JP2001327998A - Organic sludge digesting method - Google Patents
Organic sludge digesting methodInfo
- Publication number
- JP2001327998A JP2001327998A JP2000157993A JP2000157993A JP2001327998A JP 2001327998 A JP2001327998 A JP 2001327998A JP 2000157993 A JP2000157993 A JP 2000157993A JP 2000157993 A JP2000157993 A JP 2000157993A JP 2001327998 A JP2001327998 A JP 2001327998A
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- ozone
- tank
- anaerobic
- digestion tank
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/20—Sludge processing
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Treatment Of Sludge (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、有機性汚泥の消化
方法、特に難生物分解性の生物汚泥を含む有機性汚泥の
生物消化方法に関する。The present invention relates to a method for digesting organic sludge, and more particularly to a method for digesting organic sludge including biodegradable biosludge.
【０００２】[0002]
【従来の技術】有機性排水の好気性処理または嫌気性処
理により発生する生物汚泥は、生物処理を経ているため
生物学的に安定であって難生物分解性であり，その処理
は困難である。このような生物汚泥を含む有機性汚泥の
消化方法として、メタン発酵などの嫌気性消化を行う方
法があり、通常汚泥の分解率は４０％程度である。汚泥
の分解率を向上させる目的で、オゾン処理、ボールミル
処理、超音波処理、熱処理などの前処理する方法が提案
されているが、これらの前処理を行う方法でも汚泥の分
解率は５０〜６０％程度が限界であり、またコストが高
いという問題点がある。前処理する方法以外の方法とし
て、嫌気性消化した汚泥を濃縮し、この濃縮汚泥を嫌気
性消化槽に返送し、嫌気性消化槽内の汚泥濃度を増加さ
せる方法も提案されている。しかし、この方法において
も汚泥の分解率は６０％程度が限界である。2. Description of the Related Art Biological sludge generated by aerobic or anaerobic treatment of organic wastewater is biologically stable because of undergoing biological treatment, is difficult to biodegrade, and its treatment is difficult. . As a method of digesting organic sludge including such biological sludge, there is a method of performing anaerobic digestion such as methane fermentation, and the decomposition rate of sludge is usually about 40%. Pretreatment methods such as ozone treatment, ball mill treatment, ultrasonic treatment, and heat treatment have been proposed for the purpose of improving the sludge decomposition rate. However, even with these pretreatment methods, the sludge decomposition rate is 50 to 60. % Is the limit and the cost is high. As a method other than the pretreatment method, there has been proposed a method of concentrating anaerobic digested sludge, returning the concentrated sludge to the anaerobic digestion tank, and increasing the sludge concentration in the anaerobic digestion tank. However, even in this method, the limit of the sludge decomposition rate is about 60%.
【０００３】さらに別の方法として、特開平９−１３６
１００号には、嫌気性消化汚泥をオゾン処理し、このオ
ゾン処理汚泥を好気性消化する方法が記載され、原汚泥
重量の９０％以上が減量化されることが記載されてい
る。しかし上記従来の方法では、嫌気性消化汚泥に含ま
れる多量の硫化水素によりオゾンが多量に消費されるた
め、コストが高いという問題点がある。As another method, Japanese Patent Application Laid-Open No. 9-136
No. 100 describes a method of subjecting anaerobic digested sludge to ozone treatment and aerobically digesting the ozone treated sludge, and describes that 90% or more of the weight of raw sludge is reduced. However, in the above-mentioned conventional method, a large amount of ozone is consumed by a large amount of hydrogen sulfide contained in the anaerobic digested sludge, so that there is a problem that the cost is high.
【０００４】[0004]
【発明が解決しようとする課題】本発明の課題は、生物
汚泥を含む有機性汚泥を低コストで、しかも高分解率で
消化することができる有機性汚泥の消化方法を提案する
ことである。An object of the present invention is to propose a method for digesting organic sludge which can digest organic sludge including biological sludge at a low cost and at a high decomposition rate.
【０００５】[0005]
【課題を解決するための手段】本発明は、浸漬型膜分離
装置を備えた好気性消化槽に生物汚泥を含む有機性汚泥
を導入し、好気的に生物処理する好気性消化工程と、好
気性消化工程で生物処理した好気性消化汚泥をオゾン処
理するオゾン処理工程と、オゾン処理工程でオゾン処理
したオゾン処理汚泥を嫌気性消化槽において嫌気的に生
物処理する嫌気性消化工程と、嫌気性消化工程で生物処
理した嫌気性消化汚泥を濃縮汚泥と分離液とに固液分離
する固液分離工程と、固液分離工程で分離した濃縮汚泥
の一部を好気性消化槽に返送し、残部を嫌気性消化槽に
返送する返送工程とを含む有機性汚泥の消化方法であ
る。According to the present invention, there is provided an aerobic digestion step in which an organic sludge containing biological sludge is introduced into an aerobic digestion tank equipped with a submerged membrane separation device and biologically treated in an aerobic manner. An ozone treatment step of ozone-treating aerobic digestion sludge biologically treated in the aerobic digestion step; an anaerobic digestion step of anaerobic biological treatment of ozone-treated sludge ozone-treated in the ozone treatment step in an anaerobic digestion tank; A solid-liquid separation step of solid-liquid separation of the anaerobic digestion sludge biologically treated in the anaerobic digestion step into a concentrated sludge and a separated liquid, and a part of the concentrated sludge separated in the solid-liquid separation step is returned to the aerobic digestion tank, And a return step of returning the remainder to an anaerobic digestion tank.
