JP2001314887A - Activated sludge treatment apparatus and wastewater treatment system - Google Patents

Activated sludge treatment apparatus and wastewater treatment system

Info

Publication number
JP2001314887A
JP2001314887A JP2000322830A JP2000322830A JP2001314887A JP 2001314887 A JP2001314887 A JP 2001314887A JP 2000322830 A JP2000322830 A JP 2000322830A JP 2000322830 A JP2000322830 A JP 2000322830A JP 2001314887 A JP2001314887 A JP 2001314887A
Authority
JP
Japan
Prior art keywords
sludge
activated sludge
treatment system
tank
activated
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.)
Pending
Application number
JP2000322830A
Other languages
Japanese (ja)
Inventor
Hironori Nakamura
裕紀 中村
Kazuichi Isaka
和一 井坂
Shinji Aso
伸二 麻生
Hiroyoshi Emori
弘祥 江森
Kazunori Sato
一教 佐藤
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Hitachi Plant Technologies Ltd
Mitsubishi Power Ltd
Original Assignee
Babcock Hitachi KK
Hitachi Plant Technologies Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Babcock Hitachi KK, Hitachi Plant Technologies Ltd filed Critical Babcock Hitachi KK
Priority to JP2000322830A priority Critical patent/JP2001314887A/en
Publication of JP2001314887A publication Critical patent/JP2001314887A/en
Pending legal-status Critical Current

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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)
  • Treatment Of Sludge (AREA)

Abstract

PROBLEM TO BE SOLVED: To eliminate the complicatedness of an apparatus and a problem from an aspect of control by a simple means and to suppress the increase of COD in a solution after activated sludge treatment or the extinction of microorganisms in activated sludge to suppress the formation amount of sludge without deteriorating treated water to make an excess sludge amount low or zero. SOLUTION: Activated sludge is pressurized to be ejected into a container 32 under pressure from a nozzle 31 to finely divide a floatable substance constituting activated sludge without almost increasing COD in a solution and almost killing microorganisms in activated sludge to disperse microorganisms. Therefore, by reacting dispersed activated sludge with dissolved oxygen or nitrogen oxide in a digestion tank 3, activated sludge is subjected to autoxidation to be converted to inorganic matter and the volume of activated sludge is reduced.

Description

【発明の詳細な説明】DETAILED DESCRIPTION OF THE INVENTION

【０００１】[0001]

【発明の属する技術分野】本発明は、活性汚泥の処理装
置及び廃水処理システムに係わり、特に、有機性廃水を
活性汚泥処理槽で廃水処理して得られる活性汚泥を処理
する活性汚泥の処理装置及びそれを組み込んだ廃水処理
システムに関する。The present invention relates to an activated sludge treatment apparatus and a wastewater treatment system, and more particularly to an activated sludge treatment apparatus for treating activated sludge obtained by treating organic wastewater in an activated sludge treatment tank. And a wastewater treatment system incorporating the same.

【０００２】[0002]

【従来の技術】下水や産業廃水等の有機性廃水の処理の
大半は、活性汚泥を用いた活性汚泥処理槽において生物
学的処理を行なうことにより処理されている。しかし、
活性汚泥処理槽内で増殖した微生物などが余剰の活性汚
泥となって生成するため、廃水処理システムの系外に引
き抜かなくてはならず、引抜き汚泥の処分が問題となっ
ている。引き抜いた余剰の活性汚泥の処理としては、脱
水処理してから、或いは脱水・焼却して灰の状態にして
から、埋立て処分される場合が多いが、この処理方法で
は多くの手間や高額の費用を要する。また、埋立地が年
々不足してきていることから、余剰の活性汚泥を減容化
することにより、余剰汚泥を廃水処理システムの系外に
引き抜く必要のない廃水処理システムの開発が求められ
ている。2. Description of the Related Art Most of the treatment of organic wastewater such as sewage and industrial wastewater is performed by performing biological treatment in an activated sludge treatment tank using activated sludge. But,
Since microorganisms and the like proliferated in the activated sludge treatment tank are generated as surplus activated sludge, they must be extracted outside the wastewater treatment system, and disposal of the extracted sludge is a problem. Excessive activated sludge that has been extracted is often landfilled after being dehydrated or dehydrated or incinerated to form ash, but this method requires a lot of labor and expensive Expensive. In addition, since landfills are becoming scarce year by year, there is a need for the development of a wastewater treatment system that does not require excess sludge to be drawn out of the wastewater treatment system by reducing the volume of excess activated sludge.

【０００３】活性汚泥を減容化する従来の廃水処理シス
テムとしては、処理槽内の活性汚泥をオゾンやその他の
酸化剤、酸・アルカリによって処理した後、活性汚泥処
理槽に導入して無機化する方法等がすでに提案されてい
る。そのうち、代表的なものとして、被処理水中のＢＯ
Ｄ同化により増殖する活性汚泥量よりも多い量の活性汚
泥を好気性処理系から引抜き、引抜いた汚泥をオゾン処
理したのち好気性処理系に導入する方法がある（特開平
６−２０６０８８号公報）。この処理方法は、引抜き汚
泥にオゾン含有ガスを反応させ、汚泥を酸化分解して可
溶化し、生物分解可能な有機物（ＢＯＤ）に変換した
後、好気性処理系で無機化して汚泥を減容化するもので
ある。このとき、オゾン処理で生じたＢＯＤから別の生
成汚泥が生成するため、廃水中のＢＯＤの同化により増
殖する量よりも多い量の汚泥をオゾン処理することが肝
要である。[0003] As a conventional wastewater treatment system for reducing the volume of activated sludge, an activated sludge in a treatment tank is treated with ozone or another oxidizing agent, an acid or alkali, and then introduced into the activated sludge treatment tank to be mineralized. A method of doing so has already been proposed. Among them, the typical one is BO in the water to be treated.
D There is a method in which an activated sludge larger than the amount of activated sludge proliferated by assimilation is withdrawn from the aerobic treatment system, the extracted sludge is treated with ozone, and then introduced into the aerobic treatment system (JP-A-6-206088). . In this treatment method, the extracted sludge is reacted with an ozone-containing gas, and the sludge is oxidatively decomposed and solubilized to be converted into a biodegradable organic substance (BOD). Then, the sludge is reduced in volume by mineralization in an aerobic treatment system. It becomes something. At this time, another generated sludge is generated from the BOD generated by the ozone treatment. Therefore, it is important to ozone-treat an amount of the sludge larger than the amount of the sludge which multiplies by assimilation of the BOD in the wastewater.

【０００４】[0004]

【発明が解決しようとする課題】しかしながら、オゾン
反応により汚泥がＢＯＤ化される際に、生物で分解しに
くい有機物が溶出し、溶液中のＣＯＤが増加する上、オ
ゾンの殺菌作用により活性汚泥中の微生物の多くが死滅
する。このように、溶液中のＣＯＤが増加する上、微生
物の多くが死滅した汚泥溶液が好気性処理系に戻される
と、ＣＯＤが十分に処理されずに廃水処理システムから
排出される処理水の処理水質が悪化する傾向がある。ま
た、オゾン処理により活性汚泥を処理する装置は、高濃
度のオゾン発生に必要な酸素発生器や冷却水、排オゾン
処理のための触媒や活性炭を用いた装置など多くの付帯
設備が必要であり、設備とそのメンテナンスが繁雑にな
るという問題がある。特に、オゾン自体が生物に有害で
あるため、安全上の厳密な管理も必要になる。However, when sludge is converted to BOD by the ozone reaction, organic substances which are hardly decomposed by living organisms are eluted, and COD in the solution increases. Many of the microorganisms die. As described above, when the COD in the solution increases and the sludge solution in which many of the microorganisms have been killed is returned to the aerobic treatment system, the treatment of the treated water discharged from the wastewater treatment system without sufficiently treating the COD. Water quality tends to deteriorate. In addition, the equipment that treats activated sludge by ozone treatment requires many auxiliary equipment such as an oxygen generator and cooling water required for generating high-concentration ozone, a catalyst for activated ozone treatment, and an apparatus using activated carbon. However, there is a problem that the equipment and its maintenance become complicated. In particular, since ozone itself is harmful to living organisms, strict safety management is also required.

【０００５】廃水処理系内の活性汚泥を処理する従来の
別の処理方法としては、過酸化水素などの酸化剤を使用
する方法や、酸・アルカリを添加して可溶化する方法も
ある。しかし、これらの方法も、反応を促進するための
触媒や高温化のための装置が必要となりオゾン処理の場
合と同様に設備とそのメンテナンスが繁雑となる。ま
た、溶液中のＣＯＤが増加する上、微生物を死滅させて
しまうため、生物処理後の最終処理水質が悪化する問題
をかかえている。[0005] Other conventional treatment methods for treating activated sludge in a wastewater treatment system include a method using an oxidizing agent such as hydrogen peroxide and a method of adding an acid or alkali to solubilize. However, these methods also require a catalyst for accelerating the reaction and a device for raising the temperature, and the equipment and maintenance thereof become complicated as in the case of ozone treatment. In addition, the COD in the solution increases and the microorganisms are killed, so that the quality of the final treated water after the biological treatment is deteriorated.

