JP2002336890A - Method and device for treating organic effluent - Google Patents
Method and device for treating organic effluentInfo
- Publication number
- JP2002336890A JP2002336890A JP2001149774A JP2001149774A JP2002336890A JP 2002336890 A JP2002336890 A JP 2002336890A JP 2001149774 A JP2001149774 A JP 2001149774A JP 2001149774 A JP2001149774 A JP 2001149774A JP 2002336890 A JP2002336890 A JP 2002336890A
- Authority
- JP
- Japan
- Prior art keywords
- tank
- ozone
- sludge
- biological
- inner cylinder
- 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
- Degasification And Air Bubble Elimination (AREA)
- Activated Sludge Processes (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Treatment Of Sludge (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、汚水などの有機性
排水の生物処理方法及び装置に関するもので、詳細に
は、オゾンを用い有機性汚泥を可溶化処理するととも
に、有機性排水（以下「原水」ともいう）のアンモニア
性窒素の硝化を促進する新規な有機性排水の処理方法及
び装置に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and an apparatus for biologically treating organic wastewater such as wastewater. More specifically, the present invention relates to a method for solubilizing organic sludge using ozone and an organic wastewater (hereinafter referred to as "organic wastewater"). The present invention also relates to a novel organic wastewater treatment method and apparatus for promoting the nitrification of ammonia nitrogen in raw water.
【０００２】[0002]
【従来の技術】有機性排水処理の生物処理に関して、処
理により排出される余剰汚泥をオゾン処理槽でオゾンに
より液化処理を行い、減容化する技術が知られている。
これは、オゾンの持つ酸化力により、活性汚泥中の微生
物の細胞膜を破壊し、内部の細胞質を細胞外に流出させ
るものである。しかし、従来の技術は、オゾン処理槽で
生物汚泥の可溶化を進行させることができるだけであっ
た。また、従来のオゾン処理槽は、オゾンガスを有機性
排水や活性汚泥混合液に供給する反応槽には、上部に消
泡機、下部にオゾン吹き込み口が設けられた、単純な形
状の容器が用いられることが多かった。そのため、オゾ
ンによる余剰汚泥の液化効率が低いという問題もあっ
た。2. Description of the Related Art With respect to biological treatment of organic wastewater treatment, there is known a technique for reducing the volume of excess sludge discharged by treatment by liquefaction with ozone in an ozone treatment tank.
In this method, the cell membrane of microorganisms in activated sludge is destroyed by the oxidizing power of ozone, and the cytoplasm inside is discharged outside the cells. However, the prior art was only able to advance the solubilization of biological sludge in the ozonation tank. In addition, a conventional ozone treatment tank uses a simple vessel having a defoamer at an upper portion and an ozone blowing port at a lower portion in a reaction tank for supplying ozone gas to an organic wastewater or an activated sludge mixture. Was often done. Therefore, there was a problem that the liquefaction efficiency of the excess sludge due to ozone was low.
【０００３】[0003]
【発明が解決しようとする課題】本発明は、このような
従来の課題に鑑みてなされたものであり、オゾン処理槽
で生物汚泥の可溶化と、アンモニア性窒素の硝化反応を
同時に進行させ、かつこれらの作用を高めることができ
る技術を提供するものである。DISCLOSURE OF THE INVENTION The present invention has been made in view of the above-mentioned conventional problems, and the present invention simultaneously promotes solubilization of biological sludge and nitrification reaction of ammonia nitrogen in an ozone treatment tank. Further, the present invention provides a technique capable of enhancing these effects.
【０００４】[0004]
【課題を解決するための手段】上記の課題は、下記の構
成からなる本発明によって解決される。 （１）有機性排水を生物処理工程で処理する有機性排水
の処理方法において、アンモニア性窒素を含有する有機
性排水の生物処理工程からの生物汚泥と前記有機性排水
の少なくとも一部を、槽の内部に内筒又は仕切板を設
け、内筒又は仕切板を介して上昇・下降の循環水流を生
起させ、かつオゾン含有ガスを上昇流部の下部に吹き込
むことによって、槽内で生物汚泥の可溶化とアンモニア
性窒素の生物学的硝化を共に進行させるオゾン処理槽で
オゾン処理した後、前記生物処理工程に供給することを
特徴とする有機性排水の処理方法。 （２）前記オゾン処理槽からの流出汚泥スラリを、有機
性排水の生物処理工程の生物学的脱窒素部に供給するこ
とを特徴とする前記（１）記載の有機性排水の処理方
法。The above object is achieved by the present invention having the following constitution. (1) A method of treating organic wastewater in a biological treatment step, wherein biological sludge from the biological treatment step of organic wastewater containing ammonia nitrogen and at least a part of the organic wastewater are placed in a tank. Of the biological sludge in the tank by providing an inner cylinder or a partition plate inside the inside, generating an ascending or descending circulating water flow through the inner cylinder or the partition plate, and blowing the ozone-containing gas into the lower part of the ascending flow section. A method for treating organic wastewater, comprising: performing ozone treatment in an ozone treatment tank that promotes both solubilization and biological nitrification of ammonia nitrogen, and then supplying the ozone treatment to the biological treatment step. (2) The method for treating organic wastewater according to (1), wherein the sludge slurry discharged from the ozone treatment tank is supplied to a biological denitrification unit in a biological treatment step for organic wastewater.
