JPH09206785A - Anaerobic treatment and apparatus therefor - Google Patents
Anaerobic treatment and apparatus thereforInfo
- Publication number
- JPH09206785A JPH09206785A JP1912796A JP1912796A JPH09206785A JP H09206785 A JPH09206785 A JP H09206785A JP 1912796 A JP1912796 A JP 1912796A JP 1912796 A JP1912796 A JP 1912796A JP H09206785 A JPH09206785 A JP H09206785A
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- anaerobic
- anaerobic treatment
- treatment
- liquid
- 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
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
- 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
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (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】本発明は有機性排液を嫌気性
微生物を含む汚泥の存在下にメタン発酵させて処理する
嫌気性処理方法および装置、特に有機性排液を一相式の
メタン発酵により処理して減溶化する嫌気性処理方法お
よ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 an anaerobic treatment method and apparatus for treating an organic waste liquid by methane fermentation in the presence of sludge containing anaerobic microorganisms, and more particularly to a one-phase methane fermentation of the organic waste liquid. TECHNICAL FIELD The present invention relates to an anaerobic treatment method and an apparatus for treating by anaerobic treatment to reduce the solubility.
【０００２】[0002]
【従来の技術】有機性汚泥、し尿、食品排水等のスラリ
ー状の高濃度有機性排液を嫌気性微生物の存在下に、一
相式メタン発酵によって処理する嫌気性処理方法は嫌気
性消化法とも呼ばれ、古くから行われている方法であ
る。この方法では有機性物質は嫌気槽において、嫌気性
微生物により、液化、低分子化、有機酸生成、メタン生
成のステップを経てメタンガスに転換される。一相式の
メタン発酵は単一相において酸生成相とメタン生成相が
並列的に起こるものであり、従来の下水汚泥の嫌気処理
のように発酵槽と脱離液分離槽の２槽に分けて２段処理
する場合でも、各槽において酸生成相とメタン生成相が
並列的に起こる場合は一相式の処理に含まれる。BACKGROUND ART Anaerobic digestion is an anaerobic digestion method that treats highly concentrated organic wastewater in the form of slurry such as organic sludge, human waste, food wastewater, etc. in the presence of anaerobic microorganisms. It is also called, and is a method that has been practiced since ancient times. In this method, an organic substance is converted into methane gas in an anaerobic tank by anaerobic microorganisms through the steps of liquefaction, molecular weight reduction, organic acid production, and methane production. In the single-phase methane fermentation, the acid-producing phase and the methanogenic phase occur in parallel in a single phase. It is divided into two tanks, a fermentation tank and a desorbed liquid separation tank, as in the conventional anaerobic treatment of sewage sludge. Even in the case of two-stage treatment, if the acid production phase and the methane production phase occur in parallel in each tank, they are included in the one-phase treatment.
【０００３】このような嫌気性処理においては、未分解
物質および嫌気性微生物を主体とする大量の汚泥が生成
する。この汚泥は生きた菌体を主体とするため、生物学
的には安定しており、さらに生物処理を行って大幅に減
量化することは困難であり、従来は機械脱水して焼却、
埋立等により処理されていた。In such an anaerobic treatment, a large amount of sludge mainly composed of undegraded substances and anaerobic microorganisms is produced. Since this sludge is mainly composed of living cells, it is biologically stable, and it is difficult to significantly reduce the amount by biological treatment.
It was processed by landfill.
【０００４】嫌気性処理により生成する汚泥量を減容化
する方法として、特開平１−２２４１００号には、嫌気
性消化した汚泥を１００〜１８０℃で加熱処理した後、
この加熱処理汚泥を嫌気消化槽に返送する有機性汚泥の
処理方法が記載されている。しかし、このような従来の
方法では汚泥の減容化は可能であるが、可溶化処理の条
件が高温で厳しいため、難生物分解性の有機物が生成し
て処理液の色度やＣＯＤが上昇して処理水質が悪化し、
しかも耐熱性、耐圧性の高い装置を必要とし、エネルギ
ー消費量が多く、コスト高になるという問題点がある。As a method for reducing the volume of sludge produced by anaerobic treatment, Japanese Patent Laid-Open No. 1-224100 discloses that anaerobic digested sludge is heated at 100 to 180 ° C.
There is described a method for treating organic sludge in which the heat-treated sludge is returned to the anaerobic digestion tank. However, although the sludge volume can be reduced by such a conventional method, the solubilization conditions are severe at a high temperature, and thus a biodegradable organic substance is generated to increase the chromaticity and COD of the treatment liquid. And the quality of treated water deteriorates,
In addition, there is a problem that a device having high heat resistance and pressure resistance is required, energy consumption is large, and cost is high.
【０００５】一方、有機性排液の好気性処理（活性汚泥
処理）により生成する余剰汚泥を減容化する方法とし
て、特開平６−２０６０８８号には、汚泥をオゾン処理
して曝気槽に返送する方法が記載されている。しかしこ
の方法は好気性処理に関するものであり、嫌気性処理に
おける適用の可能性については開示されていない。On the other hand, as a method for reducing the volume of surplus sludge produced by aerobic treatment (activated sludge treatment) of organic waste liquid, Japanese Patent Laid-Open No. 6-206088 discloses a method of treating sludge with ozone and returning it to an aeration tank. How to do is described. However, this method relates to aerobic treatment, and does not disclose the possibility of application in anaerobic treatment.