【０００６】本発明はこのような事情に鑑みて成された
もので、簡単な装置で装置の繁雑さと管理上の問題など
を解消し、更には活性汚泥処理後の溶液中のＣＯＤの増
加や、活性汚泥中の微生物の死滅を抑制できるので、処
理水質を悪化させずに汚泥の生成量を抑制し、余剰汚泥
量を低減或いはゼロにすることができる活性汚泥の処理
装置及び廃水処理システムを提供することを目的とす
る。[0006] The present invention has been made in view of such circumstances, and solves the complexity and management problems of the apparatus with a simple apparatus, and further increases the COD in the solution after activated sludge treatment. Since the killing of microorganisms in activated sludge can be suppressed, an activated sludge treatment device and a wastewater treatment system capable of suppressing the amount of sludge generated without deteriorating the quality of treated water and reducing or eliminating surplus sludge can be provided. The purpose is to provide.

【０００７】[0007]

【課題を解決するための手段】本発明は前記目的を達成
するために、加圧部・狭窄部・低圧部から成る流路を有
し、前記加圧部で加圧した活性汚泥を前記狭窄部を介し
て前記低圧部に噴出させることにより前記活性汚泥を処
理する汚泥噴出手段と、前記汚泥噴出手段で処理した活
性汚泥を、酸素又は酸化態窒素と反応させる減容化処理
槽と、を備えたことを特徴とする。In order to achieve the above object, the present invention has a flow path comprising a pressurizing section, a constricted section, and a low pressure section, and the activated sludge pressurized by the pressurizing section is subjected to the constriction. A sludge ejecting means for treating the activated sludge by ejecting the activated sludge to the low-pressure section through a section, and a volume reduction treatment tank for reacting the activated sludge treated by the sludge ejecting means with oxygen or oxidized nitrogen. It is characterized by having.

【０００８】本発明によれば、活性汚泥を、加圧部で加
圧した加圧下で狭窄部から低圧部に噴出させることによ
り、溶液中のＣＯＤの増加が少なく、活性汚泥中の微生
物をほとんど死滅させずに、活性汚泥を構成する浮遊性
物質を微細化し、微生物を分散化することができる。そ
の為、分散化した活性汚泥を、減容化処理槽において溶
存酸素又は酸化態窒素と反応させることにより活性汚泥
が自己酸化して無機物化し、活性汚泥が減容化する。こ
の場合、分散化した活性汚泥は、汚泥微生物がほとんど
死滅せず、むしろ微生物と浮遊性有機物との反応の機会
が増加し、微生物活性を高い状態に維持できるので、活
性汚泥自らの微生物活性を利用した自己酸化が促進さ
れ、効率良く活性汚泥の減容化を行うことができる。According to the present invention, the activated sludge is ejected from the constricted part to the low-pressure part under pressure applied by the pressurizing part, so that the increase in COD in the solution is small, and the microorganisms in the activated sludge are almost eliminated. Without dying, the floating substances constituting the activated sludge can be finely divided and the microorganisms can be dispersed. For this reason, the activated sludge that has been dispersed is reacted with dissolved oxygen or oxidized nitrogen in a volume reduction treatment tank, whereby the activated sludge is self-oxidized and becomes inorganic, and the volume of the activated sludge is reduced. In this case, the dispersed activated sludge hardly kills the sludge microorganisms, but rather increases the chances of the reaction between the microorganisms and the suspended organic matter, and can maintain the microbial activity at a high level. The utilized auto-oxidation is promoted, and the volume of activated sludge can be reduced efficiently.

【０００９】また、本発明は前記目的を達成するため
に、有機性廃水を生物学的処理槽で処理する際に得られ
る活性汚泥を、請求項１又は２に記載の汚泥噴出手段で
処理させた後、前記生物学的処理槽に戻して酸素又は酸
化態窒素と反応させることを特徴とする。According to the present invention, in order to achieve the above object, activated sludge obtained when organic wastewater is treated in a biological treatment tank is treated by the sludge ejection means according to claim 1 or 2. Then, it is returned to the biological treatment tank and reacted with oxygen or oxidized nitrogen.

【００１０】本発明によれば、減容化処理槽として既存
の生物学的処理槽を使用することができるので、生物学
的処理槽において増殖する活性汚泥を廃水処理系内で処
理することができ、しかも廃水処理系から排出される処
理水の処理水質を悪化させることもない。According to the present invention, an existing biological treatment tank can be used as a volume reduction treatment tank, so that activated sludge growing in the biological treatment tank can be treated in the wastewater treatment system. In addition, the quality of the treated water discharged from the wastewater treatment system is not deteriorated.

【００１１】[0011]

【発明の実施の形態】以下添付図面に従って、本発明に
係る活性汚泥の処理装置及び廃水処理システムの好まし
い実施の形態について説明する。DESCRIPTION OF THE PREFERRED EMBODIMENTS Preferred embodiments of an activated sludge treatment apparatus and a wastewater treatment system according to the present invention will be described below with reference to the accompanying drawings.

【００１２】本発明の活性汚泥の処理装置及び廃水処理
システムを説明する前に本発明の理論的根拠を説明す
る。Before describing the activated sludge treatment apparatus and wastewater treatment system of the present invention, the theoretical basis of the present invention will be described.

【００１３】図１は、ジェット状のキャビテーションを
促進する機能を有するノズルを備えたウオータジェット
装置（ＷＪ）である。このウオータジェット装置は、プ
ランジャーポンプ（図示せず）により加圧した活性汚泥
Ｊを容器Ａの入口Ｂに装着したノズルＣへ送給する。ノ
ズルＣでは、噴出孔Ｄにおいて活性汚泥が急減圧・急加
速され、キャビテーションを伴う活性汚泥のジェットＥ
となって容器Ａ内の活性汚泥中Ｆに噴出する。このノズ
ルＣは、噴出孔Ｄの先端に、お碗型の拡大空洞部Ｇを設
けている。この拡大空洞部Ｇを設けることによって、ジ
ェットＥの付け根（噴出直後の領域）の周囲には渦Ｈが
生じる。この渦ＨがジェットＥに圧力変動を与え、また
周囲にある活性汚泥Ｆを巻き込むようにしてキャビテー
ションの核（Cavitation nuclei)を供給する。このよう
なノズルＣを用いれば、低噴射圧力でも、必要な威力の
キャビテーションを十分に発生できるようになるので、
システムの効率化（低動力化）に貢献する。FIG. 1 shows a water jet apparatus (WJ) provided with a nozzle having a function of promoting jet cavitation. This water jet device feeds activated sludge J pressurized by a plunger pump (not shown) to a nozzle C attached to an inlet B of a container A. In the nozzle C, the activated sludge is rapidly decompressed and rapidly accelerated in the ejection hole D, and the activated sludge jet E with cavitation is jetted.
And squirts into the activated sludge F in the container A. The nozzle C has a bowl-shaped enlarged cavity G at the tip of the ejection hole D. By providing the enlarged cavity G, a vortex H is generated around the base of the jet E (the area immediately after the jet). The vortex H gives pressure fluctuations to the jet E and also supplies cavitation nuclei in such a manner that the activated sludge F around the jet E is entrained. If such a nozzle C is used, cavitation of a necessary power can be sufficiently generated even at a low injection pressure.
Contributes to system efficiency (low power).

【００１４】図２は、図１のウオータジェット装置を用
いて、活性汚泥を加圧下においてジェットノズルＣから
低圧部である容器Ａ内に噴出させて分散化処理した後、
曝気処理を１日行い、溶存酸素と反応させた場合の汚泥
減容化率（％）を回分試験により調べたものである。回
分試験で使用した活性汚泥の初期汚泥濃度（初期ＭＬＳ
Ｓ濃度）は、４．３〜１０．６ｇ／Ｌであり、ウオータ
ジェット装置で発生させるキャビテーション係数ａを変
化させた場合の汚泥減容化率（％）を調べた。FIG. 2 shows that the activated sludge is ejected from a jet nozzle C into a container A, which is a low-pressure section, under pressure and dispersed by using the water jet apparatus of FIG.
The sludge volume reduction rate (%) when aeration treatment was performed for one day and reacted with dissolved oxygen was examined by a batch test. Initial sludge concentration of activated sludge used in batch test (initial MLS
S concentration) was 4.3 to 10.6 g / L, and the sludge volume reduction rate (%) when the cavitation coefficient a generated by the water jet device was changed was examined.

【００１５】尚、図２には、活性汚泥にエアを吹き込む
前処理を行った場合（図２の前処理あり）と、前処理を
行わなかった場合（図２の前処理なし）を示した。FIG. 2 shows a case where the pretreatment for blowing air into the activated sludge is performed (the pretreatment in FIG. 2 is performed) and a case where the pretreatment is not performed (no pretreatment in FIG. 2). .