【０００５】（３）槽の内部に内筒又は仕切板を設け、
かつアンモニア性窒素を含有する有機性排水を導入する
入口を槽の上部に、オゾンガスの入口を槽の下部に、生
物処理槽の返送汚泥を導入する入口を槽の上部又は下部
に設けて、槽内部に内筒又は仕切板を介して上昇流部及
び下降流部の循環水流部が形成され、槽頂部に消泡機構
を具備したことを特徴とするオゾン処理槽。 （４）槽の内部に内筒又は仕切板を設け、かつアンモニ
ア性窒素を含有する有機性排水の少なくとも一部を導入
する入口を槽の上部に、オゾンガスの入口を槽の下部
に、生物処理槽の返送汚泥を導入する入口を槽の上部又
は下部に設けて、槽内部に内筒又は仕切板を介して上昇
流部及び下降流部の循環水流部が形成され、槽頂部に消
泡機構を具備したオゾン処理槽と、前記有機性排水の残
部と前記オゾン処理槽からの流出汚泥スラリを導入する
生物処理槽と、その後段の沈殿槽と、沈殿槽底の汚泥を
生物処理槽及びオゾン処理槽へ送る配管とを有すること
を特徴とする有機性排水の処理装置。(3) An inner cylinder or a partition plate is provided inside the tank,
In addition, an inlet for introducing organic wastewater containing ammonia nitrogen is provided at the upper part of the tank, an inlet for ozone gas is provided at the lower part of the tank, and an inlet for introducing return sludge of the biological treatment tank is provided at the upper or lower part of the tank. An ozone treatment tank, wherein a circulating water flow section of an upflow section and a downflow section is formed through an inner cylinder or a partition plate therein, and a defoaming mechanism is provided at the top of the tank. (4) An internal cylinder or a partition plate is provided inside the tank, and an inlet for introducing at least a part of the organic wastewater containing ammoniacal nitrogen is provided at the upper part of the tank, and an ozone gas inlet is provided at the lower part of the tank. An inlet for introducing the return sludge of the tank is provided at the upper or lower part of the tank, and a circulating water flow part of an ascending flow part and a descending flow part is formed inside the tank through an inner cylinder or a partition plate, and a defoaming mechanism is provided at the top of the tank. , A biological treatment tank for introducing the remainder of the organic wastewater and the sludge slurry flowing out of the ozone treatment tank, a sedimentation tank at the subsequent stage, and a biological treatment tank and ozone A system for treating organic wastewater, comprising: a pipe for sending to a treatment tank.
【０００６】[0006]
【発明の実施の形態】本発明の実施の形態を、図面を参
照して詳細に説明する。図１は、本発明のオゾン接触槽
を用いて処理を行う場合におけるオゾン接触槽の一例を
示す略立面図である。図１に示す本装置は、オゾン接触
槽１の内側に上下が開口した内筒２を設けた場合の一例
である。前記内筒２は、オゾン接触槽１の内壁と間隔が
開けてあり、内筒２の内側が上昇流部を構成し、内筒２
とオゾン接触槽１の内壁との間が下降流部を構成してい
る。内筒２の下端は槽１の液内にあって槽１の底面と間
隔が開けられており、また内筒２の上端は槽１の液面よ
り下にあってもよいし、あるいは液の上昇流れの形成を
妨げるような水柱ができない程度であれば液面より多少
上にあってもよい。Embodiments of the present invention will be described in detail with reference to the drawings. FIG. 1 is a schematic elevation view showing an example of an ozone contact tank when performing a process using the ozone contact tank of the present invention. The present apparatus shown in FIG. 1 is an example in which an inner cylinder 2 having upper and lower openings is provided inside an ozone contact tank 1. The inner cylinder 2 is spaced from the inner wall of the ozone contact tank 1, and the inside of the inner cylinder 2 constitutes an upflow portion.
And the inner wall of the ozone contact tank 1 constitute a downward flow portion. The lower end of the inner cylinder 2 is in the liquid of the tank 1 and is spaced apart from the bottom surface of the tank 1, and the upper end of the inner cylinder 2 may be below the liquid level of the tank 1, or It may be slightly above the liquid level as long as a water column that prevents the formation of the upward flow cannot be formed.