【０００６】本発明において処理の対象となる有機性汚
泥は生物汚泥を含む有機性汚泥であり、生物汚泥を主要
成分として含む汚泥が好ましく、生物汚泥のほかに他の
有機物および／または無機物を含んでいてもよい。生物
汚泥としては下水、し尿、産業排水等の有機性排水の生
物処理によって生成する汚泥があげられ、活性汚泥、消
化汚泥などがこれに含まれる。有機性汚泥はこのような
生物汚泥を含む汚泥であり、生物汚泥のほかに下水等の
沈澱汚泥などの他の有機または無機物を含む汚泥との混
合汚泥でもよい。このような汚泥には水処理等によって
発生するスラリー状の汚泥のほかに、これを脱水処理し
た脱水ケーキも含まれる。The organic sludge to be treated in the present invention is an organic sludge containing biological sludge, and is preferably a sludge containing biological sludge as a main component, and contains other organic substances and / or inorganic substances in addition to biological sludge. You may go out. Examples of biological sludge include sludge generated by biological treatment of organic wastewater such as sewage, human waste, and industrial wastewater, and include activated sludge and digested sludge. Organic sludge is sludge containing such biological sludge, and may be mixed sludge with sludge containing other organic or inorganic substances, such as sedimentation sludge such as sewage, in addition to biological sludge. Such sludge includes not only slurry sludge generated by water treatment or the like, but also dewatered cake obtained by dewatering the sludge.
【０００７】本発明の好気性消化工程は生物汚泥を含む
有機性汚泥および後段の返送工程から返送される濃縮汚
泥を好気性消化槽に導入して槽内の生物汚泥と混合し、
曝気して好気的に生物処理する工程である。曝気方法と
しては、通常の空気による曝気法、酸素富化空気よる曝
気法などが採用できる。In the aerobic digestion step of the present invention, the organic sludge containing biological sludge and the concentrated sludge returned from the subsequent return step are introduced into an aerobic digestion tank and mixed with the biological sludge in the tank.
This is a process for aerobically biologically treating by aeration. As the aeration method, an aeration method using ordinary air, an aeration method using oxygen-enriched air, or the like can be employed.
【０００８】好気性消化工程では、微生物細胞内の蓄積
有機物、汚泥粘物質などが生物的に消化され、汚泥の可
溶化、減量化が促進される。この反応は滞留時間が長い
ほどよいが、あまり長すぎると後段の嫌気性消化工程で
のメタンガスの発生量が減少し、資源の回収率が低下す
るので、好気性消化工程の滞留時間は通常１時間以上、
好ましくは６〜４８時間とするのが望ましい。[0008] In the aerobic digestion step, accumulated organic matter and sludge slime in the microbial cells are biologically digested, and the solubilization and weight reduction of the sludge are promoted. The longer the residence time of this reaction, the better. However, if it is too long, the amount of methane gas generated in the subsequent anaerobic digestion step decreases, and the recovery rate of resources decreases. More than an hour,
Preferably, it is 6 to 48 hours.
【０００９】有機性汚泥は、通常運搬や貯留中に腐敗し
ている場合が多く、このため硫化水素が含まれており、
また嫌気性消化汚泥にも多量の硫化水素が含まれてい
る。本発明では硫化水素を含むこれらの汚泥を好気性消
化工程において好気的に処理することにより、汚泥中の
硫化水素は生物的に硫酸に酸化される。硫化水素の酸化
のために必要な滞留時間は通常１時間程度である。また
好気性消化により、溶解性の生分解可能な有機物のほと
んどが分解される。Organic sludge often rots during transportation and storage, and therefore contains hydrogen sulfide.
Anaerobic digested sludge also contains a large amount of hydrogen sulfide. In the present invention, hydrogen sulfide in sludge is biologically oxidized to sulfuric acid by aerobically treating these sludges containing hydrogen sulfide in the aerobic digestion step. The residence time required for the oxidation of hydrogen sulfide is usually about one hour. Aerobic digestion also breaks down most of the soluble, biodegradable organic matter.
【００１０】好気性消化槽には浸漬型膜分離装置が浸漬
配置される。この浸漬型膜分離装置は分離膜を有し、こ
の膜が槽内液に浸漬された状態で槽内液から水を濾過し
て汚泥と分離する装置である。この浸漬型膜分離装置は
好気性消化槽内に設けられた散気装置により引き起こさ
れる曝気による水流を分離膜面に当てることにより、膜
面への懸濁物質の濃縮を防止しながら濾過を行うように
構成されているのが好ましい。濾過はポンプ等の吸引手
段などにより行うことができる。浸漬型膜分離装置で分
離された水は処理水として系外へ排出される。好気性消
化槽にはバッフル板等の隔壁を設けることができる。In the aerobic digestion tank, an immersion type membrane separation device is immersed. The immersion type membrane separation device has a separation membrane, and in a state where the membrane is immersed in the liquid in the tank, water is filtered from the liquid in the tank and separated from sludge. This immersion type membrane separation device performs filtration while preventing concentration of suspended substances on the membrane surface by applying a water flow due to aeration caused by a diffuser provided in the aerobic digestion tank to the separation membrane surface. It is preferable that it is comprised as follows. Filtration can be performed by a suction means such as a pump. The water separated by the immersion type membrane separation device is discharged out of the system as treated water. The aerobic digestion tank may be provided with a partition such as a baffle plate.