【０００６】[0006]
【発明が解決しようとする課題】本発明の目的は、上記
問題点を解決するため、処理水質の悪化を抑制し、しか
も簡単な装置と操作により低エネルギー消費量かつ低コ
ストで汚泥の減容化を行うことができる有機性排液の嫌
気性処理方法および装置を提案することである。In order to solve the above problems, the object of the present invention is to suppress the deterioration of treated water quality and reduce sludge volume with low energy consumption and low cost by a simple device and operation. A method and an apparatus for anaerobic treatment of organic effluent capable of performing liquefaction.
【０００７】[0007]
【課題を解決するための手段】本発明は次の有機性排液
の処理方法および装置である。 （１） 嫌気性微生物を含む汚泥の存在下に有機性排液
をメタン発酵させる嫌気性処理工程と、嫌気性処理工程
において生成する汚泥をオゾン処理または高圧パルス放
電処理により改質する改質工程と、改質汚泥を嫌気性処
理工程に返送する返送工程とを含む嫌気性処理方法。 （２） 嫌気性微生物を含む汚泥の存在下に有機性排液
をメタン発酵させる嫌気性処理槽と、嫌気性処理槽にお
いて生成する汚泥をオゾン処理または高圧パルス放電処
理により改質する改質装置と、改質汚泥を嫌気性処理槽
に返送する返送装置とを備えた嫌気性処理装置。The present invention is the following method and apparatus for treating organic waste liquid. (1) Anaerobic treatment step of methane-fermenting an organic waste liquid in the presence of sludge containing anaerobic microorganisms, and reforming step of reforming sludge produced in the anaerobic treatment step by ozone treatment or high-pressure pulse discharge treatment And an anaerobic treatment method including a returning step of returning the modified sludge to the anaerobic treatment step. (2) Anaerobic treatment tank for methane-fermenting an organic waste liquid in the presence of sludge containing anaerobic microorganisms, and a reformer for reforming sludge produced in the anaerobic treatment tank by ozone treatment or high-pressure pulse discharge treatment And an anaerobic treatment device comprising a returning device for returning the modified sludge to the anaerobic treatment tank.
【０００８】本発明において処理の対象となる有機性排
液は、嫌気処理によって処理される有機物を含有する排
液（汚泥を含む）である。固形物を含むスラリー状のも
のが処理に適しているが、固形物を含まない液状のもの
でもよい。また難生物分解性の有機物、無機物、セルロ
ース、紙、綿、ウール布、し尿中の固形物などが含有さ
れていてもよい。このような有機性排液としては下水、
下水初沈汚泥、し尿、浄化槽汚泥、食品工場排水、ビー
ル廃酵母その他の産業排液、これらの排液を処理した際
に生じる余剰汚泥等の汚泥などがあげられる。The organic drainage to be treated in the present invention is a drainage (including sludge) containing an organic substance treated by anaerobic treatment. A slurry containing solids is suitable for the treatment, but a liquid containing no solids may be used. Further, it may contain a biodegradable organic substance, inorganic substance, cellulose, paper, cotton, wool cloth, solid matter in human waste and the like. Such organic drainage is sewage,
Examples include sewage first settled sludge, human waste, septic tank sludge, food factory wastewater, beer waste yeast and other industrial effluents, and excess sludge generated when treating these effluents.
【０００９】嫌気性処理工程は嫌気性処理槽において嫌
気性微生物を含む汚泥の存在下に有機性排液をメタン発
酵させる工程であって、酸生成相とメタン生成相とが単
一相で起こる一相式のメタン発酵工程であり、発酵槽と
脱離液分離槽とを分けてそれぞれにおいて酸生成相とメ
タン生成相を行う二段階処理を行う場合も含まれる。こ
のため嫌気性微生物を含む汚泥は酸生成菌とメタン生成
菌を含む汚泥が用いられる。この工程では有機性物質
は、嫌気性処理槽において嫌気性微生物により液化→低
分子化→有機酸生成→メタン生成のステップによりメタ
ンガスに転換される。The anaerobic treatment step is a step of methane-fermenting an organic waste liquid in the presence of sludge containing anaerobic microorganisms in an anaerobic treatment tank, and an acid-producing phase and a methanogenic phase occur in a single phase. This is a one-phase methane fermentation process, and includes a case where a fermentation tank and a desorbed liquid separation tank are separated and a two-stage treatment is performed in which an acid generation phase and a methane generation phase are performed. Therefore, as sludge containing anaerobic microorganisms, sludge containing acid-producing bacteria and methanogenic bacteria is used. In this process, the organic substance is converted into methane gas in the anaerobic treatment tank by the steps of liquefaction → low molecular weight → organic acid generation → methane generation by the anaerobic microorganism.
【００１０】メタン発酵の条件としては、３５℃付近に
最適温度がある中温メタン生成菌、および５５℃付近に
最適温度を有する高温メタン生成菌が増殖するいずれの
温度条件も可能である。中温メタン生成菌は増殖速度が
遅いため滞留時間（ＳＲＴ）が長くなるが、比較的低温
での処理が可能であるため加温および保温のための設備
が簡単になる。これに対して高温メタン生成菌の場合は
加温および保温の設備が必要になるが、増殖速度が速い
ため滞留時間が短くなり、短時間での処理が可能にな
る。The methane fermentation conditions can be any temperature condition in which a mesophilic methanogen having an optimum temperature near 35 ° C. and a high temperature methanogen having an optimum temperature near 55 ° C. grow. Since the mesophilic methanogen has a slow growth rate and has a long residence time (SRT), it can be treated at a relatively low temperature, which simplifies the equipment for heating and heat retention. On the other hand, in the case of high-temperature methanogens, heating and heat-retaining equipment is required, but since the growth rate is high, the residence time is short and treatment can be performed in a short time.