【０００７】生物処理工程からの活性汚泥は、流入汚泥
６として、オゾン接触槽１の下降流部に供給される。オ
ゾン接触槽１に原水の一部７を供給すると、オゾンによ
る余剰汚泥処理において減容化効率を上げることができ
る。オゾンガス１１は、槽１の内筒２の下端より下方に
供給され、気泡となって内筒２内部を上昇する際に気液
混合物を形成し、これは軽いために内筒２内部を上昇
し、いわゆるエアリフト作用により、上昇流を形成し、
内筒２の上端は槽１の液面より下にあるときには、気液
混合物は内筒２の上端から槽１の内壁に拡がり、そこで
ガスは液面の上方に分離し、液は下降流部に入って内筒
２の下端に戻り、これにより液の循環流を形成する。内
筒２の上端が槽１の液面より上にあるときでも、上昇流
が強ければ内筒２の上端からいつ流して同様に循環流が
形成される。オゾンガス１１の供給だけでは、液上昇流
を形成が十分形成できないことが多いので、液の循環ラ
インを設け、循環ポンプで槽１内の液を内筒２の下端に
上昇流が形成されるように供給することが好ましい。そ
の例が、図１の汚泥循環ポンプ１０を備えた汚泥循環ラ
イン９である。The activated sludge from the biological treatment step is supplied to the downflow section of the ozone contact tank 1 as inflow sludge 6. When a part of the raw water 7 is supplied to the ozone contact tank 1, the volume reduction efficiency can be increased in the treatment of excess sludge with ozone. The ozone gas 11 is supplied below the lower end of the inner cylinder 2 of the tank 1 and forms a gas-liquid mixture when it rises inside the inner cylinder 2 as bubbles and rises inside the inner cylinder 2 because it is light. With the so-called air lift effect, an upward flow is formed,
When the upper end of the inner cylinder 2 is below the liquid level of the tank 1, the gas-liquid mixture spreads from the upper end of the inner cylinder 2 to the inner wall of the tank 1, where the gas separates above the liquid level and the liquid flows downward. And returns to the lower end of the inner cylinder 2 to form a circulating flow of liquid. Even when the upper end of the inner cylinder 2 is above the liquid level of the tank 1, if the ascending flow is strong, it flows from the upper end of the inner cylinder 2 at any time to form a circulating flow. Since the supply of the ozone gas 11 alone is often not enough to form the liquid rising flow, a liquid circulation line is provided so that the liquid in the tank 1 is formed at the lower end of the inner cylinder 2 by the circulation pump. Preferably. An example is the sludge circulation line 9 provided with the sludge circulation pump 10 of FIG.
【０００８】この場合、汚泥循環ポンプ１０により槽１
内の汚泥及び液が循環する汚泥循環ライン９上に設けら
れたエジェクタ３により、オゾンガス１１はオゾン接触
槽内の汚泥中に溶解する。エジェクタ３はオゾンガスと
液体あるいは汚泥との混合接触を著しく高める作用を有
する。オゾン１１が溶解した汚泥は、オゾン接触槽１の
下部の中心部よりオゾン反応槽１に吹き込まれた状態と
なり、内筒２の内部を上昇し、内筒２の外側を降下する
循環流を形成する。オゾン接触槽１には、オゾン接触槽
流出口が設けられており、ここからオーバーフローした
汚泥スラリ８が流出する。オゾン接触槽１頂部には、反
応後のガスを排出するための排ガス（排オゾンガス）１
２の出口が設けられており、ここから反応後の排ガス１
２を排出する。オゾン接触槽１内では、オゾン１１によ
る汚泥液化処理により発泡するが、この泡がオゾン接触
排ガス出口より吹き出すことを防ぐため、消泡機４及び
消泡機用電動機５が設置されており、オゾン接触槽１内
部で発生した泡を消泡する。In this case, the sludge circulation pump 10 controls the tank 1
The ozone gas 11 is dissolved in the sludge in the ozone contact tank by the ejector 3 provided on the sludge circulation line 9 through which the sludge and the liquid circulate. The ejector 3 has a function of significantly increasing the mixed contact between the ozone gas and the liquid or the sludge. The sludge in which the ozone 11 has been dissolved is blown into the ozone reaction tank 1 from the center of the lower part of the ozone contact tank 1, and forms a circulating flow that rises inside the inner cylinder 2 and descends outside the inner cylinder 2. I do. The ozone contact tank 1 is provided with an ozone contact tank outlet, from which the overflowing sludge slurry 8 flows out. At the top of the ozone contact tank 1, exhaust gas (exhaust ozone gas) 1 for discharging gas after the reaction is placed.
2 outlets, from which the exhaust gas 1 after the reaction
Discharge 2. In the ozone contact tank 1, foaming is caused by sludge liquefaction treatment with ozone 11, but in order to prevent the foam from blowing out from the ozone contact exhaust gas outlet, a defoaming machine 4 and a motor for defoaming machine 5 are installed. The foam generated inside the contact tank 1 is eliminated.