【００１１】膜分離装置の膜の種類としては、限外濾過
（ＵＦ）膜、精密濾過（ＭＦ）膜などが使用できる。膜
の材質としては酢酸セルロース（ＣＡ）膜、ポリアミド
（ＰＡ）膜、アラミド膜、ポリスルホン膜、親水性ポリ
エチレンなど任意の材質の膜が使用できる。また膜の形
状としては平膜、スパイラル状膜、チューブラー膜、中
空糸膜など任意の形状のものが使用できる。As the type of the membrane of the membrane separation device, an ultrafiltration (UF) membrane, a microfiltration (MF) membrane or the like can be used. As a material of the membrane, a membrane of any material such as a cellulose acetate (CA) membrane, a polyamide (PA) membrane, an aramid membrane, a polysulfone membrane, and a hydrophilic polyethylene can be used. The membrane may have any shape such as a flat membrane, a spiral membrane, a tubular membrane, and a hollow fiber membrane.
【００１２】オゾン処理工程は、好気性消化工程で処理
した好気性消化汚泥をオゾンと接触させてオゾン処理す
る工程である。通常好気性消化槽の槽内液をそのままオ
ゾン処理槽に導入してオゾンと接触させることができ
る。接触方法としては、オゾン処理槽に好気性消化汚泥
を導入してオゾンを吹き込む方法、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。オゾン処理により汚泥は易生物分解
性の有機物に改質される。The ozone treatment step is a step in which the aerobic digested sludge treated in the aerobic digestion step is brought into contact with ozone to perform ozone treatment. Usually, the solution in the tank of the aerobic digestion tank can be directly introduced into the ozone treatment tank and brought into contact with ozone. As a contact method, a method of introducing aerobic digested sludge into an ozone treatment tank and blowing ozone, a method of mechanical stirring, a method of using a packed bed, and the like can be adopted. As ozone, other than ozone gas, ozone-containing air, ozonized air and the like can be used. Sludge is reformed into easily biodegradable organic matter by ozone treatment.
【００１３】オゾン処理の条件は特に限定されないが、
オゾン使用量を０．００２〜０．０５ｇ−Ｏ3／ｇ−Ｖ
ＳＳ、好ましくは０．００５〜０．０３ｇ−Ｏ3／ｇ−
ＶＳＳとして処理を行うのが望ましい。またｐＨが５以
下であるのが好ましい。The conditions of the ozone treatment are not particularly limited,
The ozone amount used 0.002~0.05g-O 3 / g-V
SS, preferably 0.005~0.03g-O 3 / g-
It is desirable to perform the processing as VSS. Further, the pH is preferably 5 or less.
【００１４】本発明では、オゾン処理の対象となる好気
性消化汚泥中には硫化水素および溶解性の有機物がほと
んど含まれていないので、このような好気性消化汚泥を
オゾン処理しても硫化水素の酸化などにオゾンが無駄に
消費されるということはない。また好気性消化汚泥は浸
漬型膜分離装置により濾過されて水が除かれているの
で、処理する量が少なくなっている。従って、少ないオ
ゾン量で低コストで効率よくオゾン処理することができ
る。In the present invention, since aerobic digested sludge to be subjected to ozone treatment contains almost no hydrogen sulfide and soluble organic substances, even if such aerobic digested sludge is treated with ozone, hydrogen sulfide can be obtained. There is no waste of ozone due to oxidation of the ozone. Further, since the aerobic digested sludge is filtered by a submerged membrane separation device to remove water, the amount to be treated is reduced. Therefore, ozone treatment can be efficiently performed at low cost with a small amount of ozone.
【００１５】嫌気性消化工程はオゾン処理工程でオゾン
処理したオゾン処理汚泥を嫌気性消化槽において嫌気的
に生物処理する工程である。嫌気性消化工程では、オゾ
ン処理汚泥中の易生物分解性有機物およびその他の有機
物が有機酸生成およびメタン生成の段階を経て分解さ
れ、メタンに変換される。嫌気性消化は有機酸生成とメ
タン生成を別々の反応槽で行う二相方式で行うこともで
きるし、１つの反応槽で行う一相方式で行うこともでき
る。The anaerobic digestion step is a step of anaerobically biologically treating the ozone-treated sludge that has been ozone-treated in the ozone treatment step in an anaerobic digestion tank. In the anaerobic digestion process, biodegradable organic substances and other organic substances in the ozonized sludge are decomposed through organic acid generation and methanation, and are converted to methane. Anaerobic digestion can be carried out in a two-phase system in which organic acid production and methane production are carried out in separate reactors, or in a one-phase system in one reactor.