【００１１】中温メタン生成菌を主体とする場合は増殖
速度がおそいため、嫌気性処理槽での汚泥の滞留時間は
１０日以上、望ましくは１５〜３０日程度が必要であ
る。これに対して高温メタン生成菌を主体とする場合は
増殖速度が速いことから、上記範囲よりも短い滞留時間
（例えば最小滞留時間として５日以上）とすることも可
能である。有機物負荷は０．６〜１．６ｋｇ−ＶＳＳ／
ｍ3・日、嫌気性処理槽内のＭＬＳＳ濃度は５，０００
〜１００，０００ｍｇ／ｌ、好ましくは３０，０００〜
６０，０００ｍｇ／ｌ、嫌気性処理温度は３０〜３８℃
または４５〜６０℃の条件で嫌気性処理することができ
る。When the mesophilic methanogens are the main constituents, the growth rate is slow, so that the residence time of sludge in the anaerobic treatment tank is required to be 10 days or longer, preferably about 15 to 30 days. On the other hand, when the high temperature methanogens are the main components, the growth rate is high, so that it is possible to make the residence time shorter than the above range (for example, 5 days or more as the minimum residence time). Organic matter load is 0.6-1.6kg-VSS /
m 3 · day, MLSS concentration in anaerobic treatment tank is 5,000
100,000 mg / l, preferably 30,000
60,000 mg / l, anaerobic treatment temperature is 30-38 ° C
Alternatively, anaerobic treatment can be performed under the condition of 45 to 60 ° C.
【００１２】嫌気性処理工程には、膜分離装置、デカン
ター、ろ過装置などの固液分離装置を用いる固液分離工
程を組合わせることができる。固液分離工程では嫌気性
処理槽内液の固液分離を行い、分離液を処理液として排
出するとともに、濃縮汚泥を嫌気性処理槽に戻すように
構成される。膜分離を利用する場合は、中空糸、チュー
ブラー、平膜などの種々の膜形式が利用できる。また膜
分離は固形物を分離することが目的であるため、ＭＦ、
ＵＦなどの比較的大きなポアサイズを有する膜が好まし
い。The anaerobic treatment process can be combined with a solid-liquid separation process using a solid-liquid separation device such as a membrane separation device, a decanter and a filtration device. In the solid-liquid separation step, the liquid in the anaerobic treatment tank is subjected to solid-liquid separation, the separated liquid is discharged as a treatment liquid, and the concentrated sludge is returned to the anaerobic treatment tank. When using membrane separation, various membrane types such as hollow fiber, tubular, and flat membrane can be used. Since the purpose of membrane separation is to separate solids, MF,
Membranes with relatively large pore sizes such as UF are preferred.
【００１３】改質工程はこのような嫌気性処理工程にお
ける処理系から生物汚泥の一部を改質装置において、オ
ゾン処理またはパルス放電処理により易生物分解性に改
質する工程である。生物汚泥を引抜く場合、固液分離装
置で分離された濃縮汚泥を引抜いて改質処理するのが好
ましいが、嫌気性処理槽から混合液の状態で引抜いて処
理してもよい。また場合によっては嫌気性処理槽内にこ
れらの改質装置を設けることもできる。The reforming step is a step of reforming a part of the biological sludge from the treatment system in the anaerobic treatment step in the reforming apparatus by ozone treatment or pulse discharge treatment so as to be easily biodegradable. When the biological sludge is extracted, it is preferable to extract the concentrated sludge separated by the solid-liquid separation device for reforming treatment, but it may be extracted from the anaerobic treatment tank in a mixed liquid state for treatment. Further, in some cases, these reforming devices can be provided in the anaerobic treatment tank.
【００１４】オゾン処理は、汚泥をオゾンと接触させる
ことにより行う。接触方法としては、オゾン処理槽に消
化汚泥を導入してオゾンを吹込む方法、機械攪拌による
方法、充填層を利用する方法などが採用できる。オゾン
としてはオゾンガスの他、オゾン含有空気、オゾン化空
気などが使用できる。オゾンの使用量は０．００５〜
０．０４ｇ−Ｏ3／ｇ−ＶＳＳ、好ましくは０．０１〜
０．０３ｇ−Ｏ3／ｇ−ＶＳＳとするのが望ましい。充
填層を用いる場合は充填層のＳＶを１〜１０ｈｒ-1、望
ましくは３〜６ｈｒ-1とするのが好ましい。The ozone treatment is carried out by bringing sludge into contact with ozone. As a contact method, a method of introducing digested sludge into an ozone treatment tank and blowing ozone, a method of mechanical stirring, a method of utilizing a packed bed, and the like can be adopted. As ozone, ozone-containing air, ozonized air, or the like can be used in addition to ozone gas. The amount of ozone used is 0.005
0.04 g-O 3 / g-VSS, preferably 0.01-
It is preferably 0.03 g-O 3 / g-VSS. When the packed bed is used, the SV of the packed bed is preferably set to 1 to 10 hr -1 , desirably 3 to 6 hr -1 .
【００１５】高電圧のパルス放電処理は、電極間隔３〜
１０ｍｍ、好ましくは４〜８ｍｍのタングステン／トリ
ウム合金等の＋極と、ステンレス鋼等の−極間に汚泥を
存在させ、印加電圧１０〜５０ｋＶ、好ましくは２０〜
４０ｋＶ、パルス間隔２０〜８０Ｈｚ、好ましくは４０
〜６０Ｈｚでパルス放電を行い、汚泥は順次循環させな
がら処理を行うことができる。The high-voltage pulse discharge process is performed with an electrode interval of 3 to
Sludge is allowed to exist between a positive electrode such as a tungsten / thorium alloy of 10 mm, preferably 4 to 8 mm, and a negative electrode of stainless steel, and an applied voltage is 10 to 50 kV, preferably 20 to
40 kV, pulse interval 20-80 Hz, preferably 40
The pulse discharge is performed at -60 Hz, and the sludge can be treated while being sequentially circulated.