【００１６】ここで、汚泥減容化率とは、初期汚泥量
（ＳＳ）に対して本発明の処理により消滅した汚泥減容
化量（ΔＳＳ）の比率（ΔＳＳ／ＳＳ）を示したもので
ある。Here, the sludge volume reduction ratio indicates the ratio (ΔSS / SS) of the sludge volume reduction (ΔSS) that has disappeared by the treatment of the present invention to the initial sludge volume (SS). is there.

【００１７】図３は、活性汚泥にエアを吹き込んで前処
理をした後、ジェットノズルから噴出させた直後の、微
生物活性（呼吸速度）と汚泥溶液中のＣＯＤ濃度および
曝気処理後のＣＯＤ濃度を示したものである。FIG. 3 shows the microbial activity (respiration rate), the COD concentration in the sludge solution, and the COD concentration after the aeration treatment immediately after the activated sludge was pre-treated by blowing air into the activated sludge and jetted from the jet nozzle. It is shown.

【００１８】図２には、横軸にキャビテーション係数、
縦軸に汚泥減容化率を示すと共に、ウオータジェット装
置で処理しない未処理の場合（図２のＷＪ未処理）の汚
泥減容化率を示した。また、図３には、横軸にキャビテ
ーション係数、縦軸に微生物活性（％）、溶液中のＣＯ
Ｄ濃度（ｍｇ／Ｌ）を示すと共に、ウオータジェット装
置で処理しない未処理の場合（図３のＷＪ未処理）の微
生物活性と溶液中のＣＯＤ濃度（ｍｇ／Ｌ）を示した。
尚、キャビテーション係数ａは、数値が大きくなるほど
キャビテーションの強度が弱くなり、数値が小さくなる
ほどキャビテーションの強度が強くなる。In FIG. 2, the horizontal axis represents the cavitation coefficient,
The vertical axis shows the sludge volume reduction rate, and the sludge volume reduction rate in the case of untreated (not treated with WJ in FIG. 2) which is not treated by the water jet device. In FIG. 3, the horizontal axis indicates the cavitation coefficient, the vertical axis indicates the microbial activity (%), and the CO in the solution.
In addition to the D concentration (mg / L), the microbial activity and the COD concentration (mg / L) in the untreated case (not treated with WJ in FIG. 3) not treated with the water jet device are shown.
As the cavitation coefficient a increases, the cavitation intensity decreases as the numerical value increases, and the cavitation intensity increases as the numerical value decreases.

【００１９】図２から分かるように、活性汚泥をそのま
ま曝気処理（１日）したＷＪ未処理の場合には、汚泥減
容化率が６％程度であった。これに対し、前処理ありの
活性汚泥の汚泥減容化率は、キャビテーション係数ａが
０．００５まではａを大きくするに従って低下するが、
キャビテーション係数ａが０．０１〜０．１の範囲で汚
泥減容化率がほぼ１８％の極大値を示した。その後、キ
ャビテーション係数ａを大きくしていくと、汚泥減容化
率が低下し、キャビテーション係数ａが０．７のときに
ＷＪ未処理の場合と同程度まで低下した。また、ジェッ
トノズルＣを通過させる前に、活性汚泥Ｊにエアを吹き
込む前処理の有り無しの比較では、エアを吹き込んだ方
が、より高い汚泥減容化率が得られた。As can be seen from FIG. 2, the sludge volume reduction rate was about 6% in the case of untreated WJ in which activated sludge was aerated (1 day). On the other hand, the sludge volume reduction rate of the activated sludge with the pretreatment decreases as the cavitation coefficient a increases up to 0.005.
When the cavitation coefficient a was in the range of 0.01 to 0.1, the sludge volume reduction rate showed a maximum value of approximately 18%. Thereafter, as the cavitation coefficient a was increased, the sludge volume reduction rate was reduced, and when the cavitation coefficient a was 0.7, it was reduced to about the same level as in the case without WJ treatment. In addition, in comparison with the presence or absence of the pretreatment in which air was blown into the activated sludge J before passing through the jet nozzle C, a higher sludge volume reduction ratio was obtained by blowing air.

【００２０】キャビテーション係数ａが０．４以下で汚
泥減容化率が高くなる理由として、図３に示されるよう
に、０．４以下でＷＪ未処理の場合より微生物活性がむ
しろ高くなっており、活性汚泥中の菌体コロニーやＳＳ
成分が十分に分散化されたため、その後の曝気処理で微
生物による溶存酸素を利用した有機物分解の反応性が高
まったことが考えられる。ＷＪ処理による汚泥フロック
の変化の推定概念図を図８に示す。これに対し、キャビ
テーション係数ａが０．４を超える場合、キャビテーシ
ョンが弱く、活性汚泥の分散化が不十分であるため、汚
泥減容化率が低いと考えられる。しかし、図３から分か
るように、キャビテーション係数ａを０．００５未満に
すると、キャビテーションが強くなりすぎて汚泥が液中
に溶出し、見かけ上、汚泥減容化率が高くなるが、微生
物が破壊されて活性が減少するとともに溶液中のＣＯＤ
が増加するため、曝気処理を１日行なった後も残存して
しまう。The reason why the sludge volume reduction rate becomes high when the cavitation coefficient a is 0.4 or less is that the microbial activity is rather high when the cavitation coefficient a is 0.4 or less than when WJ is not treated, as shown in FIG. Cell colonies and SS in activated sludge
It is considered that the reactivity of organic matter decomposition using dissolved oxygen by microorganisms was increased in the subsequent aeration treatment because the components were sufficiently dispersed. FIG. 8 is a conceptual diagram of estimation of a change in sludge floc due to the WJ process. On the other hand, when the cavitation coefficient a exceeds 0.4, the cavitation is weak and the dispersion of the activated sludge is insufficient, so that the sludge volume reduction rate is considered to be low. However, as can be seen from FIG. 3, when the cavitation coefficient a is less than 0.005, the cavitation becomes too strong, and the sludge elutes into the liquid, and the sludge volume reduction rate increases, but the microorganisms are destroyed. Activity and decrease COD in solution
And remains after one day of aeration.

【００２１】以上のことから分かるように、ウオータジ
ェット装置の例のように加圧部・狭窄部・低圧部から成
る流路を有する汚泥噴出手段を用いて活性汚泥を減容化
する場合、キャビテーション係数ａの大きさが汚泥減容
化率に大きく影響する。従って、キャビテーション係数
ａの適切な値を考察した場合、汚泥噴出手段により発生
するキャビテーション係数ａ範囲は、Ｐｊをジェットノ
ズル（狭窄部）の上流側圧力、Ｐｒをジェットノズルの
下流側圧力、Ｐｖを活性汚泥の蒸気圧としたときに次式
（１）、（２）As can be seen from the above description, when activated sludge is reduced in volume by using sludge jetting means having a flow path composed of a pressurized portion, a narrowed portion and a low-pressure portion as in the case of a water jet device, cavitation The magnitude of the coefficient a greatly affects the sludge volume reduction rate. Therefore, when considering an appropriate value of the cavitation coefficient a, the range of the cavitation coefficient a generated by the sludge ejecting means is such that Pj is the upstream pressure of the jet nozzle (constriction), Pr is the downstream pressure of the jet nozzle, and Pv is the downstream pressure of the jet nozzle. The following equations (1) and (2) when the vapor pressure of activated sludge is used

【００２２】[0022]

【数１】０．００５＜ａ＜０．４ …（１）## EQU1 ## 0.005 <a <0.4 (1)

【００２３】[0023]

【数２】 但し、ａ＝（Ｐｒ−Ｐｖ）／（Ｐｊ−Ｐｒ）…（２） を満足することが必要であり、更に好ましくは、キャビ
テーション係数ａの範囲が次式（３）、（４）It is necessary that a = (Pr−Pv) / (Pj−Pr) (2) is satisfied. More preferably, the range of the cavitation coefficient a is expressed by the following equations (3) and (4). )

【００２４】[0024]

【数３】０．０１＜ａ＜０．１ …（３）## EQU3 ## 0.01 <a <0.1 (3)

【００２５】[0025]

【数４】 但し、ａ＝（Ｐｒ−Ｐｖ）／（Ｐｊ−Ｐｒ）…（４） を満足するとよい。Where a = (Pr−Pv) / (Pj−Pr) (4)

【００２６】本発明の活性汚泥の処理装置は、上記知見
に基づいて成されたものであり、基本構成は、活性汚泥
を、加圧部・狭窄部・低圧部から成る流路を通過させる
ことにより活性汚泥を分散化させる汚泥噴出手段と、汚
泥噴出手段を通過した活性汚泥を、酸素又は酸化態窒素
と反応させる減容化処理槽とで構成される。そして、狭
窄部は、オリフィス、ベンチュリ、若しくは仕切板で構
成され、０．００５＜ａ＜０．４の範囲のキャビテーシ
ョン係数ａ、更に好ましくは０．０１＜ａ＜０．１の範
囲のキャビテーション係数ａを発生させるものである。The activated sludge treatment apparatus of the present invention has been made based on the above findings, and has a basic configuration in which activated sludge is passed through a flow path comprising a pressurized section, a narrowed section, and a low pressure section. And a volume reduction treatment tank for reacting the activated sludge that has passed through the sludge ejection means with oxygen or oxidized nitrogen. The stenosis portion is formed of an orifice, a venturi, or a partition plate, and has a cavitation coefficient a in a range of 0.005 <a <0.4, and more preferably a cavitation coefficient a in a range of 0.01 <a <0.1. a.