【０００９】このオゾン接触槽１では、吹き込まれるオ
ゾンガスは、その製造に際して高濃度酸素ガスを原料と
している関係で、オゾンの他にかなり濃度の高い酸素を
含有しており、オゾン接触槽１の上昇流部での汚泥及び
有機性排水との混合物との接触の際に、液中にかなりの
酸素が溶解し、液面に上昇した際の脱気現象の際にも溶
解した酸素の濃度は高いものとなる。そして、この溶解
した酸素は、有機性排水中のアンモニア性窒素に対して
酸化作用を有するので、下降流部及び上昇流部におい
て、その酸化作用を行い、つまりアンモニア性窒素に対
して硝化作用をする。高濃度酸素を原料としないオゾン
ガスを供給しても良いが、望ましくは高濃度酸素を原料
としたオゾンガスの方がより効果を期待できる。また、
オゾン接触槽１の上部から排出される少量のオゾンを含
有する排ガス１２は、ある程度の酸素ガスを含有するの
で、図２の生物処理槽１３の曝気用空気１５に混合して
利用することが好ましい。なお、前記内筒２の代わりに
仕切板を用いてオゾン接触槽１内部を区画して、上昇流
部と下降流部を形成するようにしても、内筒２を設置し
た場合と同様の効果を得ることができる。この方が構造
が簡単で工作が容易である。In the ozone contact tank 1, the ozone gas to be blown in contains high-concentration oxygen in addition to ozone because high-concentration oxygen gas is used as a raw material in the production thereof. Considerable oxygen dissolves in the liquid upon contact with sludge and organic wastewater in the stream, and the concentration of dissolved oxygen is high even during degassing when rising to the liquid level. It will be. Since the dissolved oxygen has an oxidizing effect on the ammonia nitrogen in the organic wastewater, the oxidizing effect is performed in the downflow section and the upflow section, that is, the nitrification action is performed on the ammonia nitrogen. I do. Although ozone gas not using high-concentration oxygen as a raw material may be supplied, desirably, ozone gas using high-concentration oxygen as a raw material can be more effective. Also,
Since the exhaust gas 12 containing a small amount of ozone discharged from the upper part of the ozone contact tank 1 contains a certain amount of oxygen gas, it is preferable to mix and use it with the aeration air 15 of the biological treatment tank 13 in FIG. . Even if the inside of the ozone contact tank 1 is partitioned by using a partition plate instead of the inner cylinder 2 to form an ascending flow portion and a descending flow portion, the same effect as when the inner cylinder 2 is installed is obtained. Can be obtained. This has a simple structure and is easy to work.
【００１０】[0010]
【実施例】以下において、本発明を実施例によりさらに
具体的に説明するが、本発明は、この実施例により限定
されるものではない。実施例及び比較例を説明するため
の全図において、同一機能を有するものは同一符号を付
け、その繰り返しの説明は省略する。EXAMPLES Hereinafter, the present invention will be described more specifically with reference to examples, but the present invention is not limited to these examples. In all the drawings for explaining the examples and comparative examples, those having the same functions are denoted by the same reference numerals, and their repeated description will be omitted.
【００１１】実施例１ この実施例１においては、図１に示す構造のオゾン接触
槽を用いて、余剰汚泥のオゾン１１による減容化処理を
行った例を示している。本実施例では、図２に示すよう
な団地下水の活性汚泥処理プロセスに、オゾン接触槽１
を組み込んで検討を行った。団地下水７は生物処理槽１
３に供給され、活性汚泥処理される。活性汚泥混合液１
６は沈殿池１７へ供給され、固液分離した後、上澄み水
は処理水１８として放流される。固液分離された活性汚
泥は返送汚泥１９として再び生物処理槽１３に返送され
る。この返送汚泥１９の一部を、オゾン接触槽１に供給
する。また、オゾン接触槽１には原水７の一部やオゾン
発生器２０からのオゾンガス１１が供給される。オゾン
接触槽１で活性汚泥混合液は液化処理された後、オゾン
接触槽流出液８として生物処理槽１３に返送される。オ
ゾン接触槽１からの排ガス１２は残留オゾンを除く処理
をした後、大気中に放出される。第１表に生物処理槽の
運転条件を示す。Embodiment 1 In this embodiment 1, an example is shown in which the volume of excess sludge is reduced by ozone 11 using an ozone contact tank having the structure shown in FIG. In this embodiment, the ozone contact tank 1 is used for the activated sludge treatment process of the groundwater as shown in FIG.
The study was conducted by incorporating. Groundwater 7 is biological treatment tank 1
3 to be treated with activated sludge. Activated sludge mixture 1
6 is supplied to a sedimentation basin 17 and solid-liquid separated, after which the supernatant water is discharged as treated water 18. The activated sludge separated into solid and liquid is returned to the biological treatment tank 13 again as returned sludge 19. A part of the returned sludge 19 is supplied to the ozone contact tank 1. Further, a part of the raw water 7 and the ozone gas 11 from the ozone generator 20 are supplied to the ozone contact tank 1. After the activated sludge mixture is liquefied in the ozone contact tank 1, it is returned to the biological treatment tank 13 as the ozone contact tank effluent 8. The exhaust gas 12 from the ozone contact tank 1 is released into the atmosphere after the treatment for removing residual ozone. Table 1 shows the operating conditions of the biological treatment tank.