【００１６】嫌気性処理槽から引抜いて改質を行う汚泥
量は、汚泥の減容効果を確保するために少なくとも嫌気
性処理槽へ投入する固形物量と同等以上、好ましくは２
倍以上が良い。例えば１５日滞留の嫌気性処理槽であれ
ば、循環比は１／１５ｄａｙ -1以上、好ましくは２／１
５ｄａｙ-1以上とすることができる。循環比の上限値は
有効な嫌気性処理の確保の点から、１日あたり嫌気性処
理槽の全保有汚泥量の１／１５以下、好ましくは１／１
５〜１／５０の量（固形分重量）に相当する量とするの
が望ましい。Sludge drawn from an anaerobic treatment tank for reforming
The amount should be at least anaerobic to ensure the sludge volume reduction effect.
Equal to or greater than the amount of solids charged to the oxidative treatment tank, preferably 2
More than double is good. For example, if it is an anaerobic treatment tank that stays for 15 days,
For example, the circulation ratio is 1 / 15day -1Above, preferably 2/1
5 days-1The above can be done. The upper limit of the circulation ratio is
From the viewpoint of ensuring effective anaerobic treatment, anaerobic treatment per day
1/15 or less, preferably 1/1 of the total amount of sludge in the tank
5 to 1/50 (solid weight)
Is desirable.
【００１７】このように引抜く汚泥の量を投入する固形
物量の１倍以上の量とすることにより、処理系全体とし
ての汚泥の減容化を高くすることができ、また嫌気性処
理槽の全保有汚泥量の１／１５以下とすることにより、
嫌気性処理槽全体としての汚泥活性を高く維持した状態
で嫌気性処理を有効に行うことができる。嫌気性処理槽
が発酵槽と脱離液分離槽の２個に分けられた２段処理の
場合には、改質処理のための汚泥の引抜は１段目、２段
目いずれからでもよい。By thus setting the amount of sludge to be drawn out to be at least one time the amount of solid matter to be added, the volume reduction of sludge in the entire treatment system can be increased, and the anaerobic treatment tank By reducing the total amount of sludge to 1/15 or less,
The anaerobic treatment can be effectively performed in a state where the sludge activity of the entire anaerobic treatment tank is maintained high. In the case of a two-stage treatment in which the anaerobic treatment tank is divided into a fermentation tank and a desorbed liquid separation tank, the sludge may be drawn out for the reforming treatment from either the first or second step.
【００１８】返送工程は改質工程で改質された汚泥を嫌
気性処理工程に返送する工程であり、嫌気性処理工程か
ら汚泥を引抜く場合はこの引抜と返送を組合せて循環工
程とすることができる。嫌気性処理槽内において改質を
行う場合は、嫌気性処理槽内の液が循環するように構成
する。The returning step is a step of returning the sludge modified in the reforming step to the anaerobic treatment step. When the sludge is extracted from the anaerobic treatment step, the extraction and the return must be combined to form a circulation step. You can When the reforming is performed in the anaerobic treatment tank, the liquid in the anaerobic treatment tank is circulated.
【００１９】本発明の嫌気性処理装置による処理方法
は、嫌気性処理工程において、有機性排液を嫌気性処理
槽に導入して、嫌気性微生物を含む汚泥と混合して嫌気
性処理を行い、メタン発酵を起こさせる。ここでは有機
性物質は液化、低分子化、有機酸生成、メタン生成のス
テップを経てメタンガスに転換される。嫌気性処理槽内
の液は固液分離装置において固液分離し、分離液は処理
液として排出し、濃縮汚泥は嫌気性処理槽に返送する。In the treatment method using the anaerobic treatment apparatus of the present invention, in the anaerobic treatment step, the organic waste liquid is introduced into the anaerobic treatment tank and mixed with sludge containing anaerobic microorganisms to perform anaerobic treatment. , Cause methane fermentation. Here, the organic substance is converted into methane gas through the steps of liquefaction, molecular weight reduction, organic acid generation, and methane generation. The liquid in the anaerobic treatment tank is subjected to solid-liquid separation in a solid-liquid separator, the separated liquid is discharged as a treatment liquid, and the concentrated sludge is returned to the anaerobic treatment tank.
【００２０】上記嫌気性処理槽内の汚泥を含む液または
濃縮汚泥の一部は改質装置において、オゾン処理または
高圧パルス放電処理により易生物分解性に改質する。嫌
気性処理工程では汚泥中の微生物の増殖により菌体が増
加するが、生きている菌体を濃縮して嫌気性処理槽に戻
しても消化による減容化には限度がある。A part of the liquid containing sludge or the concentrated sludge in the anaerobic treatment tank is easily biodegradable by ozone treatment or high-pressure pulse discharge treatment in a reformer. In the anaerobic treatment process, the bacterial cells increase due to the growth of microorganisms in the sludge, but even if the living bacterial cells are concentrated and returned to the anaerobic treatment tank, there is a limit to the volume reduction by digestion.