【００２７】また、前記低圧部は、キャビテーションを
発生させる狭窄部、例えばノズルを入口に備え、該ノズ
ルから噴出されるジェット流方向を長手方向とする閉止
状の容器であり、該容器内で活性汚泥の分散、酸化ない
し可溶化を行わせるものである。The low-pressure section is a closed vessel having a constricted section for generating cavitation, for example, a nozzle at an inlet and having a longitudinal direction of a jet flow ejected from the nozzle. It disperses, oxidizes or solubilizes sludge.

【００２８】また、減容化処理槽は、廃水処理を行なう
既存の活性汚泥処理槽でもよく、或いは汚泥処理のため
に別途設けた曝気手段付きの消化槽でもよい。更に、こ
の基本構成に、汚泥噴出手段から噴出する前の活性汚泥
にエアを吹き込むエア吹込み手段を付加して構成すると
一層良い。The volume reduction treatment tank may be an existing activated sludge treatment tank for performing wastewater treatment, or a digestion tank with aeration means separately provided for sludge treatment. Further, it is more preferable to add an air blowing means for blowing air into activated sludge before it is blown out from the sludge blowing means to the basic structure.

【００２９】図４は、本発明の活性汚泥の処理装置を、
有機性廃水を処理する廃水処理系統に組み込んだ廃水処
理システムの第１の実施の形態である。FIG. 4 shows an activated sludge treatment apparatus of the present invention.
1 is a first embodiment of a wastewater treatment system incorporated in a wastewater treatment system for treating organic wastewater.

【００３０】図４に示すように、廃水処理システム１０
は、主として、廃水処理系統３０と汚泥処理系統４０と
から構成される。As shown in FIG. 4, the wastewater treatment system 10
Is mainly composed of a wastewater treatment system 30 and a sludge treatment system 40.

【００３１】廃水処理系統３０は、主として、好気的に
生物学的な処理を行なう活性汚泥処理槽１と汚泥分離槽
２とから構成される。活性汚泥処理槽１には、廃水管１
１から有機性廃水が供給され、曝気装置２１から曝気さ
れることにより、好気的な生物学的処理が行なわれ、有
機性廃水が浄化される。浄化後の活性汚泥混合液は、流
出管１３を介して汚泥分離槽２に流入する。活性汚泥混
合液は、汚泥分離槽２で処理水（上澄水）と沈降汚泥に
固液分離される。処理水は処理水管１４を介して系外に
排出される。一方、汚泥分離槽２で分離された沈降汚泥
は、その一部が返送汚泥管１２を介して活性汚泥処理槽
１に戻され、残りの汚泥が汚泥引出管１５を介して汚泥
処理系統４０に送られる。The wastewater treatment system 30 mainly comprises an activated sludge treatment tank 1 for performing aerobic biological treatment and a sludge separation tank 2. The activated sludge treatment tank 1 has a wastewater pipe 1
The organic wastewater is supplied from 1 and aerated from the aeration device 21, whereby aerobic biological treatment is performed and the organic wastewater is purified. The purified activated sludge mixture flows into the sludge separation tank 2 via the outflow pipe 13. The activated sludge mixture is solid-liquid separated into treated water (supernatant water) and settled sludge in the sludge separation tank 2. The treated water is discharged out of the system via the treated water pipe 14. On the other hand, part of the settled sludge separated in the sludge separation tank 2 is returned to the activated sludge treatment tank 1 via the return sludge pipe 12, and the remaining sludge is sent to the sludge treatment system 40 via the sludge extraction pipe 15. Sent.

【００３２】また、汚泥処理系統４０は、主として、消
化槽３、汚泥噴出手段、汚泥濃縮槽６とから構成され
る。また、汚泥噴出手段は、高圧ポンプ４と、ジェット
ノズル３１及び容器３２から成るリアクタ５とで構成さ
れ、高圧ポンプ４とリアクタ５とを組み合わせたもの
は、基本的にはウオータジェット装置と同様の構成を形
成する。The sludge treatment system 40 mainly comprises a digestion tank 3, sludge jetting means, and a sludge thickening tank 6. The sludge jetting means is composed of a high-pressure pump 4 and a reactor 5 comprising a jet nozzle 31 and a container 32. The combination of the high-pressure pump 4 and the reactor 5 is basically the same as that of a water jet device. Form the configuration.

【００３３】消化槽３には、曝気装置２２が設けられ、
汚泥引出管１５から送られた活性汚泥にエアを曝気す
る。この曝気装置２２は、活性汚泥を次のリアクタ５に
供給する前のエアの吹き込みと、リアクタ５を通過した
活性汚泥を好気的に生物学的処理を行なうための曝気の
両方を兼用する。また、消化槽３はリアクタ５に接続
し、リアクタ５は処理汚泥管１７を介して汚泥濃縮槽６
に接続すると共に、濃縮汚泥管１９を介して消化槽３に
接続している。これにより、消化槽３、リアクタ５、汚
泥濃縮槽６の間には汚泥の循環系路が形成される。ま
た、汚泥濃縮槽６は、分離水流出管１８を介して活性汚
泥処理槽１に接続され、汚泥濃縮槽６で汚泥と分離され
た分離水は、活性汚泥処理槽１で浄化される。The digestion tank 3 is provided with an aeration device 22.
The activated sludge sent from the sludge extraction pipe 15 is aerated with air. The aeration device 22 is used both for blowing air before supplying activated sludge to the next reactor 5 and for aerobically performing aerobic biological treatment of the activated sludge that has passed through the reactor 5. Further, the digestion tank 3 is connected to the reactor 5, and the reactor 5 is connected to the sludge concentration tank 6 through the treated sludge pipe 17.
And to the digestion tank 3 via the concentrated sludge pipe 19. Thereby, a circulation path of sludge is formed between the digestion tank 3, the reactor 5, and the sludge concentration tank 6. Further, the sludge concentration tank 6 is connected to the activated sludge treatment tank 1 via the separated water outflow pipe 18, and the separated water separated from the sludge in the sludge concentration tank 6 is purified in the activated sludge treatment tank 1.

【００３４】ここで、リアクタ５の好ましい構成と作用
について図５により詳細に説明する。Here, a preferred configuration and operation of the reactor 5 will be described in detail with reference to FIG.

【００３５】ジェットノズル３１はノズルマウント５０
に装着されて容器３２の入口に備えられる。加圧された
活性汚泥５２は、ジェットノズル３１において急減圧・
急加速され、キャビテーション・ジェット流５４となっ
て容器３２内の活性汚泥５６の中に噴出される。このキ
ャビテーション・ジェット流５４は閉止高速空間である
容器３２内に噴出するため、まず容器３２の内壁とキャ
ビテーション・ジェット流５４との間には、比較的大き
な容器内循環渦５８が生じて、強力な混合が生じる。そ
の為、キャビテーションの作用は、容器３２内の活性汚
泥５６の全域に及ぶ。また、この容器内循環渦５８の作
用によって、周囲から液や汚泥を巻き込むエントレン６
０が活発となって、周囲の気泡核（Nuclei) が、キャビ
テーション・ジェット流５４中に供給されてキャビテー
ションが促進される。The jet nozzle 31 has a nozzle mount 50
And provided at the entrance of the container 32. The pressurized activated sludge 52 is rapidly decompressed at the jet nozzle 31.
It is rapidly accelerated and jetted into the activated sludge 56 in the container 32 as a cavitation jet stream 54. Since the cavitation jet flow 54 is jetted into the container 32 which is a closed high-speed space, a relatively large circulation vortex 58 in the container is generated between the inner wall of the container 32 and the cavitation jet flow 54, and the strong Mixing occurs. Therefore, the action of the cavitation extends to the entire area of the activated sludge 56 in the container 32. In addition, by the action of the circulation vortex 58 in the container, the entrain 6 that entrains the liquid or sludge from the surroundings
When 0 becomes active, the surrounding bubble nuclei (Nuclei) are fed into the cavitation jet stream 54 to promote cavitation.

【００３６】次に、上記の如く構成された廃水処理シス
テムの第１の実施の形態の作用について説明する。Next, the operation of the first embodiment of the wastewater treatment system configured as described above will be described.