【００１２】[0012]
【表１】 [Table 1]
【００１３】第２表にオゾン接触槽１の運転条件を示
す。また、第３表にオゾン接触槽１での処理結果を示
す。オゾン接触槽１に供給するオゾンガスのオゾン濃度
が３２ｍｇ／リットルに対し、排ガス１２のオゾン濃度
は０．１ｍｇ／リットル以下であり、供給したオゾンガ
ス１１のオゾンはほぼ利用されたと考えられる。Table 2 shows the operating conditions of the ozone contact tank 1. Table 3 shows the processing results in the ozone contact tank 1. The ozone concentration of the ozone gas supplied to the ozone contact tank 1 was 32 mg / liter, whereas the ozone concentration of the exhaust gas 12 was 0.1 mg / liter or less. It is considered that the ozone of the supplied ozone gas 11 was almost used.
【００１４】[0014]
【表２】 [Table 2]
【００１５】[0015]
【表３】 [Table 3]
【００１６】第３表より、オゾン接触槽の流出汚泥スラ
リ８と活性汚泥混合液（返送汚泥１９＋原水７）を比較
すると、流出汚泥スラリ８ではＭＬＳＳが低下し、各溶
解成分が増加したことから、オゾン接触槽１でのオゾン
処理により、活性汚泥の一部が液化された。また、返送
汚泥１９と原水７の混合液と流出汚泥スラリ８を比較す
ると、アンモニア性窒素の減少と硝酸性窒素の増加が見
られたことから、オゾン接触槽内で硝化反応が進行した
と考えられる。第４表に、原水と処理水の水質を示す。
処理水のＣＯＤ、ＢＯＤが２０ｍｇ／リットル以下であ
り、良好な処理水水質を得ることができた。From Table 3, a comparison between the sludge slurry 8 discharged from the ozone contact tank and the activated sludge mixed liquid (returned sludge 19 + raw water 7) shows that the MLSS of the sludge slurry 8 decreased and the amount of each dissolved component increased. By the ozone treatment in the ozone contact tank 1, a part of the activated sludge was liquefied. Also, comparing the mixed liquid of the returned sludge 19 and the raw water 7 with the effluent sludge 8, it was considered that the nitrification reaction proceeded in the ozone contact tank because the decrease in ammonia nitrogen and the increase in nitrate nitrogen were observed. Can be Table 4 shows the quality of raw water and treated water.
The COD and BOD of the treated water were 20 mg / liter or less, and good treated water quality could be obtained.
【００１７】[0017]
【表４】 [Table 4]
【００１８】生物処理槽１３内の汚泥量の経過を図３に
示す。６０日の連続運転中、生物処理槽１３内の汚泥量
は、ほぼ９ｋｇで安定しており、余剰汚泥の排出をせず
に安定した運転が行えた。The progress of the amount of sludge in the biological treatment tank 13 is shown in FIG. During the continuous operation for 60 days, the amount of sludge in the biological treatment tank 13 was stable at approximately 9 kg, and stable operation was performed without discharging excess sludge.
【００１９】比較例１ 本発明の効果を検討するため、図４に示すように内筒や
仕切板を設けない、単純な形状のオゾン接触槽を用いて
比較実験を行った。処理は実施例１と同じフローを用い
た。第５表に比較例１の生物処理槽の運転条件を示す。Comparative Example 1 In order to examine the effect of the present invention, a comparative experiment was performed using an ozone contact tank having a simple shape without an inner cylinder or a partition plate as shown in FIG. The same flow as in Example 1 was used for the processing. Table 5 shows the operating conditions of the biological treatment tank of Comparative Example 1.