【００１６】嫌気性消化としては、通常の嫌気性消化法
に用いられる浮遊法が一般に採用できるが、固定床法、
流動床法、ＵＡＳＢ法などの高負荷嫌気性生物処理など
を採用することもできる。嫌気性消化の処理条件は特に
制限されず、通常の嫌気処理の条件が採用できる。例え
ば、温度は３０〜６０℃とすることができる。３０〜４
０℃では中温性のメタン発酵菌が作用し、４５℃〜６０
℃では高温性のメタン発酵菌が作用する。滞留時間は５
〜３０日、好ましくは１０〜２０日、ｐＨは６〜８．
５、好ましくは７〜８とするのが望ましい。As the anaerobic digestion, a suspension method used in a usual anaerobic digestion method can be generally adopted.
High-load anaerobic biological treatment such as a fluidized bed method and a UASB method can also be adopted. The processing conditions for anaerobic digestion are not particularly limited, and ordinary anaerobic processing conditions can be employed. For example, the temperature can be 30-60 ° C. 30-4
At 0 ° C, a mesophilic methane fermentation bacterium acts, and
At ℃, high temperature methane fermentation bacteria act. Residence time is 5
３０30 days, preferably 10-20 days, pH 6-8.
5, preferably 7 to 8.
【００１７】本発明における嫌気性消化では、前記好気
性消化工程において浸漬型膜分離装置により水を濾過し
て分離しているので、嫌気性消化処理する汚泥の容量が
少なくなっている。このため嫌気性消化槽を小さくする
ことができるほか、加温に使用する熱量も少なくなり、
低コストで効率的な処理が可能である。In the anaerobic digestion according to the present invention, since the water is filtered and separated by the immersion type membrane separation device in the aerobic digestion step, the volume of the sludge to be subjected to the anaerobic digestion treatment is reduced. For this reason, the anaerobic digestion tank can be made smaller, and the amount of heat used for heating is reduced,
Low cost and efficient processing is possible.
【００１８】固液分離工程では嫌気性消化汚泥を濃縮汚
泥と分離液とに固液分離を行う。固液分離手段としては
沈殿分離、加圧浮上、遠心分離、ＭＦ膜およびＵＦ膜な
ど、通常の固液分離手段が採用できる。沈殿分離または
加圧浮上などを採用する場合、メタン発酵菌は酸素に弱
いため、空気にできるだけ触れないようにするのが好ま
しい。また遠心分離などを採用する場合、分離液中のＳ
Ｓ濃度を低減するため、高分子凝集剤を併用することが
好ましい。In the solid-liquid separation step, anaerobic digested sludge is subjected to solid-liquid separation into concentrated sludge and a separated liquid. As the solid-liquid separation means, ordinary solid-liquid separation means such as precipitation separation, flotation under pressure, centrifugal separation, MF membrane and UF membrane can be adopted. When sedimentation separation or pressurized flotation is employed, it is preferable that methane fermentation bacteria be exposed to air as much as possible because they are vulnerable to oxygen. When centrifugation or the like is employed, S
In order to reduce the S concentration, it is preferable to use a polymer flocculant in combination.
【００１９】固液分離工程で分離した分離液は処理水と
して系外へ排出し、濃縮汚泥は返送工程として、一部を
好気性消化工程の好気性消化槽に返送し、残部を嫌気性
消化工程の嫌気性消化槽に返送する。また一部を系外へ
引き抜いて脱水などの他の処理を行ってもよい。The separated liquid separated in the solid-liquid separation step is discharged out of the system as treated water, and the concentrated sludge is returned to the aerobic digestion tank in the aerobic digestion step as a return step, and the remaining part is subjected to anaerobic digestion. Return to process anaerobic digestion tank. Further, another process such as dehydration may be performed by pulling a part out of the system.
【００２０】濃縮汚泥の返送の割合は、嫌気性消化槽に
おける汚泥濃度および滞留時間などにより変わるが、好
気性消化槽に返送する量よりも嫌気性消化槽に返送する
量を多くするのが好ましい。例えば、嫌気性消化槽にお
ける汚泥濃度１％、滞留時間２０日の場合、濃縮汚泥の
１０〜３０％程度を好気性消化槽に返送し、７０〜９０
％を嫌気性消化槽に返送するのが望ましい。The rate of return of the concentrated sludge depends on the sludge concentration and the residence time in the anaerobic digestion tank, but it is preferable that the amount returned to the anaerobic digestion tank is larger than the amount returned to the aerobic digestion tank. . For example, when the sludge concentration in the anaerobic digestion tank is 1% and the residence time is 20 days, about 10 to 30% of the concentrated sludge is returned to the aerobic digestion tank, and 70 to 90%.
% Is desirably returned to the anaerobic digester.