【００３７】有機性廃水を廃水管１１から活性汚泥処理
槽１に導入し、返送汚泥管１２から返送される返送汚泥
および曝気装置２１から供給される空気とを活性汚泥処
理槽１内で混合し、好気的な生物学的処理を行なう。ま
た活性汚泥処理槽１内の活性汚泥混合液を流出管１３か
ら汚泥分離槽２に導いて固液分離を行う。ここで分離し
た処理水を処理水管１４から排出すると共に、分離汚泥
を返送汚泥管１２から活性汚泥処理槽１に返送する。The organic wastewater is introduced into the activated sludge treatment tank 1 from the wastewater pipe 11, and the returned sludge returned from the returned sludge pipe 12 and the air supplied from the aeration device 21 are mixed in the activated sludge treatment tank 1. Perform aerobic biological treatments. The activated sludge mixed liquid in the activated sludge treatment tank 1 is guided from the outflow pipe 13 to the sludge separation tank 2 to perform solid-liquid separation. The separated treated water is discharged from the treated water pipe 14 and the separated sludge is returned from the return sludge pipe 12 to the activated sludge treatment tank 1.

【００３８】汚泥処理系統４０では、返送汚泥の一部を
汚泥引出管１５により消化槽３に導入し、濃縮汚泥管１
９から循環される濃縮汚泥と曝気装置２２から供給され
るエアとを混合する。消化槽３内の汚泥は高圧ポンプ４
によりリアクタ５に送られ、ジェットノズル３１から容
器３２内の汚泥溶液中に勢いよく噴出されて汚泥が分散
化される。この場合、高圧ポンプ４の吐出圧力などの調
整によりジェットノズル３１により発生するキャビテー
ション係数ａを、０．００５＜ａ＜０．４の範囲にある
のが好ましく、更に好ましくは０．０１＜ａ＜０．１の
範囲にあることが良い。In the sludge treatment system 40, a part of the returned sludge is introduced into the digestion tank 3 by the sludge extraction pipe 15, and the concentrated sludge pipe 1
9 and the air supplied from the aeration device 22 are mixed. Sludge in digestion tank 3 is pumped by high pressure pump 4
To the reactor 5, and is vigorously jetted out of the jet nozzle 31 into the sludge solution in the container 32 to disperse the sludge. In this case, the cavitation coefficient a generated by the jet nozzle 31 by adjusting the discharge pressure or the like of the high-pressure pump 4 is preferably in the range of 0.005 <a <0.4, more preferably 0.01 <a <. It is better to be in the range of 0.1.

【００３９】そして、リアクタ５内の汚泥は、汚泥移送
管１７により汚泥濃縮槽６に移送され、濃縮分離され
る。濃縮汚泥は濃縮汚泥管１９を通って消化槽３に循環
される一方、分離水は分離水流出管１８を通って水処理
系の活性汚泥処理槽１に戻される。ここで、汚泥移送管
１６の高圧ポンプ４の吸い込み側に曝気装置２２から少
量のエアを吹き込むことにより、ジェットノズル３１に
より発生するキャビテーションの核となると共に、リア
クタ５内で微細気泡が析出し、汚泥濃縮槽６で汚泥が浮
上分離・濃縮され易くなる。濃縮された汚泥は、消化槽
３内で自己酸化し、汚泥引出管１５から消化槽３に投入
された汚泥と同量が減容化される。また、高圧ポンプ４
とリアクタ５で汚泥を分散化処理した際に、溶液中のＣ
ＯＤが幾分増加するが、消化槽３及び活性汚泥処理槽１
でＣＯＤが十分に処理されるため、処理水のＣＯＤが上
昇することはない。Then, the sludge in the reactor 5 is transferred to the sludge thickening tank 6 by the sludge transfer pipe 17 and concentrated and separated. The concentrated sludge is circulated to the digestion tank 3 through the concentrated sludge pipe 19, while the separated water is returned to the activated sludge treatment tank 1 of the water treatment system through the separated water outflow pipe 18. Here, by blowing a small amount of air from the aeration device 22 into the suction side of the high-pressure pump 4 of the sludge transfer pipe 16, it becomes a core of cavitation generated by the jet nozzle 31, and fine bubbles precipitate in the reactor 5, In the sludge thickening tank 6, the sludge is easily floated, separated and concentrated. The concentrated sludge is self-oxidized in the digestion tank 3, and the volume is reduced by the same amount as the sludge introduced into the digestion tank 3 from the sludge extraction pipe 15. In addition, high pressure pump 4
And sludge in the reactor 5 when the sludge is dispersed,
Although the OD increases somewhat, the digestion tank 3 and the activated sludge treatment tank 1
, COD is sufficiently treated, so that COD of treated water does not increase.

【００４０】これにより、本発明の第１の実施の形態に
よれば、装置の繁雑さと管理上の問題などを解消し、活
性汚泥の分散化処理後の溶液中のＣＯＤの増加や、活性
汚泥中の微生物の死滅を抑制できるので、処理水質を悪
化させずに汚泥の生成量を抑制し、余剰汚泥量を低減或
いはゼロにすることができる。Thus, according to the first embodiment of the present invention, the complexity of the apparatus and the problems in management are solved, and the COD in the solution after the dispersion treatment of the activated sludge is increased, and the activated sludge is reduced. Since the killing of microorganisms inside can be suppressed, the amount of sludge generated can be suppressed without deteriorating the quality of treated water, and the amount of surplus sludge can be reduced or reduced to zero.

【００４１】次に、第１の実施の形態における廃水処理
システムを使用して下水処理場からの余剰汚泥を用い、
Ｆｉｌｌ ａｎｄ Ｄｒａｗ方式で汚泥減容化効果を検
討した例を説明する。Next, using the excess sludge from the sewage treatment plant using the wastewater treatment system in the first embodiment,
An example of examining the sludge volume reduction effect by the Fill and Draw method will be described.

【００４２】まず、初期活性汚泥濃度が１０ｇ／Ｌの活
性汚泥３５Ｌの全量を、０．０３のキャビテーション係
数ａを発生させてリアクタに１回通過させた後、汚泥濃
縮槽で汚泥を３０分沈殿濃縮させ、上澄水１０Ｌを捨て
た。ちなみに、ここでの汚泥の濃縮方法は浮上濃縮でな
く、汚泥中に微細気泡を曝気した後で沈降濃縮とした
が、ジェットノズル処理により沈降性が改善されるた
め、容易に濃縮汚泥が得られた。First, 35 L of activated sludge having an initial activated sludge concentration of 10 g / L was once passed through a reactor with a cavitation coefficient a of 0.03, and then sludge was settled in a sludge concentration tank for 30 minutes. After concentration, 10 L of the supernatant water was discarded. By the way, the method of concentrating sludge here was not flotation concentration, but sedimentation concentration after aerating fine bubbles in the sludge, but the sedimentation was improved by jet nozzle treatment, so concentrated sludge was easily obtained. Was.

【００４３】次に、活性汚泥濃度が５ｇ／Ｌの新しい余
剰汚泥１０Ｌを追加して３５Ｌとし、消化槽３内で１日
間曝気処理した。翌日からも毎日新しい余剰汚泥を追加
して全体として３５Ｌ全量を用いて、ジェットノズル処
理から曝気処理に至る一連の操作を同じ条件で繰り返し
た。その結果、毎日のジェットノズル処理前に測定した
汚泥濃度は、初期活性汚泥濃度である１０ｇ／Ｌに略維
持されていた。このことは、１日ごとに新しい余剰汚泥
量５ｇ／Ｌ×１０Ｌ＝５０ｇを追加しながら、追加汚泥
の約７倍に相当する１０ｇ／Ｌ×３５Ｌ＝３５０ｇの活
性汚泥量を本発明による汚泥処理（ジェットノズル処理
後に曝気処理）を行なえば、廃水処理システムの系外に
引き抜く引抜汚泥が全く発生することのない廃水処理シ
ステムを構築できることを意味する。Next, 10 L of new excess sludge having an activated sludge concentration of 5 g / L was added to 35 L, and aeration treatment was performed in the digestion tank 3 for one day. From the next day, a series of operations from jet nozzle treatment to aeration treatment was repeated under the same conditions by adding a new excess sludge every day and using the entire amount of 35 L as a whole. As a result, the sludge concentration measured before daily jet nozzle treatment was substantially maintained at the initial activated sludge concentration of 10 g / L. This means that while adding a new excess sludge amount of 5 g / L × 10 L = 50 g every day, the activated sludge amount of 10 g / L × 35 L = 350 g corresponding to about 7 times the additional sludge according to the present invention. By performing (aeration treatment after jet nozzle treatment), it means that a wastewater treatment system can be constructed in which no extracted sludge is drawn out of the wastewater treatment system.

【００４４】図６は、本発明の活性汚泥の処理装置を、
有機性廃水を処理する廃水処理系統に組み込んだ廃水処
理システムの第２の実施の形態であり、ジェットノズル
３１から活性汚泥処理槽１内に減容化するための活性汚
泥を直接噴出させるようにしたものである。尚、第１の
実施の形態と同じ部材、装置には同符号を付して説明す
る。FIG. 6 shows an activated sludge treatment apparatus of the present invention.
This is a second embodiment of a wastewater treatment system incorporated in a wastewater treatment system for treating organic wastewater, in which activated sludge for reducing the volume of the activated sludge is directly ejected from a jet nozzle 31 into an activated sludge treatment tank 1. It was done. The same members and devices as those in the first embodiment will be described with the same reference numerals.

