to produce the second biological treatment water,
It does not have a means for returning the sludge mixture and / or separated sludge from the second biological treatment tank or its downstream side to the first biological treatment tank or its upstream side,
A biological treatment apparatus for organic wastewater, comprising a return line for returning the first biological treatment tank contents liquid or the first biological treatment water to the raw water tank at a rate of 20% or less with respect to the raw water flow rate.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP6195000B1 (en) * | 2016-09-23 | 2017-09-13 | 栗田工業株式会社 | Biological treatment method for organic wastewater |
| JP2017159204A (en) * | 2016-03-08 | 2017-09-14 | 住友重機械エンバイロメント株式会社 | Water treatment equipment and operation method thereof |
| JP2017159243A (en) * | 2016-03-09 | 2017-09-14 | 荏原実業株式会社 | Biological treatment equipment and biological treatment method for organic waste water |
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|---|---|---|---|---|
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Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS585194A (en) * | 1981-06-29 | 1983-01-12 | Matsushita Electric Works Ltd | Methane gas fermentation method |
| JPH05123693A (en) * | 1991-11-06 | 1993-05-21 | Japan Organo Co Ltd | Disposal equipment for organic drainage by anaerobic microorganism |
| JP2000271593A (en) * | 1999-03-24 | 2000-10-03 | Ebara Corp | Anaerobic treatment method of grease-containing waste water |
| JP2001038378A (en) * | 1999-07-29 | 2001-02-13 | Sumitomo Heavy Ind Ltd | Method and device for anaerobically treating organic waste water |
| JP2001137887A (en) * | 1999-11-10 | 2001-05-22 | Hitachi Plant Eng & Constr Co Ltd | Anaerobic biological treating method |
| JP2004298678A (en) * | 2003-03-28 | 2004-10-28 | Asahi Breweries Ltd | Microorganism group efficiently performing acid production in anaerobic treatment for sugar-based waste water |
| JP2006247566A (en) * | 2005-03-11 | 2006-09-21 | Kurita Water Ind Ltd | Biological treatment method for organic waste water |
| JP2007253003A (en) * | 2006-03-22 | 2007-10-04 | Tokyo Metropolis | Method for estimating quality of inflow sewage by eluting phosphorus from activated sludge, nutritional source addition unit in advanced sewage treatment system and advanced sewage treatment system |
| JP2009066505A (en) * | 2007-09-12 | 2009-04-02 | Univ Waseda | Method of forming aerobic granule, water treatment method and water treatment apparatus |
| JP2010063974A (en) * | 2008-09-09 | 2010-03-25 | Sumitomo Heavy Industries Environment Co Ltd | Anaerobic treatment apparatus and anaerobic treatment method |
| JP2013236996A (en) * | 2012-05-14 | 2013-11-28 | Hitachi Ltd | Water treatment process |
-
2014
- 2014-04-10 JP JP2014081154A patent/JP6442856B2/en active Active
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS585194A (en) * | 1981-06-29 | 1983-01-12 | Matsushita Electric Works Ltd | Methane gas fermentation method |
| JPH05123693A (en) * | 1991-11-06 | 1993-05-21 | Japan Organo Co Ltd | Disposal equipment for organic drainage by anaerobic microorganism |
| JP2000271593A (en) * | 1999-03-24 | 2000-10-03 | Ebara Corp | Anaerobic treatment method of grease-containing waste water |
| JP2001038378A (en) * | 1999-07-29 | 2001-02-13 | Sumitomo Heavy Ind Ltd | Method and device for anaerobically treating organic waste water |
| JP2001137887A (en) * | 1999-11-10 | 2001-05-22 | Hitachi Plant Eng & Constr Co Ltd | Anaerobic biological treating method |
| JP2004298678A (en) * | 2003-03-28 | 2004-10-28 | Asahi Breweries Ltd | Microorganism group efficiently performing acid production in anaerobic treatment for sugar-based waste water |
| JP2006247566A (en) * | 2005-03-11 | 2006-09-21 | Kurita Water Ind Ltd | Biological treatment method for organic waste water |
| JP2007253003A (en) * | 2006-03-22 | 2007-10-04 | Tokyo Metropolis | Method for estimating quality of inflow sewage by eluting phosphorus from activated sludge, nutritional source addition unit in advanced sewage treatment system and advanced sewage treatment system |
| JP2009066505A (en) * | 2007-09-12 | 2009-04-02 | Univ Waseda | Method of forming aerobic granule, water treatment method and water treatment apparatus |
| JP2010063974A (en) * | 2008-09-09 | 2010-03-25 | Sumitomo Heavy Industries Environment Co Ltd | Anaerobic treatment apparatus and anaerobic treatment method |
| JP2013236996A (en) * | 2012-05-14 | 2013-11-28 | Hitachi Ltd | Water treatment process |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2017159204A (en) * | 2016-03-08 | 2017-09-14 | 住友重機械エンバイロメント株式会社 | Water treatment equipment and operation method thereof |
| JP2017159243A (en) * | 2016-03-09 | 2017-09-14 | 荏原実業株式会社 | Biological treatment equipment and biological treatment method for organic waste water |
| JP6195000B1 (en) * | 2016-09-23 | 2017-09-13 | 栗田工業株式会社 | Biological treatment method for organic wastewater |
| JP2018047431A (en) * | 2016-09-23 | 2018-03-29 | 栗田工業株式会社 | Biotreatment method of organic waste water |
| WO2018055793A1 (en) * | 2016-09-23 | 2018-03-29 | 栗田工業株式会社 | Biological treatment method for organic wastewater |
| KR20190053833A (en) | 2016-09-23 | 2019-05-20 | 쿠리타 고교 가부시키가이샤 | Biological treatment of organic wastewater |
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|---|---|
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