【００２１】ところが改質装置においてオゾン処理また
は高圧パルス放電処理等により改質を行うことにより汚
泥中の菌体は死滅し、その他の有機物とともに分解され
て、低分子の有機物および一部無機物が生成し、易生物
分解性に改質される。このような改質汚泥は嫌気性処理
槽に循環することにより、嫌気性微生物の基質として利
用され分解される。これにより汚泥は減容化され、余剰
汚泥として排出される汚泥量は減少する。However, by performing reforming by ozone treatment or high-pressure pulse discharge treatment in the reforming device, the cells in the sludge are killed and decomposed together with other organic substances to form low-molecular organic substances and some inorganic substances. However, it is easily biodegradable. By circulating such modified sludge in the anaerobic treatment tank, it is used as a substrate for anaerobic microorganisms and decomposed. This reduces the volume of sludge and reduces the amount of sludge discharged as excess sludge.
【００２２】嫌気性処理工程から余剰汚泥として排出さ
れる汚泥を全量改質して循環しても、これを資化して汚
泥が増殖するため、嫌気性処理槽内の汚泥は増量してい
き、一部の汚泥を余剰汚泥として排出しなければなら
ず、排出汚泥をゼロに近づけることはできない。そこで
余剰汚泥量がゼロとなるように、余剰汚泥として発生す
る汚泥量より多い汚泥を抜出し、これを改質処理して循
環すると、過剰に抜出した汚泥量と増殖した汚泥量がバ
ランスし、見掛上汚泥の増加量がゼロに近づく。この場
合でも無機化した汚泥の蓄積を避けるために、最小限の
消化汚泥を排出するのが望ましい。Even if all sludge discharged as excess sludge from the anaerobic treatment step is reformed and circulated, the sludge grows by assimilating this and the sludge in the anaerobic treatment tank increases, Some sludge must be discharged as excess sludge, and discharged sludge cannot approach zero. Therefore, if you extract more sludge than the amount of excess sludge generated so that the amount of excess sludge becomes zero, and modify and circulate this sludge, the amount of excess sludge and the amount of grown sludge balance, The increase in the amount of hanging sludge approaches zero. Even in this case, it is desirable to discharge the minimum digested sludge in order to avoid the accumulation of mineralized sludge.
【００２３】このように過剰の汚泥を改質処理すると、
消化効率は低下するが、嫌気性処理槽では通常ＳＲＴを
１５日程度と比較的長くとって運転されるため、改質処
理によりＳＲＴが短くなっても余裕のある運転が可能で
あり、効率の低下はそれほど重大ではない。When the excess sludge is reformed as described above,
Although the digestion efficiency decreases, the anaerobic treatment tank is usually operated with a relatively long SRT of about 15 days, so that even if the SRT is shortened due to the reforming treatment, there is a margin of operation, and the efficiency is improved. The decline is not so serious.
【００２４】嫌気性処理工程の処理液はそのまま下水等
へ放流することができるが、好気性生物処理その他の後
処理を行ったのち放流してもよい。The treatment liquid of the anaerobic treatment step can be discharged as it is to sewage or the like, but it may be discharged after aerobic biological treatment and other post-treatments.
【００２５】[0025]
【発明の実施の形態】次に本発明の実施の形態を図面に
より説明する。図１および図２はそれぞれ別の実施の形
態の嫌気性処理装置を示す系統図であり、図１は嫌気性
処理液を固液分離装置により濃縮した濃縮汚泥を改質す
る例、図２は嫌気性処理槽内の混合液を改質する例を示
している。Embodiments of the present invention will now be described with reference to the drawings. 1 and 2 are system diagrams showing an anaerobic treatment apparatus according to different embodiments, FIG. 1 is an example of reforming concentrated sludge in which an anaerobic treatment liquid is concentrated by a solid-liquid separator, and FIG. An example of reforming the mixed liquid in the anaerobic treatment tank is shown.
【００２６】図１において、１は嫌気性処理槽、２は固
液分離装置としての膜分離装置、３は改質槽である。図
１の処理装置では、嫌気性処理槽１は被処理液路４から
有機性排液を導入し、返送汚泥路５を通して返送される
返送汚泥および嫌気性処理槽１内の嫌気性生物汚泥と混
合し、攪拌器６により緩やかに攪拌しながら嫌気性処理
を行うように構成されている。ここで行われる嫌気性処
理により、被処理液中の有機物は酸生成菌およびメタン
生成菌により分解される。生成するメタンガスを含む消
化ガスは排ガス路７から排出する。In FIG. 1, 1 is an anaerobic treatment tank, 2 is a membrane separator as a solid-liquid separator, and 3 is a reforming tank. In the treatment apparatus of FIG. 1, the anaerobic treatment tank 1 introduces the organic waste liquid from the liquid to be treated 4 and returns the sludge returned through the return sludge passage 5 and the anaerobic biological sludge in the anaerobic treatment tank 1. The anaerobic treatment is performed while mixing and gently stirring with the stirrer 6. By the anaerobic treatment performed here, organic substances in the liquid to be treated are decomposed by acid-producing bacteria and methanogenic bacteria. The digestion gas containing the produced methane gas is discharged from the exhaust gas passage 7.