【００４５】第２の実施の形態における廃水処理システ
ム１０は、廃水処理系統３０と汚泥処理系統４０とから
構成されるが、廃水処理系統は第１の実施の形態と同様
なので説明は省略する。The wastewater treatment system 10 according to the second embodiment includes a wastewater treatment system 30 and a sludge treatment system 40. The description of the wastewater treatment system is omitted because it is the same as that of the first embodiment.

【００４６】汚泥処理系統４０は、主として、予備曝気
槽７、高圧ポンプ４、ジェットノズル３１から構成され
ると共に、ジェットノズル３１の噴出口は廃水処理系統
３０の活性汚泥処理槽１内に設けられる。そして、汚泥
引出管１５が予備曝気装置２３を備えた予備曝気槽７に
接続されると共に、予備曝気槽７は高圧ポンプ４と汚泥
移送管１６を介して活性汚泥処理槽１に設けたジェット
ノズル３１に接続される。The sludge treatment system 40 mainly includes a preliminary aeration tank 7, a high-pressure pump 4, and a jet nozzle 31, and the jet port of the jet nozzle 31 is provided in the activated sludge treatment tank 1 of the wastewater treatment system 30. . The sludge extraction pipe 15 is connected to the preliminary aeration tank 7 provided with the preliminary aeration device 23, and the preliminary aeration tank 7 is connected to the jet nozzle provided in the activated sludge treatment tank 1 via the high-pressure pump 4 and the sludge transfer pipe 16. 31.

【００４７】上記の如く構成された本発明の廃水処理シ
ステムの第２の実施の形態によれば、廃水処理系統３０
における廃水処理は第１の実施の形態と同様である。そ
して、汚泥処理系統４０においては、汚泥分離槽２で固
液分離された活性汚泥の一部は汚泥引出管１５を通って
予備曝気槽７に送られ、予備曝気装置２３からエアが供
給される。エアを溶解した活性汚泥は、高圧ポンプ４と
汚泥移送管１６を経てジェットノズル３１から活性汚泥
処理槽１内に勢いよく噴出される。ジェットノズル処理
された活性汚泥は、上記したように活性汚泥処理槽１内
での自己酸化率を増加させることができる。これによ
り、第２の実施の形態の場合も、装置の繁雑さと管理上
の問題などを解消し、活性汚泥の分散化処理後の溶液中
のＣＯＤの増加や、活性汚泥中の微生物の死滅を抑制で
きるので、処理水質を悪化させずに汚泥の生成量を抑制
し、余剰汚泥量を低減或いはゼロにすることができる。
更に、第２の実施の形態では、ジェットノズル３１の噴
出口は廃水処理系統３０の活性汚泥処理槽１内に設けた
ので、減容化処理槽として特別な槽を設ける必要がな
く、また活性汚泥処理槽１が低圧部をも兼用するので、
廃水処理システム全体を大幅にコンパクト化できる。According to the second embodiment of the wastewater treatment system of the present invention configured as described above, the wastewater treatment system 30
Is the same as in the first embodiment. Then, in the sludge treatment system 40, a part of the activated sludge separated into solid and liquid in the sludge separation tank 2 is sent to the preliminary aeration tank 7 through the sludge extraction pipe 15, and air is supplied from the preliminary aeration device 23. . The activated sludge in which the air is dissolved is vigorously jetted from the jet nozzle 31 into the activated sludge treatment tank 1 via the high-pressure pump 4 and the sludge transfer pipe 16. The activated sludge subjected to the jet nozzle treatment can increase the auto-oxidation rate in the activated sludge treatment tank 1 as described above. Thereby, also in the case of the second embodiment, the complexity of the apparatus and the problem of management are solved, and the COD in the solution after the dispersion treatment of the activated sludge is increased and the microorganisms in the activated sludge are killed. Since the amount of sludge can be suppressed, the amount of generated sludge can be suppressed without deteriorating the quality of treated water, and the amount of excess sludge can be reduced or reduced to zero.
Furthermore, in the second embodiment, since the jet port of the jet nozzle 31 is provided in the activated sludge treatment tank 1 of the wastewater treatment system 30, there is no need to provide a special tank as a volume reduction treatment tank. Since the sludge treatment tank 1 also serves as a low pressure part,
The entire wastewater treatment system can be made much more compact.

【００４８】次に、第２の実施の形態における廃水処理
システムを使用して食品廃液（コーンスティープリカ
ー）を主成分とするＢＯＤ約１５０ｍｇ／Ｌの合成廃水
を用いて汚泥減容化効果を検討した例を説明する。Next, using the wastewater treatment system according to the second embodiment, the effect of reducing the volume of sludge using synthetic wastewater having a BOD of about 150 mg / L containing food waste liquid (corn steep liquor) as a main component was examined. An example will be described.

【００４９】図６のフローで、汚泥処理系統４０の高圧
ポンプ４を運転しない場合、活性汚泥処理槽１の滞留時
間を１２時間、汚泥濃度を約２ｇ／Ｌとしたときの余剰
汚泥生成量は、約０．１ｋｇ−ＳＳ／ｍ3 ・日であっ
た。次に、高圧ポンプ４を運転し、余剰汚泥の７倍量に
あたる約０．７ｋｇ−ＳＳ／ｍ3 ・日をジェットノズル
処理したところ、活性汚泥処理槽の汚泥濃度が約２．２
ｇ／Ｌに幾分上昇したものの、余剰汚泥を引き抜く必要
がなく、第１の実施の形態と同様に、汚泥の全く生成し
ない廃水処理システムを構築できた。In the flow of FIG. 6, when the high-pressure pump 4 of the sludge treatment system 40 is not operated, the amount of surplus sludge generated when the residence time of the activated sludge treatment tank 1 is 12 hours and the sludge concentration is about 2 g / L is as follows. , About 0.1 kg-SS / m 3 · day. Next, the high-pressure pump 4 was operated to perform jet nozzle treatment of about 0.7 kg-SS / m 3 · day, which is seven times the amount of excess sludge, and the sludge concentration in the activated sludge treatment tank was about 2.2.
Although it increased to a little g / L, there was no need to pull out excess sludge, and a wastewater treatment system that did not generate any sludge could be constructed as in the first embodiment.

【００５０】図７は、本発明の活性汚泥の処理装置を、
有機性廃水を処理する廃水処理系統に組み込んだ廃水処
理システムの第３の実施の形態である。尚、第１及び第
２の実施の形態と同じ部材、装置には同符号を付して説
明する。FIG. 7 shows an activated sludge treatment apparatus of the present invention.
It is a third embodiment of a wastewater treatment system incorporated in a wastewater treatment system for treating organic wastewater. The same members and devices as those of the first and second embodiments are denoted by the same reference numerals and described.

【００５１】第３の実施の形態における廃水処理システ
ム１０は、廃水処理系統３０と汚泥処理系統４０とから
構成される。The wastewater treatment system 10 according to the third embodiment includes a wastewater treatment system 30 and a sludge treatment system 40.

【００５２】廃水処理系統は、活性汚泥処理槽１の前段
に無酸素槽８が設けられ、活性汚泥処理槽１から無酸素
槽８に汚泥循環路２０が連絡している以外は、図４の第
１の実施の形態と同様である。汚泥処理系統４０は、主
として、予備曝気槽７、高圧ポンプ４、リアクタ５から
構成され、予備曝気槽７は予備曝気装置２３が備えら
れ、リアクタ５は、ジェットノズル３１と容器３２から
構成される。In the wastewater treatment system, an anoxic tank 8 is provided in front of the activated sludge treatment tank 1, and a sludge circulation path 20 is connected from the activated sludge treatment tank 1 to the anoxic tank 8 in FIG. This is the same as in the first embodiment. The sludge treatment system 40 mainly includes a preliminary aeration tank 7, a high-pressure pump 4, and a reactor 5. The preliminary aeration tank 7 includes a preliminary aeration device 23. The reactor 5 includes a jet nozzle 31 and a container 32. .

【００５３】ここで、第３の実施の形態が第１及び第２
の実施の形態と異なる点を説明すると、廃水処理系統３
０では、有機性廃水を廃水管１１から無酸素槽８に導入
し、返送汚泥管１２から返送される返送汚泥および活性
汚泥処理槽１から汚泥循環路２０を通って循環される循
環汚泥とを混合し、循環汚泥や返送汚泥に含まれる酸化
態窒素の脱窒処理を行う。一方、汚泥処理系統４０で
は、汚泥引出管１５からの汚泥は、予備曝気槽７で予備
曝気された後、リアクタ５内でジェットノズル処理さ
れ、汚泥移送管１７を通って無酸素槽８に戻され、酸化
態窒素と反応して自己酸化して減容化する。Here, the third embodiment is different from the first and second embodiments.
The point different from the embodiment of the present invention will be described.
At 0, the organic wastewater is introduced from the wastewater pipe 11 into the oxygen-free tank 8, and the returned sludge returned from the returned sludge pipe 12 and the circulated sludge circulated from the activated sludge treatment tank 1 through the sludge circulation path 20 are separated. Mix and denitrify oxidized nitrogen contained in circulating sludge and returned sludge. On the other hand, in the sludge treatment system 40, the sludge from the sludge withdrawal pipe 15 is pre-aerated in the pre-aeration tank 7, jet-treated in the reactor 5, and returned to the oxygen-free tank 8 through the sludge transfer pipe 17. It reacts with oxidized nitrogen and self-oxidizes to reduce its volume.