【００２１】本発明の方法では好気性消化汚泥をオゾン
処理しているので、オゾンが硫化水素の酸化に無駄に消
費されることはなく、このためオゾンの使用量を少なく
して低コストで処理することができる。また本発明の方
法では浸漬型膜分離装置により水を好気性消化槽から引
き抜いているので、硫黄化合物が硫酸イオンの形で処理
水として好気性消化槽から引き抜かれる。これに対し
て、好気性消化槽から処理水を引き抜かない場合は、硫
黄化合物は再び嫌気性消化槽へ流入してＳ2-となり、鉄
などの金属イオンと不溶性塩を形成して系内に蓄積して
しまう。従って、好気性消化槽から浸漬型膜分離装置に
より水を引き抜くことにより、汚泥を高分解率で消化す
ることができる。このため、嫌気性消化工程での汚泥の
分解率が９０％以上に向上し、汚泥を完全に消化するこ
とも可能である。In the method of the present invention, the aerobic digested sludge is subjected to ozone treatment, so that ozone is not wastefully consumed in the oxidation of hydrogen sulfide, and therefore, the amount of ozone used is reduced and the treatment is carried out at low cost. can do. Further, in the method of the present invention, since water is extracted from the aerobic digestion tank by the immersion type membrane separation device, the sulfur compound is extracted from the aerobic digestion tank as treated water in the form of sulfate ions. On the other hand, if the treated water is not withdrawn from the aerobic digestion tank, the sulfur compound flows into the anaerobic digestion tank again and becomes S 2− , forming an insoluble salt with metal ions such as iron and entering the system. Accumulate. Therefore, sludge can be digested at a high decomposition rate by extracting water from the aerobic digestion tank with a submerged membrane separation device. For this reason, the decomposition rate of sludge in the anaerobic digestion step is improved to 90% or more, and sludge can be completely digested.
【００２２】[0022]
【発明の効果】以上の通り本発明によれば、生物汚泥を
含む有機性汚泥を好気性消化したのちオゾン処理し、こ
のオゾン処理汚泥を嫌気性消化したのち固液分離し、濃
縮汚泥の一部を好気性消化、残部を嫌気性消化処理に返
送しているので、有機性汚泥を低コストで、かつ高分解
率で消化することができる。As described above, according to the present invention, organic sludge including biological sludge is subjected to aerobic digestion, followed by ozone treatment, and this ozone-treated sludge is subjected to anaerobic digestion, followed by solid-liquid separation to form a concentrated sludge. Since the part is returned to the aerobic digestion and the remaining part is returned to the anaerobic digestion treatment, the organic sludge can be digested at a low cost and at a high decomposition rate.
【００２３】[0023]
【発明の実施の形態】以下、本発明の実施の形態を図面
により説明する。図１は実施形態の有機性汚泥の消化装
置を示す系統図である。図１において、１は好気性消化
槽であり、槽内に浸漬型膜分離装置２が浸漬配置されて
いる。３はオゾン処理槽、４は嫌気性消化槽、５は固液
分離槽である。Embodiments of the present invention will be described below with reference to the drawings. FIG. 1 is a system diagram showing an organic sludge digester of the embodiment. In FIG. 1, reference numeral 1 denotes an aerobic digestion tank in which an immersion type membrane separation device 2 is immersed. 3 is an ozone treatment tank, 4 is an anaerobic digestion tank, and 5 is a solid-liquid separation tank.
【００２４】図１の装置で生物汚泥を含む有機性汚泥を
処理するには、汚泥導入路１１から生物汚泥を含む有機
性汚泥を好気性消化槽１に導入するとともに、返送汚泥
路１２から返送される濃縮汚泥を好気性消化槽１に導入
して槽内の生物汚泥と混合し、酸素供給路１３から供給
される空気を散気装置１４から散気し、好気的に生物処
理する。このようにして汚泥を好気性消化するととも
に、ポンプ１５を駆動し、分離膜１６を透過させて水を
濾過する。濾過水は排水路１７から系外へ排出する。In order to treat organic sludge containing biological sludge with the apparatus shown in FIG. 1, organic sludge containing biological sludge is introduced into the aerobic digestion tank 1 from the sludge introduction passage 11 and returned from the return sludge passage 12. The concentrated sludge to be introduced is introduced into the aerobic digestion tank 1 and mixed with the biological sludge in the tank, and the air supplied from the oxygen supply path 13 is diffused from the air diffuser 14 to aerobically biologically treat. In this way, the sludge is aerobicly digested, and the pump 15 is driven to permeate the separation membrane 16 to filter water. The filtered water is discharged from the drainage channel 17 to the outside of the system.
【００２５】好気性消化槽１の槽内液は好気性消化汚泥
として連絡路２１から取り出し、オゾン処理槽３に導入
する。オゾン処理槽３ではオゾン発生器２２で発生させ
たオゾンをオゾン供給路２３から導入し、連絡路２１か
ら導入される好気性消化汚泥と接触させてオゾン処理す
る。オゾン排ガスはオゾン排ガス路２４から排出する。
オゾン処理汚泥は、連絡路２５から嫌気性消化槽４に導
入する。The liquid in the aerobic digestion tank 1 is taken out of the communication channel 21 as aerobic digestion sludge and introduced into the ozone treatment tank 3. In the ozone treatment tank 3, ozone generated by the ozone generator 22 is introduced from the ozone supply path 23, and is brought into contact with the aerobic digested sludge introduced from the communication path 21 to perform ozone treatment. The ozone exhaust gas is discharged from the ozone exhaust gas passage 24.