【００２７】膜分離装置２は、嫌気性処理槽１内の混合
液の一部は連絡路１１から取出し、ポンプ１２で加圧し
て膜分離装置２に導いて、分離膜１３により膜分離する
ように構成されている。ここで行われる膜分離により透
過液１４と濃縮汚泥１５とに分離される。透過液１４は
処理液として処理液路１６から系外に排出される。濃縮
汚泥１５の一部は濃縮液取出路１７から取出して改質処
理槽３に導入し、残部の一部または全部は返送汚泥路５
から嫌気性処理槽１に返送される。余剰汚泥が生じる場
合は余剰汚泥排出路１８から系外へ排出される。In the membrane separation device 2, part of the mixed liquid in the anaerobic treatment tank 1 is taken out from the communication path 11, pressurized by the pump 12 and guided to the membrane separation device 2, and separated by the separation membrane 13. Is configured. The permeation liquid 14 and the concentrated sludge 15 are separated by the membrane separation performed here. The permeated liquid 14 is discharged as a processing liquid from the processing liquid passage 16 to the outside of the system. A part of the concentrated sludge 15 is taken out from the concentrated liquid take-out path 17 and introduced into the reforming treatment tank 3, and a part or all of the remaining part is returned to the sludge path 5.
Is returned to the anaerobic treatment tank 1. When excess sludge is produced, it is discharged from the excess sludge discharge path 18 to the outside of the system.
【００２８】改質槽３はオゾン処理槽が用いられてお
り、充填層２１に濃縮汚泥１５を通過させ、オゾン発生
器２２からオゾンを吹込んで接触させてオゾン処理する
ことにより汚泥が改質される。改質汚泥は改質汚泥路２
３から嫌気性処理槽１に戻し、嫌気処理する。こうして
改質により易生物分解性に改質された固形分が嫌気性処
理槽１で消化され、処理系から生じる余剰汚泥が減容化
する。An ozone treatment tank is used as the reforming tank 3, and the sludge is reformed by passing the concentrated sludge 15 through the packed bed 21 and blowing the ozone from the ozone generator 22 into contact with the sludge for ozone treatment. It Modified sludge is modified sludge path 2
It is returned from 3 to the anaerobic treatment tank 1 and anaerobic treatment is performed. In this way, the solid content that has been easily biodegradable by the reforming is digested in the anaerobic treatment tank 1, and the excess sludge generated from the treatment system is reduced in volume.
【００２９】図２の処理装置は、嫌気性処理槽１内の混
合液の一部を引抜汚泥として汚泥引抜路２４から引抜
き、この引抜汚泥を改質槽３に導入して改質処理を行う
ように構成される。改質槽３は高圧パルス放電処理を行
うように構成され、＋極２５および−極２６間に電源装
置２７から高圧パルスを印加して放電を行い、汚泥を改
質させる。膜分離装置２の濃縮汚泥は嫌気性処理槽１に
返送される。In the treatment apparatus shown in FIG. 2, a part of the mixed liquid in the anaerobic treatment tank 1 is drawn out as sludge from the sludge drawing passage 24, and the drawn sludge is introduced into the reforming tank 3 to carry out a reforming process. Is configured as follows. The reforming tank 3 is configured to perform a high-voltage pulse discharge treatment, and applies a high-voltage pulse from the power supply device 27 between the + pole 25 and the − pole 26 to perform discharge to reform the sludge. The concentrated sludge of the membrane separation device 2 is returned to the anaerobic treatment tank 1.
【００３０】図１および図２では、固液分離装置として
膜分離装置２を使用しているが、沈殿装置、遠心分離装
置などの他の固液分離装置を採用することもできる。ま
た図１では、返送汚泥路５からの汚泥の返送を省略する
こともできる。Although the membrane separator 2 is used as the solid-liquid separator in FIGS. 1 and 2, other solid-liquid separators such as a precipitation device and a centrifugal separator can be used. Further, in FIG. 1, the returning of the sludge from the returning sludge passage 5 can be omitted.
【００３１】[0031]
実施例１、比較例１ 有効容量２ literのジャーファーメンターを用いて、液
量１．２ literの嫌気性処理槽とし、下水処理場の余剰
汚泥をＴＳとして約２重量％に濃縮した原泥を１日に１
回８０ｍｌずつシリンジで供給した。嫌気性処理槽には
分画分子量３万、膜面積１７７ｃｍ2の平膜モジュール
を有する膜分離装置を接続して、ポンプで循環しながら
１日に８０ｍｌずつ槽内液をろ過し、槽内液量が一定に
なるように循環した。嫌気性処理槽は温度３５℃で制御
し、種汚泥としてＵＡＳＢのグラニュールを約５０ｍｌ
添加した。Example 1 and Comparative Example 1 A jar fermenter with an effective capacity of 2 liters was used as an anaerobic treatment tank with a liquid volume of 1.2 liters, and excess sludge from a sewage treatment plant was concentrated to about 2% by weight as raw sludge. 1 a day
80 ml each was supplied by a syringe. The anaerobic treatment tank is connected to a membrane separation device having a flat membrane module with a molecular weight cutoff of 30,000 and a membrane area of 177 cm 2 , and 80 ml of liquid per tank is filtered while circulating with a pump. It was circulated so that the amount was constant. The anaerobic treatment tank is controlled at a temperature of 35 ° C, and about 50 ml of UASB granules are used as seed sludge.
Was added.
【００３２】実施例１では改質処理槽として高圧パルス
放電装置を用い、１日に１回、原泥供給量と同一量の汚
泥８０ｍｌをシリンジで引抜き、容量１５０ｍｌのセル
中に導入し、タングステン／トリウム合金製の＋極とス
テンレス鋼製の−極間に、電極間隔：５ｍｍ、印加電
圧：３０ｋＶ、パルス間隔：５０Ｈｚで１０分間高圧パ
ルス放電を行って改質処理した後に嫌気性処理槽に戻し
た。In Example 1, a high-pressure pulse discharge device was used as a reforming treatment tank, and once a day, 80 ml of sludge, which was the same amount as the amount of raw sludge supplied, was drawn out with a syringe and introduced into a cell having a capacity of 150 ml. / Between the positive electrode made of thorium alloy and the negative electrode made of stainless steel, electrode interval: 5 mm, applied voltage: 30 kV, pulse interval: 50 Hz, high-voltage pulse discharge was performed for 10 minutes for modification treatment, and then anaerobic treatment tank. I brought it back.