【００５４】本発明の第３の実施の形態の場合にも、装
置の繁雑さと管理上の問題などを解消し、活性汚泥の分
散化処理後の溶液中のＣＯＤの増加や、活性汚泥中の微
生物の死滅を抑制できるので、処理水質を悪化させずに
汚泥の生成量を抑制し、余剰汚泥量を低減或いはゼロに
することができる。Also in the case of the third embodiment of the present invention, the complexity of the apparatus and the problems in management are solved, and the COD in the solution after the dispersion treatment of the activated sludge is increased, and Since the killing of microorganisms can be suppressed, the amount of generated sludge can be suppressed without deteriorating the quality of treated water, and the amount of excess sludge can be reduced or eliminated.

【００５５】図９は、本発明の活性汚泥の処理装置を、
有機性廃水を処理する廃水処理系統に組み込んだ廃水処
理システムの第４の実施の形態である。尚、第１及び第
３の実施の形態と同じ部材、装置には同符号を付してい
る。FIG. 9 shows an activated sludge treatment apparatus of the present invention.
It is a fourth embodiment of a wastewater treatment system incorporated in a wastewater treatment system for treating organic wastewater. The same members and devices as those in the first and third embodiments are denoted by the same reference numerals.

【００５６】第４の実施の形態における廃水処理システ
ム１０は、廃水処理系統３０と汚泥処理系統４０とから
構成されるが、廃水処理系統３０は第１の実施と形態と
同じにし、汚泥処理系統４０は第３の実施の形態と同じ
にしたものである。The wastewater treatment system 10 according to the fourth embodiment comprises a wastewater treatment system 30 and a sludge treatment system 40. The wastewater treatment system 30 is the same as that of the first embodiment. Reference numeral 40 is the same as in the third embodiment.

【００５７】第４の実施の形態における廃水処理システ
ム１０を使用して、下水を処理した場合の汚泥減容化効
果を検討した例を以下に説明する。An example in which the effect of sludge volume reduction when sewage is treated using the wastewater treatment system 10 according to the fourth embodiment will be described below.

【００５８】本発明（ＷＪ処理系）は、図９のフロー
で、活性汚泥処理槽１の容積を６００Ｌとし、下水を６
００Ｌ／日で連続供給した。１日に１回、活性汚泥処理
槽１の汚泥を５００Ｌに相当する量を、キャビテーショ
ン係数ａが０．０２でジェットノズル処理し、活性汚泥
処理槽１の汚泥濃度（ＭＬＳＳ）と処理水質（ＳＳ及び
溶解性ＣＯＤ）の経日変化を測定した。また、従来例と
して、図９のフローで汚泥処理系統４０を運転しない場
合について、同時に汚泥濃度と処理水質を測定した。
尚、活性汚泥（余剰汚泥）の引き抜きは行っていない。
その結果、図１０に示すように、約１０日間で、従来例
は汚泥濃度（ＭＬＳＳ）が初期の約２０００ｍｇ／Ｌか
ら２５００ｍｇ／Ｌ以上まで増加しているが、本発明で
は、ほぼ２０００ｍｇ／Ｌを維持し、汚泥の増加がみら
れない。また処理水質は、図１１に示すように、本発明
では、従来例と同様のＳＳ＜５ｍｇ／Ｌ、溶解性ＣＯＤ
（S -ＣＯＤ）＜１０ｍｇ／Ｌをほぼ満足する値が得ら
れた。以上のことから、本発明による廃水処理システム
により、処理水質をほとんど悪化させずに、余剰汚泥量
の低減が可能であることが示された。In the present invention (WJ treatment system), according to the flow of FIG.
It was supplied continuously at 00 L / day. Once a day, the amount of sludge in the activated sludge treatment tank 1 is jet nozzle treated in an amount corresponding to 500 L with a cavitation coefficient a of 0.02, and the sludge concentration (MLSS) and the treated water quality (SS) in the activated sludge treatment tank 1 are treated. And the change over time of the soluble COD) were measured. Further, as a conventional example, when the sludge treatment system 40 was not operated in the flow of FIG. 9, the sludge concentration and the treated water quality were measured at the same time.
The activated sludge (excess sludge) was not extracted.
As a result, as shown in FIG. 10, in about 10 days, the sludge concentration (MLSS) in the conventional example increased from about 2000 mg / L in the initial stage to 2500 mg / L or more, but in the present invention, it was almost 2000 mg / L. And no increase in sludge is observed. Further, as shown in FIG. 11, in the present invention, the treated water quality is the same as that of the conventional example: SS <5 mg / L, soluble COD
A value almost satisfying ( S- COD) <10 mg / L was obtained. From the above, it was shown that the wastewater treatment system according to the present invention can reduce the amount of excess sludge without substantially deteriorating the quality of treated water.

【００５９】尚、汚泥噴出手段は、加圧部・狭窄部・低
圧部から成る流路であることから、本発明の実施の形態
では、高圧ポンプ４（加圧部）、ジェットノズル３１
（狭窄部）、容器３２（低圧部）というように対応させ
たが、図１のウオータジェット装置そのものを使用して
もよいことはいうまでもない。Since the sludge jetting means is a flow path composed of a pressurized portion, a constricted portion, and a low-pressure portion, in the embodiment of the present invention, the high-pressure pump 4 (pressurized portion) and the jet nozzle 31 are used.
(Stenosis portion) and container 32 (low-pressure portion) are used, but it goes without saying that the water jet device itself shown in FIG. 1 may be used.

【００６０】尚、上記した第１〜第４の実施の形態で処
理する活性汚泥として、活性汚泥処理槽内の活性汚泥を
濃縮して得られるものを使用すると、処理効率を向上さ
せることができる。When activated sludge obtained by concentrating activated sludge in the activated sludge treatment tank is used as the activated sludge to be treated in the above-described first to fourth embodiments, the treatment efficiency can be improved. .

【００６１】[0061]

【発明の効果】以上説明したように、本発明の活性汚泥
の処理装置及び廃水処理システムによれば、処理水質の
悪化や装置の煩雑さによる管理上の問題がなく、簡単な
装置で汚泥の生成量を抑制し、余剰汚泥量を低減或いは
ゼロにすることができる。As described above, according to the activated sludge treatment apparatus and the wastewater treatment system of the present invention, there is no management problem due to the deterioration of treated water quality and the complexity of the apparatus. The amount of generated sludge can be suppressed, and the amount of excess sludge can be reduced or made zero.

【００６２】従って、廃水処理システムの系外に引き抜
く引抜汚泥が全く発生することのない廃水処理システム
を構築できる。Therefore, it is possible to construct a wastewater treatment system in which no extracted sludge is drawn out of the wastewater treatment system.

【図面の簡単な説明】[Brief description of the drawings]

【図１】ジェット状のキャビテーションを促進する機能
を有するノズルを備えたウオータジェット装置（ＷＪ）
の説明図FIG. 1 shows a water jet device (WJ) equipped with a nozzle having a function of promoting jet cavitation.
Illustration of

【図２】キャビテーション係数と汚泥減容化率の関係を
説明する説明図FIG. 2 is an explanatory diagram illustrating a relationship between a cavitation coefficient and a sludge volume reduction rate.

【図３】キャビテーション係数と微生物活性又は溶液中
ＣＯＤ濃度の関係を説明する説明図FIG. 3 is an explanatory diagram for explaining a relationship between a cavitation coefficient and a microbial activity or a COD concentration in a solution.

【図４】本発明の廃水処理システムの第１の実施の形態
の構成図FIG. 4 is a configuration diagram of a first embodiment of a wastewater treatment system of the present invention.

【図５】リアクタの構成例とその作用を示す説明図FIG. 5 is an explanatory diagram showing a configuration example of a reactor and its operation.

【図６】本発明の廃水処理システムの第２の実施の形態
の構成図FIG. 6 is a configuration diagram of a second embodiment of the wastewater treatment system of the present invention.

【図７】本発明の廃水処理システムの第３の実施の形態
の構成図FIG. 7 is a configuration diagram of a wastewater treatment system according to a third embodiment of the present invention.

【図８】ＷＪ処理による汚泥フロックの変化の推定概念
図FIG. 8 is a conceptual diagram of estimation of change in sludge floc due to WJ processing.

【図９】本発明の廃水処理システムの第４の実施の形態
の構成図FIG. 9 is a configuration diagram of a fourth embodiment of the wastewater treatment system of the present invention.

【図１０】本発明の廃水処理システムの第４の実施にお
いて、本発明と従来例との汚泥減容化試験の比較結果を
説明する説明図FIG. 10 is an explanatory diagram illustrating a comparison result of a sludge reduction test between the present invention and a conventional example in a fourth embodiment of the wastewater treatment system of the present invention.