【００２０】[0020]
【表５】 [Table 5]
【００２１】第６表にオゾン接触槽１の運転条件を示
す。また、第７表にオゾン接触槽１での処理結果を示
す。第６表に示すように、比較例１では、オゾン接触槽
１からの排ガス１２にオゾンの残留が見られ、オゾンガ
ス１１が完全に利用されていないと考えられた。また、
第７表より流出汚泥スラリ８と活性汚泥混合液（返送汚
泥１９＋原水７）を比較すると、オゾン接触槽１でのオ
ゾン処理により、活性汚泥の一部が液化されたが、液化
成分の増加量が実施例１と比較して低く、液化しにくく
なったと考えられた。また、返送汚泥１９と原水７の混
合液と、流出汚泥スラリ８を比較すると、アンモニア性
窒素の減少量と硝酸性窒素の増加量が共に小さく、オゾ
ン接触槽１内で硝化反応があまり進行しなかったと考え
られる。Table 6 shows the operating conditions of the ozone contact tank 1. Table 7 shows the processing results in the ozone contact tank 1. As shown in Table 6, in Comparative Example 1, residual ozone was observed in the exhaust gas 12 from the ozone contact tank 1, and it was considered that the ozone gas 11 was not completely used. Also,
From Table 7, comparing the outflow sludge slurry 8 and the activated sludge mixture (returned sludge 19 + raw water 7), a part of the activated sludge was liquefied by the ozone treatment in the ozone contact tank 1, but the increased amount of the liquefied component Was lower than that of Example 1, and it was considered that liquefaction became difficult. Further, comparing the mixed liquid of the returned sludge 19 and the raw water 7 with the outflow sludge 8, both the decrease amount of the ammonia nitrogen and the increase amount of the nitrate nitrogen are small, and the nitrification reaction proceeds very much in the ozone contact tank 1. Probably not.
【００２２】[0022]
【表６】 [Table 6]
【００２３】[0023]
【表７】 [Table 7]
【００２４】比較例１の処理水の結果を第８表に示す。
比較例１では、実施例１と比較して処理水のＳＳとＣＯ
Ｄが増加し、処理水水質が悪化したことが認められた。The results of the treated water of Comparative Example 1 are shown in Table 8.
In Comparative Example 1, the SS and CO of the treated water were compared with those of Example 1.
It was recognized that D increased and the quality of treated water deteriorated.
【００２５】[0025]
【表８】 [Table 8]
【００２６】比較例１での生物処理槽内の汚泥量の経過
を図５に示す。図５に示すように、本比較例では生物処
理槽内の汚泥量は徐々に増加しており、１日当たり約
０．０４ｋｇの割合で汚泥が増加した。比較例１の実験
から、実施例１では処理水水質の向上が見られ、また、
実施例１と比較例１で同じオゾン量を供給したが、実施
例１が比較例１よりも汚泥が減少したと考えられる。The progress of the amount of sludge in the biological treatment tank in Comparative Example 1 is shown in FIG. As shown in FIG. 5, in this comparative example, the amount of sludge in the biological treatment tank gradually increased, and the sludge increased at a rate of about 0.04 kg per day. From the experiment of Comparative Example 1, the quality of the treated water was improved in Example 1;
Although the same ozone amount was supplied in Example 1 and Comparative Example 1, it is considered that sludge was reduced in Example 1 as compared with Comparative Example 1.
【００２７】[0027]
【発明の効果】本発明によれば、排水処理のうち、オゾ
ンを用いた余剰汚泥の減容化処理において、オゾンの利
用効率を上げ、同じ効果を得るためのオゾン量が従来技
術よりも少なくできるため、省エネルギーにつながるこ
とが期待できる。さらに、オゾン接触槽でも硝化反応が
起きるため、生物処理槽で硝化のために必要な曝気動力
を削減でき、この点からも省エネルギーにつながること
が期待できる。According to the present invention, in waste water treatment, in the treatment of reducing excess sludge using ozone, the use efficiency of ozone is increased, and the amount of ozone for obtaining the same effect is smaller than in the prior art. Can be expected to lead to energy savings. Furthermore, since a nitrification reaction also occurs in the ozone contact tank, the aeration power required for nitrification in the biological treatment tank can be reduced, and from this point it can be expected that energy can be saved.
【図１】本発明に係るオゾン接触槽の概略説明図であ
る。FIG. 1 is a schematic explanatory view of an ozone contact tank according to the present invention.
【図２】本発明の有機性排水処理工程のフローシートで
ある。FIG. 2 is a flow sheet of an organic wastewater treatment step of the present invention.
【図３】実施例１における生物処理槽の汚泥量と時間の
経過との関係を示すグラフである。FIG. 3 is a graph showing the relationship between the amount of sludge in a biological treatment tank and the passage of time in Example 1.
【図４】比較例１のオゾン接触槽の概略説明図である。FIG. 4 is a schematic explanatory view of an ozone contact tank of Comparative Example 1.
【図５】比較例１における生物処理槽の汚泥量と時間の
経過との関係を示すグラフである。FIG. 5 is a graph showing the relationship between the amount of sludge in a biological treatment tank and the passage of time in Comparative Example 1.