The ozone-treated sludge is introduced into the anaerobic digestion tank 4 from the communication channel 25.
【００２６】嫌気性消化槽４では連絡路２５から導入さ
れるオゾン処理汚泥および返送汚泥路２６から返送され
る濃縮汚泥を導入し、槽内の生物汚泥と混合し、嫌気性
を維持して嫌気性消化を行う。嫌気性消化を中温性のメ
タン発酵菌により行う場合は加熱手段（図示せず）によ
り３０〜４０℃に加温し、高温性のメタン発酵菌により
行う場合は４５℃〜６０℃に加温する。生成するメタン
ガスはメタンガス排出路２７から排出する。In the anaerobic digestion tank 4, ozone-treated sludge introduced from the communication line 25 and concentrated sludge returned from the return sludge passage 26 are introduced, mixed with biological sludge in the tank, and maintained in anaerobic condition to be anaerobic. Perform sexual digestion. When anaerobic digestion is performed by a mesophilic methane fermentation bacterium, the mixture is heated to 30 to 40 ° C. by a heating means (not shown). . The generated methane gas is discharged from the methane gas discharge path 27.
【００２７】嫌気性消化汚泥は連絡路２８から固液分離
槽５に導入し、分離汚泥と分離液とに固液分離する。分
離汚泥は濃縮汚泥とし、その一部は返送汚泥路１２から
好気性消化槽１に返送し、残部は返送汚泥路２６から嫌
気性消化槽４に返送する。余剰汚泥が生じる場合は汚泥
排出路２９から排出する。分離液は排水路３０から排出
する。The anaerobic digested sludge is introduced into the solid-liquid separation tank 5 through the communication path 28, and is separated into a separated liquid and a separated liquid. The separated sludge is concentrated sludge, and a part of the sludge is returned to the aerobic digestion tank 1 from the return sludge passage 12, and the remainder is returned to the anaerobic digestion tank 4 from the return sludge passage 26. When excess sludge is generated, the sludge is discharged from the sludge discharge passage 29. The separated liquid is discharged from the drain 30.
【００２８】上記のような処理方法では、有機性汚泥お
よび濃縮汚泥に含まれる硫化水素は好気性消化槽１で酸
化されて硫酸に変換されるので、オゾン処理槽３に硫化
水素が導入されることはなく、このためオゾンが硫化水
素の酸化のために無駄に消費されることはなく、オゾン
の使用量を少なくして低コストでオゾン処理することが
できる。また浸漬型膜分離装置２により水を濾過して好
気性消化槽１から引き抜いているので、硫黄化合物が硫
酸イオンの形で引き抜かれるとともに、嫌気性消化槽４
で処理する汚泥の容量が少なくなっており、このため汚
泥を高分解率で消化することができるとともに、嫌気性
消化槽４を小さくすることができるほか、加温に使用す
る熱量も少なくなり、低コストで効率的な処理が可能で
ある。In the above treatment method, hydrogen sulfide contained in the organic sludge and the concentrated sludge is oxidized in the aerobic digestion tank 1 and converted into sulfuric acid. Therefore, ozone is not wastefully consumed for oxidation of hydrogen sulfide, and ozone treatment can be performed at a low cost by reducing the amount of ozone used. Further, since water is filtered by the immersion type membrane separation device 2 and extracted from the aerobic digestion tank 1, sulfur compounds are extracted in the form of sulfate ions, and the anaerobic digestion tank 4 is removed.
The volume of sludge to be treated in is reduced, so that sludge can be digested with a high decomposition rate, the size of the anaerobic digestion tank 4 can be reduced, and the amount of heat used for heating also decreases, Low cost and efficient processing is possible.
【００２９】図１では嫌気性消化槽４は１つの反応槽で
行っているが、有機酸発酵とメタン発酵とを別々の反応
槽で行うこともできる。In FIG. 1, the anaerobic digestion tank 4 is performed in one reaction tank, but the organic acid fermentation and the methane fermentation can be performed in separate reaction tanks.
【００３０】[0030]
【実施例】比較例１ 下水を処理している活性汚泥法の余剰汚泥と最初沈殿池
汚泥とを１：１で混合した有機性汚泥を濃度１．５％に
調整し、これを被処理汚泥（硫化水素濃度：１２ｍｇ／
Ｌ）とした。この被処理汚泥を０．５Ｌ／ｄａｙの流速
で１ literの好気性消化槽に連続通水した。曝気量は２
Ｌ／ｈｒとした。この好気性消化汚泥（硫化水素濃度：
検出限界以下）０．５ literを容積１ literの洗浄びん
に取り、濃度２５ｇ／ｍ3のオゾン含有ガスを１０ｍＬ
／ｍｉｎの割合で通気した。流入および排出ガス濃度を
測定し、オゾン消費量が５０ｇ／ｋｇ−汚泥となった時
点でオゾン処理を終了した。COMPARATIVE EXAMPLE 1 Organic sludge obtained by mixing excess sludge of the activated sludge method for treating sewage and first settling tank sludge at a ratio of 1: 1 was adjusted to a concentration of 1.5%. (Hydrogen sulfide concentration: 12 mg /
L). The sludge to be treated was continuously passed through a 1 liter aerobic digestion tank at a flow rate of 0.5 L / day. Aeration amount is 2
L / hr. This aerobic digested sludge (hydrogen sulfide concentration:
Take 0.5 liter into a 1 liter washing bottle and 10 mL of ozone-containing gas with a concentration of 25 g / m 3.