【図１１】本発明の廃水処理システムの第４の実施にお
いて、本発明と従来例との処理水質の比較結果を説明す
る説明図FIG. 11 is an explanatory diagram illustrating a comparison result of treated water quality between the present invention and a conventional example in a fourth embodiment of the wastewater treatment system of the present invention.

【符号の説明】[Explanation of symbols]

Ａ…容器、Ｂ…入口、Ｃ…ノズル、Ｄ…噴出孔、Ｅ…ジ
ェット、Ｆ…容器内の活性汚泥、Ｇ…拡大空洞部、Ｈ…
渦、１…活性汚泥処理槽、２…汚泥分離槽、３…消化
槽、４…高圧ポンプ、５…リアクタ、６…汚泥濃縮槽、
７…予備曝気槽、８…無酸素槽、１０…廃水処理システ
ム、１２…返送汚泥管、１４…処理水管、１５…汚泥引
出管、１８…分離水流出管、２０…汚泥循環路、２１、
２２、２３…曝気装置、３０…廃水処理系統、３１…ジ
ェットノズル、３２…容器、４０…汚泥処理系統A: Container, B: Inlet, C: Nozzle, D: Jet hole, E: Jet, F: Activated sludge in the container, G: Expanded cavity, H:
Vortex, 1 ... Activated sludge treatment tank, 2 ... Sludge separation tank, 3 ... Digestion tank, 4 ... High pressure pump, 5 ... Reactor, 6 ... Sludge concentration tank,
7: Preliminary aeration tank, 8: Oxygen-free tank, 10: Wastewater treatment system, 12: Returned sludge pipe, 14: Treated water pipe, 15: Sludge withdrawal pipe, 18: Separated water outflow pipe, 20: Sludge circulation path, 21,
22, 23 aeration device, 30 wastewater treatment system, 31 jet nozzle, 32 container, 40 sludge treatment system

───────────────────────────────────────────────────── フロントページの続き (72)発明者 井坂 和一 東京都千代田区内神田１丁目１番14号 日 立プラント建設株式会社内 (72)発明者 麻生 伸二 東京都千代田区内神田１丁目１番14号 日 立プラント建設株式会社内 (72)発明者 江森 弘祥 東京都千代田区内神田１丁目１番14号 日 立プラント建設株式会社内 (72)発明者 佐藤 一教 広島県呉市宝町６番９号 バブコック日立 株式会社内 Ｆターム(参考） 4D028 AB03 BD11 4D040 BB05 BB12 BB22 BB57 BB65 BB91 4D059 AA05 BF20 BK11 BK12 BK16 BK30 EB20  ──────────────────────────────────────────────────続 き Continuing from the front page (72) Inventor Kazuichi Isaka 1-1-1 Uchikanda, Chiyoda-ku, Tokyo Inside Hitachi Plant Construction Co., Ltd. (72) Inventor Shinji Aso 1-1-1, Uchikanda, Chiyoda-ku, Tokyo No. 14 Hitachi Plant Construction Co., Ltd. (72) Inventor Hiroyoshi Emori 1-1-14 Uchikanda, Chiyoda-ku, Tokyo Inside Hitachi Plant Construction Co., Ltd. (72) Inventor Kazunori Sato Takaracho, Kure City, Hiroshima Prefecture No. 6-9 Babcock Hitachi F-term (reference) 4D028 AB03 BD11 4D040 BB05 BB12 BB22 BB57 BB65 BB91 4D059 AA05 BF20 BK11 BK12 BK16 BK30 EB20

Claims (5)

【特許請求の範囲】[Claims] 【請求項１】加圧部・狭窄部・低圧部から成る流路を有
し、前記加圧部で加圧した活性汚泥を前記狭窄部を介し
て前記低圧部に噴出させることにより前記活性汚泥を処
理する汚泥噴出手段と、 前記汚泥噴出手段で処理した活性汚泥を、酸素又は酸化
態窒素と反応させる減容化処理槽と、 を備えたことを特徴とする活性汚泥の処理装置。1. An activated sludge having a flow path comprising a pressurized portion, a constricted portion, and a low-pressure portion, wherein the activated sludge pressurized by the pressurized portion is jetted to the low-pressure portion through the constricted portion. A sludge ejecting means for treating the activated sludge, and a volume reduction treatment tank for reacting the activated sludge treated by the sludge ejecting means with oxygen or oxidized nitrogen. 【請求項２】前記狭窄部は、ジェット状のキャビテーシ
ョンを作り出すノズルであって、該キャビテーション
は、Ｐｊを前記狭窄部の上流側圧力、Ｐｒを前記狭窄部
の下流側圧力、Ｐｖを活性汚泥の蒸気圧としたときに、
キャビテーション係数ａの範囲が次式、 ０．００５＜ａ＜０．４ ａ＝（Ｐｒ−Ｐｖ）／（Ｐｊ−Ｐｒ） を満足することを特徴とする請求項１の活性汚泥の処理
装置。2. The stenosis portion is a nozzle for producing jet-shaped cavitation. In the cavitation, Pj is an upstream pressure of the stenosis portion, Pr is a downstream pressure of the stenosis portion, and Pv is a pressure of the activated sludge. When the vapor pressure is
The activated sludge treatment apparatus according to claim 1, wherein the range of the cavitation coefficient a satisfies the following expression: 0.005 <a <0.4a = (Pr-Pv) / (Pj-Pr). 【請求項３】前記減容化処理槽が、前記低圧部をも兼用
することを特徴とする請求項１又は２に記載の活性汚泥
の処理装置。3. The activated sludge treatment apparatus according to claim 1, wherein the volume reduction treatment tank also serves as the low-pressure section. 【請求項４】前記加圧部に活性汚泥を通過させる前に、
前記活性汚泥に空気又は酸素を含む気体を供給する供給
手段を設けたことを特徴とする請求項１〜３の何れかに
記載の活性汚泥の処理装置。4. Before passing activated sludge through the pressurizing section,
The activated sludge treatment apparatus according to any one of claims 1 to 3, further comprising a supply unit configured to supply a gas containing air or oxygen to the activated sludge. 【請求項５】有機性廃水を生物学的処理槽で処理する際
に得られる活性汚泥の一部を、請求項１又は２に記載の
汚泥噴出手段で処理した後、前記生物学的処理槽に戻し
て酸素又は酸化態窒素と反応させることを特徴とする廃
水処理システム。5. The biological treatment tank after a part of the activated sludge obtained when treating the organic wastewater in the biological treatment tank is treated by the sludge jetting means according to claim 1 or 2. A wastewater treatment system, wherein the wastewater treatment system is returned to oxygen and reacted with oxygen or oxidized nitrogen.
JP2000322830A 2000-03-01 2000-10-23 Activated sludge treatment apparatus and wastewater treatment system Pending JP2001314887A (en)

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2005066504A (en) * 2003-08-26 2005-03-17 Ataka Construction & Engineering Co Ltd Method and apparatus for treating sewage
JP2005508751A (en) * 2001-11-12 2005-04-07 エーエムウー ウンターヴァッサープムペン ゲゼルシャフト ミット ベシュレンクテル ハフツング Method and apparatus for treating effluent, sludge, and organic substrates
WO2009028481A1 (en) 2007-08-28 2009-03-05 Diamond Engineering Co., Ltd. Activated sludge material, reduction method of excess sludge amount in bioreactor, and maintenance method of bioreactor
JP4939940B2 (en) * 2003-08-29 2012-05-30 ビオニーク ゲーエムベーハー − イノヴァティーフェ テヒニーク フュア ディー ウムヴェルト Method and apparatus for pulverizing particulate organic material in a suspension of microorganisms
KR101164207B1 (en) * 2012-02-01 2012-07-11 박병진 Wast water treatment apparatus comprising tubular air supplier

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2005508751A (en) * 2001-11-12 2005-04-07 エーエムウー ウンターヴァッサープムペン ゲゼルシャフト ミット ベシュレンクテル ハフツング Method and apparatus for treating effluent, sludge, and organic substrates
JP2005066504A (en) * 2003-08-26 2005-03-17 Ataka Construction & Engineering Co Ltd Method and apparatus for treating sewage
JP4632397B2 (en) * 2003-08-26 2011-02-16 アタカ大機株式会社 Sewage treatment method and apparatus
JP4939940B2 (en) * 2003-08-29 2012-05-30 ビオニーク ゲーエムベーハー − イノヴァティーフェ テヒニーク フュア ディー ウムヴェルト Method and apparatus for pulverizing particulate organic material in a suspension of microorganisms
WO2009028481A1 (en) 2007-08-28 2009-03-05 Diamond Engineering Co., Ltd. Activated sludge material, reduction method of excess sludge amount in bioreactor, and maintenance method of bioreactor
US8603339B2 (en) 2007-08-28 2013-12-10 Diamond Engineering Co., Ltd. Activated sludge material, method for reducing excess sludge production in bioreactor, and method of controlling bioreactor
KR101164207B1 (en) * 2012-02-01 2012-07-11 박병진 Wast water treatment apparatus comprising tubular air supplier

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