１ オゾン接触槽（処理槽） ２ 内筒 ３ エジェクタ ４ 消泡機 ５ 消泡機用電動機 ６ 流入汚泥 ７ 原水（団地下水） ８ オゾン接触槽 ９ 汚泥循環ライン １０ 汚泥循環ポンプ １１ オゾンガス １２ 排ガス １３ 生物処理槽 １４ 散気管 １５ 曝気用空気 １６ 活性汚泥混合液 １７ 沈殿池 １８ 処理水 １９ 返送汚泥 ２０ オゾンガス発生器 DESCRIPTION OF SYMBOLS 1 Ozone contact tank (processing tank) 2 Inner cylinder 3 Ejector 4 Defoamer 5 Electric motor for defoamer 6 Inflow sludge 7 Raw water (dan groundwater) 8 Ozone contact tank 9 Sludge circulation line 10 Sludge circulation pump 11 Ozone gas 12 Exhaust gas 13 Biology Treatment tank 14 Air diffuser 15 Aeration air 16 Activated sludge mixture 17 Sedimentation basin 18 Treated water 19 Returned sludge 20 Ozone gas generator
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.7 識別記号 ＦＩ テーマコート゛(参考） Ｃ０２Ｆ 1/78 Ｃ０２Ｆ 1/78 11/06 11/06 Ａ (72)発明者 片岡 克之 東京都大田区羽田旭町11番１号 株式会社 荏原製作所内 (72)発明者 田中 俊博 東京都大田区羽田旭町11番１号 株式会社 荏原製作所内 Ｆターム(参考） 4D011 BA02 4D028 AA08 AC03 AC09 BA00 BD07 BD11 4D050 AA15 AB07 BB02 BD02 BD03 BD06 CA17 4D059 AA05 BC02 BK12 CA28 DA43 4G035 AA01 AB05 ──────────────────────────────────────────────────の Continued on the front page (51) Int.Cl. 7 Identification symbol FI Theme coat ゛ (Reference) C02F 1/78 C02F 1/78 11/06 11/06 A (72) Inventor Katsuyuki Kataoka Haneda, Ota-ku, Tokyo 11-1 Asahicho, EBARA CORPORATION (72) Inventor Toshihiro Tanaka 11-1, Haneda Asahicho, Ota-ku, Tokyo F-term (reference) 4D011 BA02 4D028 AA08 AC03 AC09 BA00 BD07 BD11 4D050 AA15 AB07 BB02 BD02 BD03 BD06 CA17 4D059 AA05 BC02 BK12 CA28 DA43 4G035 AA01 AB05
Claims (4)
機性排水の処理方法において、アンモニア性窒素を含有
する有機性排水の生物処理工程からの生物汚泥と前記有
機性排水の少なくとも一部を、槽の内部に内筒又は仕切
板を設け、内筒又は仕切板を介して上昇・下降の循環水
流を生起させ、かつオゾン含有ガスを上昇流部の下部に
吹き込むことによって、槽内で生物汚泥の可溶化とアン
モニア性窒素の生物学的硝化を共に進行させるオゾン処
理槽でオゾン処理した後、前記生物処理工程に供給する
ことを特徴とする有機性排水の処理方法。1. A method for treating organic wastewater, wherein organic wastewater is treated in a biological treatment step, wherein biological sludge from the biological treatment step of organic wastewater containing ammonia nitrogen and at least a part of the organic wastewater are removed. By providing an inner cylinder or partition plate inside the tank, generating an ascending / descending circulating water flow through the inner cylinder or partition plate, and blowing the ozone-containing gas into the lower part of the ascending flow section, the organism in the tank is A method for treating organic wastewater, wherein the wastewater is subjected to ozone treatment in an ozone treatment tank that promotes both the solubilization of sludge and the biological nitrification of ammoniacal nitrogen, and then supplies the treated wastewater to the biological treatment step.
を、有機性排水の生物処理工程の生物学的脱窒素部に供
給することを特徴とする請求項１記載の有機性排水の処
理方法。2. The method for treating organic wastewater according to claim 1, wherein the sludge slurry discharged from the ozone treatment tank is supplied to a biological denitrification unit in a biological treatment step of organic wastewater.
アンモニア性窒素を含有する有機性排水を導入する入口
を槽の上部に、オゾンガスの入口を槽の下部に、生物処
理槽の返送汚泥を導入する入口を槽の上部又は下部に設
けて、槽内部に内筒又は仕切板を介して上昇流部及び下
降流部の循環水流部が形成され、槽頂部に消泡機構を具
備したことを特徴とするオゾン処理槽。3. An inner cylinder or partition plate is provided inside the tank, and an inlet for introducing organic waste water containing ammonia nitrogen is provided at the upper part of the tank, an ozone gas inlet is provided at the lower part of the tank, and a biological treatment tank is provided. An inlet for introducing return sludge is provided at the upper or lower part of the tank, and a circulating water flow part of an ascending flow part and a descending flow part is formed inside the tank through an inner cylinder or a partition plate, and a defoaming mechanism is provided at the top of the tank. An ozone treatment tank characterized in that:
アンモニア性窒素を含有する有機性排水の少なくとも一
部を導入する入口を槽の上部に、オゾンガスの入口を槽
の下部に、生物処理槽の返送汚泥を導入する入口を槽の
上部又は下部に設けて、槽内部に内筒又は仕切板を介し
て上昇流部及び下降流部の循環水流部が形成され、槽頂
部に消泡機構を具備したオゾン処理槽と、前記有機性排
水の残部と前記オゾン処理槽からの流出汚泥スラリを導
入する生物処理槽と、その後段の沈殿槽と、沈殿槽底の
汚泥を生物処理槽及びオゾン処理槽へ送る配管とを有す
ることを特徴とする有機性排水の処理装置。4. An inner cylinder or a partition plate is provided inside the tank, and an inlet for introducing at least a part of the organic waste water containing ammonia nitrogen is provided at an upper part of the tank, an ozone gas inlet is provided at a lower part of the tank, An inlet for introducing the return sludge of the biological treatment tank is provided at the upper or lower part of the tank, and a circulating water flow section of an upflow section and a downflow section is formed inside the tank via an inner cylinder or a partition plate, and the effluent is discharged at the top of the tank. An ozone treatment tank equipped with a foaming mechanism, a biological treatment tank for introducing the remainder of the organic wastewater and the sludge slurry flowing out of the ozone treatment tank, a sedimentation tank at a subsequent stage, and a biological treatment tank for sludge at the bottom of the sedimentation tank. And a pipe for sending to an ozone treatment tank.