/ Min. The inflow and exhaust gas concentrations were measured, and the ozone treatment was terminated when the ozone consumption reached 50 g / kg-sludge.
【００３１】オゾン処理汚泥を取り出し、嫌気性消化槽
に投入した。同量を嫌気性消化槽から引き抜き、これを
嫌気性消化汚泥とした。また、その嫌気性消化汚泥の一
部で汚泥濃度などの分析を行った。嫌気性消化槽は有効
容積７．５ literで、種汚泥として下水嫌気性消化槽の
汚泥を乾燥重量で７５ｇ投入した。この操作を一日一
回、３か月継続した。なおオゾン処理、および嫌気性消
化槽へのオゾン処理汚泥の投入は週に５回とした。The ozone-treated sludge was taken out and put into an anaerobic digestion tank. The same amount was withdrawn from the anaerobic digestion tank, and this was defined as anaerobic digested sludge. In addition, the sludge concentration was analyzed for a part of the anaerobic digested sludge. The anaerobic digester had an effective volume of 7.5 liters, and 75 g of sewage anaerobic digester sludge was introduced as seed sludge by dry weight. This operation was continued once a day for three months. The ozone treatment and the injection of the ozonized sludge into the anaerobic digestion tank were performed five times a week.
【００３２】また嫌気性消化汚泥を１５０００ｒｐｍで
１０分間遠心分離し、上澄みを捨てた。沈殿した汚泥を
３等分し、１／３を好気性消化槽へ戻し、残部を嫌気性
消化槽に戻した。その結果、嫌気性消化槽の汚泥濃度は
当初１５．２ｇ／Ｌであったが、３か月経過後には２
２．２ｇ／Ｌとなり、３か月間で汚泥濃度は約１．５倍
に上昇した。The anaerobic digested sludge was centrifuged at 15000 rpm for 10 minutes, and the supernatant was discarded. The precipitated sludge was divided into three equal parts, one third was returned to the aerobic digestion tank, and the remainder was returned to the anaerobic digestion tank. As a result, the sludge concentration in the anaerobic digester was 15.2 g / L at first, but after 3 months, it was 2 g / L.
It became 2.2 g / L, and the sludge concentration increased about 1.5 times in three months.
【００３３】実施例１ 比較例１と同じ被処理汚泥を０．５Ｌ／ｄａｙの流速で
１ literの好気性消化槽に連続通水した。この好気性消
化槽に三菱レーヨン社製の中空糸浸漬膜を浸漬して、２
５０ｍＬ／ｄａｙの流速で処理水を引き抜いた。曝気量
は５Ｌ／ｈｒとした。好気性消化汚泥は比較例１と同じ
方法でオゾン処理および嫌気性消化を行った。その結
果、嫌気性消化槽の汚泥濃度は当初１５．２ｇ／Ｌ、３
か月経過した後も１６．０ｇ／Ｌであり、大きな上昇は
認められなかった。Example 1 The same sludge to be treated as in Comparative Example 1 was continuously passed through a 1 liter aerobic digestion tank at a flow rate of 0.5 L / day. A hollow fiber immersion membrane manufactured by Mitsubishi Rayon Co., Ltd. was immersed in this aerobic digestion tank,
The treated water was withdrawn at a flow rate of 50 mL / day. The aeration amount was 5 L / hr. The aerobic digested sludge was subjected to ozone treatment and anaerobic digestion in the same manner as in Comparative Example 1. As a result, the sludge concentration in the anaerobic digestion tank was initially 15.2 g / L, 3
Even after a lapse of months, the weight was still 16.0 g / L, and no large increase was observed.
【図１】実施形態の有機性汚泥の消化装置を示す系統図
である。FIG. 1 is a system diagram showing an organic sludge digester according to an embodiment.