【００３３】比較例１として改質処理を全く行わないも
のも同時にテストして、槽内の汚泥濃度の変化を比較し
た。ガス発生量の経日変化を図３に、ＴＳ濃度の経日変
化を図４に示す。これらの結果から、実施例１では比較
例１に比べて汚泥の分解率が高まり、実質的に余剰汚泥
がほとんど出ない程度まで減容化されていることがわか
る。As Comparative Example 1, a sample which was not subjected to any modification treatment was also tested at the same time to compare changes in the sludge concentration in the tank. FIG. 3 shows the daily change of the gas generation amount, and FIG. 4 shows the daily change of the TS concentration. From these results, it can be seen that in Example 1, the sludge decomposition rate was higher than in Comparative Example 1, and the volume was reduced to the extent that substantially no excess sludge was produced.
【００３４】実施例２ 実施例２では実施例１における改質処理槽としてオゾン
処理槽を用い、１日に１回、原泥供給量と同一量の汚泥
８０ｍｌをシリンジで引抜き、オゾン注入率を０．０５
ｇ−Ｏ3／ｇ−ＴＳの条件でオゾン処理して改質処理し
た後に嫌気性処理槽に戻した。実施例１と同様にテスト
して、オゾン処理を全く行わない比較例１と槽内の汚泥
濃度の変化を比較した。Example 2 In Example 2, the ozone treatment tank was used as the reforming treatment tank in Example 1, and once a day, 80 ml of sludge having the same amount as the raw sludge supply amount was drawn out by a syringe to measure the ozone injection rate. 0.05
It was returned to the anaerobic treatment tank after processing reformed to ozone treatment under the conditions of the g-O 3 / g-TS . The same test as in Example 1 was performed to compare the change in sludge concentration in the tank with Comparative Example 1 in which no ozone treatment was performed.
【００３５】その結果、実施例１と同様、オゾン処理を
施した実施例２は嫌気性消化槽内の汚泥濃度はＴＳとし
て１．８重量％で安定していたが、比較例１は継続して
上昇し運転開始３０日目には５重量％以上に達した。こ
れらの結果から、実施例１と同様に、実施例２でも比較
例１に比べて汚泥の分解率が高まり、実質的に余剰汚泥
がほとんどでない程度まで減容化されていることが明か
である。As a result, as in Example 1, Example 2 which was subjected to ozone treatment had a stable sludge concentration of 1.8 wt% as TS in the anaerobic digestion tank, but Comparative Example 1 was continued. It increased to 5% by weight or more on the 30th day from the start of operation. From these results, it is clear that, similarly to Example 1, Example 2 has a higher sludge decomposition rate than Comparative Example 1, and the volume is reduced to the extent that substantially no excess sludge is present. .
【００３６】[0036]
【発明の効果】本発明の嫌気性処理方法および装置によ
れば、嫌気性処理槽における嫌気性処理工程で生成する
汚泥をオゾン処理または高圧パルス放電処理により改質
して嫌気性処理を行うため、色度やＣＯＤが上昇するな
どの処理水質の悪化を抑制して汚泥の減容化を行うこと
ができる。また従来の加熱処理と比べてエネルギー消費
量を少なくすることができ、かつ耐熱性および耐圧性の
高い装置を使用する必要がなくなり、このため低コスト
での処理が可能となる。According to the anaerobic treatment method and apparatus of the present invention, the sludge produced in the anaerobic treatment step in the anaerobic treatment tank is reformed by ozone treatment or high-pressure pulse discharge treatment to perform anaerobic treatment. It is possible to reduce the volume of sludge by suppressing deterioration of treated water quality such as increase in chromaticity and COD. In addition, the energy consumption can be reduced as compared with the conventional heat treatment, and it is not necessary to use a device having high heat resistance and pressure resistance, and therefore the treatment can be performed at low cost.
【図１】本発明の実施形態の嫌気性処理装置を示す系統
図である。FIG. 1 is a system diagram showing an anaerobic treatment apparatus according to an embodiment of the present invention.
【図２】本発明の他の実施形態の嫌気性処理装置を示す
系統図である。FIG. 2 is a system diagram showing an anaerobic treatment apparatus according to another embodiment of the present invention.
【図３】実施例１および比較例１のガス発生量の経日変
化を示すグラフである。FIG. 3 is a graph showing changes with time of gas generation amounts in Example 1 and Comparative Example 1.
【図４】実施例１および比較例１のＴＳ濃度の経日変化
を示すグラフである。FIG. 4 is a graph showing changes with time of TS concentrations in Example 1 and Comparative Example 1.