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| JP2001149774A JP3731806B2 (en) | 2001-05-18 | 2001-05-18 | Organic wastewater treatment method and apparatus |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2001149774A JP3731806B2 (en) | 2001-05-18 | 2001-05-18 | Organic wastewater treatment method and apparatus |
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|---|---|
| JP2002336890A true JP2002336890A (en) | 2002-11-26 |
| JP3731806B2 JP3731806B2 (en) | 2006-01-05 |
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| JP2001149774A Expired - Fee Related JP3731806B2 (en) | 2001-05-18 | 2001-05-18 | Organic wastewater treatment method and apparatus |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2006212581A (en) * | 2005-02-04 | 2006-08-17 | Mitsubishi Heavy Ind Ltd | Method for treating organic waste material |
| JP2008018309A (en) * | 2006-07-11 | 2008-01-31 | Yaskawa Electric Corp | Apparatus for treating sludge |
| JP2008093601A (en) * | 2006-10-13 | 2008-04-24 | Ihi Corp | Waste water treatment equipment |
| JP2008221114A (en) * | 2007-03-12 | 2008-09-25 | Yaskawa Electric Corp | Phosphorous separation device, treatment method for phosphorous-containing organic waste water, and device therefor |
| JP2010022992A (en) * | 2008-07-24 | 2010-02-04 | Yaskawa Electric Corp | Method and device for treating organic waste water |
| JP2010247121A (en) * | 2009-04-20 | 2010-11-04 | Japan Organo Co Ltd | Gas-liquid dissolving tank |
| JP2011056461A (en) * | 2009-09-14 | 2011-03-24 | Fuji Koki Kk | Apparatus and method for reducing volume of sludge |
| CN102583936A (en) * | 2012-02-02 | 2012-07-18 | 重庆大学 | Air lift type internal-external double circulation ozone sludge contact reaction device |
| JP2016209800A (en) * | 2015-05-01 | 2016-12-15 | 株式会社安川電機 | Excess sludge weight loss device |
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2001
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2006212581A (en) * | 2005-02-04 | 2006-08-17 | Mitsubishi Heavy Ind Ltd | Method for treating organic waste material |
| JP4667890B2 (en) * | 2005-02-04 | 2011-04-13 | 三菱重工環境・化学エンジニアリング株式会社 | Organic waste treatment methods |
| JP2008018309A (en) * | 2006-07-11 | 2008-01-31 | Yaskawa Electric Corp | Apparatus for treating sludge |
| JP4666228B2 (en) * | 2006-07-11 | 2011-04-06 | 株式会社安川電機 | Sludge treatment equipment |
| JP2008093601A (en) * | 2006-10-13 | 2008-04-24 | Ihi Corp | Waste water treatment equipment |
| JP2008221114A (en) * | 2007-03-12 | 2008-09-25 | Yaskawa Electric Corp | Phosphorous separation device, treatment method for phosphorous-containing organic waste water, and device therefor |
| JP2010022992A (en) * | 2008-07-24 | 2010-02-04 | Yaskawa Electric Corp | Method and device for treating organic waste water |
| JP2010247121A (en) * | 2009-04-20 | 2010-11-04 | Japan Organo Co Ltd | Gas-liquid dissolving tank |
| JP2011056461A (en) * | 2009-09-14 | 2011-03-24 | Fuji Koki Kk | Apparatus and method for reducing volume of sludge |
| CN102583936A (en) * | 2012-02-02 | 2012-07-18 | 重庆大学 | Air lift type internal-external double circulation ozone sludge contact reaction device |
| JP2016209800A (en) * | 2015-05-01 | 2016-12-15 | 株式会社安川電機 | Excess sludge weight loss device |
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