１ 好気性消化槽 ２ 浸漬型膜分離装置 ３ オゾン処理槽 ４ 嫌気性消化槽 ５ 固液分離槽 １１ 汚泥導入路 １２、２６ 返送汚泥路 １３ 酸素供給路 １４ 散気装置 １５ ポンプ １６ 分離膜 １７、３０ 排水路 ２１、２５、２８ 連絡路 ２２ オゾン発生器 ２３ オゾン供給路 ２４ オゾン排ガス路 ２７ メタンガス排出路 ２９ 汚泥排出路 Reference Signs List 1 aerobic digestion tank 2 immersion type membrane separation device 3 ozone treatment tank 4 anaerobic digestion tank 5 solid-liquid separation tank 11 sludge introduction path 12, 26 return sludge path 13 oxygen supply path 14 air diffuser 15 pump 16 separation membrane 17, Reference Signs List 30 drainage channel 21, 25, 28 communication channel 22 ozone generator 23 ozone supply channel 24 ozone exhaust gas channel 27 methane gas discharge channel 29 sludge discharge channel
───────────────────────────────────────────────────── フロントページの続き Ｆターム(参考） 4D006 GA06 GA07 HA01 HA21 HA41 HA61 HA93 KA31 KA44 KB22 KE08P MA01 MA02 MA03 MC18 MC22 MC54 MC62 PA01 PA02 PB08 PB28 PC64 4D059 AA04 AA05 AA23 BA03 BA13 BC02 BE31 BE37 BE41 BE42 DA33 DA34 DA43 ──────────────────────────────────────────────────続 き Continued on the front page F term (reference) 4D006 GA06 GA07 HA01 HA21 HA41 HA61 HA93 KA31 KA44 KB22 KE08P MA01 MA02 MA03 MC18 MC22 MC54 MC62 PA01 PA02 PB08 PB28 PC64 4D059 AA04 AA05 AA23 BA03 BA13 BC02 BE31 DA37 DA33 DA33
Claims (1)
に生物汚泥を含む有機性汚泥を導入し、好気的に生物処
理する好気性消化工程と、 好気性消化工程で生物処理した好気性消化汚泥をオゾン
処理するオゾン処理工程と、 オゾン処理工程でオゾン処理したオゾン処理汚泥を嫌気
性消化槽において嫌気的に生物処理する嫌気性消化工程
と、 嫌気性消化工程で生物処理した嫌気性消化汚泥を濃縮汚
泥と分離液とに固液分離する固液分離工程と、 固液分離工程で分離した濃縮汚泥の一部を好気性消化槽
に返送し、残部を嫌気性消化槽に返送する返送工程とを
含む有機性汚泥の消化方法。1. An aerobic digestion step in which organic sludge including biological sludge is introduced into an aerobic digestion tank equipped with a submerged membrane separation device, and a biological treatment is performed in an aerobic digestion step. An ozone treatment step for ozonizing aerobic digestion sludge, an anaerobic digestion step for anaerobically biologically treating ozone-treated sludge ozone-treated in the ozone treatment step in an anaerobic digestion tank, and an anaerobic biological treatment in the anaerobic digestion step -Liquid separation process for solid-liquid separation of anaerobic digestion sludge into concentrated sludge and a separated liquid; part of the concentrated sludge separated in the solid-liquid separation process is returned to the aerobic digestion tank, and the remainder is returned to the anaerobic digestion tank A method for digesting organic sludge, comprising:
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000157993A JP3636035B2 (en) | 2000-05-24 | 2000-05-24 | Digestion method of organic sludge |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005279551A (en) * | 2004-03-30 | 2005-10-13 | Kurita Water Ind Ltd | Biological treatment method for organic waste water |
| CN1296292C (en) * | 2003-01-09 | 2007-01-24 | 可乐丽股份有限公司 | Waste water treatment method |
| JP2007098229A (en) * | 2005-09-30 | 2007-04-19 | Kurita Water Ind Ltd | Method and apparatus for treating organic waste material |
| 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 |
| JP2009255074A (en) * | 2008-04-11 | 2009-11-05 | Hanbat National Univ Industry-Academic Cooperation Foundation | Anaerobic integration process apparatus for organic waste treatment |
| CN103803770A (en) * | 2014-02-26 | 2014-05-21 | 江苏理工学院 | Organic sludge high-temperature microaerobic-anaerobic digestion device and method |
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| KR101367765B1 (en) * | 2012-05-21 | 2014-02-27 | 서울과학기술대학교 산학협력단 | Sludge treatment installation using hydrodynamic cavitation |
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2000
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|---|---|---|---|---|
| CN1296292C (en) * | 2003-01-09 | 2007-01-24 | 可乐丽股份有限公司 | Waste water treatment method |
| JP4501496B2 (en) * | 2004-03-30 | 2010-07-14 | 栗田工業株式会社 | Biological treatment method for organic wastewater |
| JP2005279551A (en) * | 2004-03-30 | 2005-10-13 | Kurita Water Ind Ltd | Biological treatment method for organic waste water |
| JP2007098229A (en) * | 2005-09-30 | 2007-04-19 | Kurita Water Ind Ltd | Method and apparatus for treating organic waste material |
| JP4665693B2 (en) * | 2005-09-30 | 2011-04-06 | 栗田工業株式会社 | Method and apparatus for treating organic waste |
| 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 |
| JP2009255074A (en) * | 2008-04-11 | 2009-11-05 | Hanbat National Univ Industry-Academic Cooperation Foundation | Anaerobic integration process apparatus for organic waste treatment |
| CN103803770A (en) * | 2014-02-26 | 2014-05-21 | 江苏理工学院 | Organic sludge high-temperature microaerobic-anaerobic digestion device and method |
| WO2021075148A1 (en) * | 2019-10-18 | 2021-04-22 | ユニ・チャーム株式会社 | Production method for biogas using used sanitary articles |
| JP2021065816A (en) * | 2019-10-18 | 2021-04-30 | ユニ・チャーム株式会社 | Manufacturing method of biogas using used sanitary articles |
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| JP7379076B2 (en) | 2019-10-18 | 2023-11-14 | ユニ・チャーム株式会社 | Method for producing biogas using used sanitary products |
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