１ 嫌気性処理槽 ２ 膜分離装置 ３ 改質槽 ４ 被処理液路 ５ 返送汚泥路 ６、２２ 攪拌器 ７ 排ガス路 １１ 連絡路 １２ ポンプ １３ 分離膜 １４ 透過液 １５ 濃縮汚泥 １６ 処理液路 １７ 濃縮液取出路 １８ 余剰汚泥排出路 ２１ 充填層 ２２ オゾン発生器 ２３ 改質汚泥路 ２４ 汚泥引抜路 ２５ ＋極 ２６ −極 1 Anaerobic treatment tank 2 Membrane separation device 3 Reforming tank 4 Treated liquid passage 5 Return sludge passage 6, 22 Stirrer 7 Exhaust gas passage 11 Communication passage 12 Pump 13 Separation membrane 14 Permeate 15 Concentrated sludge 16 Treatment liquid passage 17 Concentration Liquid extraction passage 18 Excess sludge discharge passage 21 Packed bed 22 Ozone generator 23 Reforming sludge passage 24 Sludge extraction passage 25 + pole 26-pole
─────────────────────────────────────────────────────
─────────────────────────────────────────────────── ───
【手続補正書】[Procedure amendment]
【提出日】平成８年２月８日[Submission date] February 8, 1996
【手続補正１】[Procedure amendment 1]
【補正対象書類名】図面[Document name to be amended] Drawing
【補正対象項目名】図１[Correction target item name] Fig. 1
【補正方法】変更[Correction method] Change
【補正内容】[Correction contents]
【図１】 FIG.
【手続補正２】[Procedure amendment 2]
【補正対象書類名】図面[Document name to be amended] Drawing
【補正対象項目名】図２[Correction target item name] Figure 2
【補正方法】変更[Correction method] Change
【補正内容】[Correction contents]
【図２】 [Fig. 2]
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 庁内整理番号 ＦＩ 技術表示箇所 Ｃ０２Ｆ 11/06 Ｃ０２Ｆ 11/06 ─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 6 Identification code Internal reference number FI technical display location C02F 11/06 C02F 11/06
Claims (2)
性排液をメタン発酵させる嫌気性処理工程と、 嫌気性処理工程において生成する汚泥をオゾン処理また
は高圧パルス放電処理により改質する改質工程と、 改質汚泥を嫌気性処理工程に返送する返送工程とを含む
嫌気性処理方法。1. An anaerobic treatment step of methane-fermenting an organic waste liquid in the presence of sludge containing anaerobic microorganisms, and a modification of reforming sludge produced in the anaerobic treatment step by ozone treatment or high-pressure pulse discharge treatment. An anaerobic treatment method including a quality process and a returning process for returning the modified sludge to the anaerobic treatment process.
性排液をメタン発酵させる嫌気性処理槽と、 嫌気性処理槽において生成する汚泥をオゾン処理または
高圧パルス放電処理により改質する改質装置と、 改質汚泥を嫌気性処理槽に返送する返送装置とを備えた
嫌気性処理装置。2. An anaerobic treatment tank for methane-fermenting an organic waste liquid in the presence of sludge containing anaerobic microorganisms, and a modification for reforming sludge produced in the anaerobic treatment tank by ozone treatment or high-pressure pulse discharge treatment. An anaerobic treatment device equipped with a quality device and a return device for returning the modified sludge to the anaerobic treatment tank.
Priority Applications (1)
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|---|---|---|---|
| JP1912796A JPH09206785A (en) | 1996-02-05 | 1996-02-05 | Anaerobic treatment and apparatus therefor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1912796A JPH09206785A (en) | 1996-02-05 | 1996-02-05 | Anaerobic treatment and apparatus therefor |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2004114629A Division JP4311264B2 (en) | 2004-04-08 | 2004-04-08 | Anaerobic treatment method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH09206785A true JPH09206785A (en) | 1997-08-12 |
Family
ID=11990806
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1912796A Pending JPH09206785A (en) | 1996-02-05 | 1996-02-05 | Anaerobic treatment and apparatus therefor |
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| Country | Link |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002186992A (en) * | 2000-12-19 | 2002-07-02 | Kurita Water Ind Ltd | Biological de-phosphorization apparatus |
| JP2002301495A (en) * | 2001-04-03 | 2002-10-15 | Kurita Water Ind Ltd | Apparatus and method for anaerobic digestion |
| US6884355B2 (en) | 2002-06-05 | 2005-04-26 | Mitsubishi Denki Kabushiki Kaisha | Process for treating organic wastewater and apparatus for treating the organic wastewater |
| JP2005349335A (en) * | 2004-06-11 | 2005-12-22 | Kurita Water Ind Ltd | Method for anaerobically digesting organic sludge |
| KR101238314B1 (en) * | 2010-12-16 | 2013-02-28 | 주식회사 포휴먼 | An apparatus of high voltage pulse discharge for ballast water treatment |
-
1996
- 1996-02-05 JP JP1912796A patent/JPH09206785A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002186992A (en) * | 2000-12-19 | 2002-07-02 | Kurita Water Ind Ltd | Biological de-phosphorization apparatus |
| JP2002301495A (en) * | 2001-04-03 | 2002-10-15 | Kurita Water Ind Ltd | Apparatus and method for anaerobic digestion |
| JP4595230B2 (en) * | 2001-04-03 | 2010-12-08 | 栗田工業株式会社 | Anaerobic digestion apparatus and anaerobic digestion method |
| US6884355B2 (en) | 2002-06-05 | 2005-04-26 | Mitsubishi Denki Kabushiki Kaisha | Process for treating organic wastewater and apparatus for treating the organic wastewater |
| JP2005349335A (en) * | 2004-06-11 | 2005-12-22 | Kurita Water Ind Ltd | Method for anaerobically digesting organic sludge |
| JP4576893B2 (en) * | 2004-06-11 | 2010-11-10 | 栗田工業株式会社 | Anaerobic digestion of organic sludge |
| KR101238314B1 (en) * | 2010-12-16 | 2013-02-28 | 주식회사 포휴먼 | An apparatus of high voltage pulse discharge for ballast water treatment |
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