JP2003225697A - Anaerobic fermentation system of organic waste - Google Patents
Anaerobic fermentation system of organic wasteInfo
- Publication number
- JP2003225697A JP2003225697A JP2002025332A JP2002025332A JP2003225697A JP 2003225697 A JP2003225697 A JP 2003225697A JP 2002025332 A JP2002025332 A JP 2002025332A JP 2002025332 A JP2002025332 A JP 2002025332A JP 2003225697 A JP2003225697 A JP 2003225697A
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- ammonia
- methane
- acid
- anaerobic fermentation
- 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
Landscapes
- Processing Of Solid Wastes (AREA)
- Degasification And Air Bubble Elimination (AREA)
- Treatment Of Sludge (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、アルカリ処理を利
用した有機性廃棄物の嫌気性発酵システムの改良に関す
るものである。TECHNICAL FIELD The present invention relates to an improvement in an anaerobic fermentation system for organic waste utilizing alkali treatment.
【０００２】[0002]
【従来の技術】下水処理場などから発生する有機性汚泥
など有機廃棄物の処理方法として、嫌気性発酵処理法が
知られている。この方法は、有機廃棄物を嫌気性消化槽
で酸発酵およびメタン発酵させることにより有機物を分
解すると同時に、有価資源であるメタンガスを回収する
ことができる利点がある。2. Description of the Related Art An anaerobic fermentation treatment method is known as a method for treating organic waste such as organic sludge generated from a sewage treatment plant. This method has an advantage that organic matter is decomposed by acid fermentation and methane fermentation of an organic waste in an anaerobic digestion tank, and at the same time, methane gas which is a valuable resource can be recovered.
【０００３】本出願人は、この嫌気性発酵処理の前段に
おいて、アルカリ処理を行い、有機廃棄物中の有機物の
可溶化を促進して嫌気性消化処理能力を向上させる方法
を先に開発し、既に特許登録第２１３６８２６号、第２
６５９８９５号を取得済みである。また、これらの処理
方法において、処理すべき有機性汚泥の濃度が高くなり
過ぎると引き起こされるアンモニア阻害による嫌気性消
化効率低下を解消するための手段を特願２０００−３７
５７２２号「有機性汚泥の消化処理方法及び装置」とし
て提案している。The applicant of the present invention first developed a method for improving the anaerobic digestion treatment capacity by performing alkali treatment before the anaerobic fermentation treatment to promote the solubilization of the organic matter in the organic waste, Already registered patents 213626826, 2nd
We have obtained No. 598895. In addition, in these treatment methods, Japanese Patent Application No. 2000-37 discloses a means for eliminating a decrease in anaerobic digestion efficiency due to ammonia inhibition caused when the concentration of organic sludge to be treated becomes too high.
No. 5722, "Method and apparatus for digesting and treating organic sludge".
【０００４】この方法は、図６に例示するように、有機
性汚泥など廃棄物をアルカリ処理槽１１でアルカリ処理
した後、発生したアンモニアをアンモニア除去装置１２
で除去してから消化槽１３で嫌気性消化処理するもので
あり、かくして消化処理に及ぼすアンモニアの悪影響を
排除しようとする方法である。In this method, as shown in FIG. 6, after wastes such as organic sludge are alkali-treated in an alkali treatment tank 11, ammonia generated is removed by an ammonia removing device 12.
This is a method in which the anaerobic digestion treatment is carried out in the digestion tank 13 after the removal by the method described above, and thus the adverse effect of ammonia on the digestion treatment is eliminated.
【０００５】この場合、アルカリ処理汚泥スラリからア
ンモニアを分離、除去するには、前記スラリから遊離し
たアンモニアガスあるいはアンモニア態窒素（以下、単
にアンモニアという）を嫌気性ガス（窒素ガスなど）で
パージして取り出す、吸引ブロワで吸引して取り出す、
あるいは前記スラリの流路に沿って嫌気性ガスを吹き込
んで気液接触させて、アンモニアを嫌気性ガス側に放散
分離するなど、同出願発明に開示した方法が用いられ
る。In this case, in order to separate and remove ammonia from the alkali-treated sludge slurry, the ammonia gas or ammonia nitrogen liberated from the slurry (hereinafter simply referred to as ammonia) is purged with an anaerobic gas (nitrogen gas etc.). , Take out with a suction blower,
Alternatively, the method disclosed in the invention of the same application is used, for example, in which anaerobic gas is blown along the flow path of the slurry to make gas-liquid contact, and ammonia is diffused and separated to the anaerobic gas side.
【０００６】[0006]
【発明が解決しようとする課題】本発明は、上記した有
機廃棄物の嫌気性発酵システムにおける、処理可能な有
機物濃度を高めようとする研究に基づいてなされたもの
であり、嫌気性発酵処理とアルカリ処理との組合せにお
ける発生アンモニアを可能な限り反応系から除去して、
処理有機物の濃度を高めることを可能とする有機性廃棄
物の嫌気性発酵システムを提供する。DISCLOSURE OF THE INVENTION The present invention has been made on the basis of research for increasing the concentration of treatable organic substances in the above-mentioned anaerobic fermentation system for organic wastes. As much ammonia as possible generated in combination with alkali treatment is removed from the reaction system,
Provided is an anaerobic fermentation system for organic waste, which makes it possible to increase the concentration of treated organic matter.
【０００７】[0007]
【課題を解決するための手段】（第１発明）上記の問題
は、第１発明であるところの、有機廃棄物を消化槽にお
いて嫌気性消化し、消化ガスを取り出すとともに、排出
した消化汚泥を次工程に送るようにした嫌気性発酵シス
テムであって、その消化汚泥の一部をアルカリ処理工
程、次いでアンモニア除去工程の各工程で処理した後、
当該消化槽に返送して循環させることを特徴とする、本
発明の有機廃棄物の嫌気性発酵システムによって、解決
することができる。[Means for Solving the Problems] (First Invention) The above-mentioned problem is the first invention, in which organic waste is anaerobically digested in a digestion tank, digested gas is taken out, and discharged digested sludge is removed. An anaerobic fermentation system to be sent to the next step, after treating a part of the digested sludge in the alkali treatment step and then in the ammonia removal step,
This can be solved by the anaerobic fermentation system for organic waste of the present invention, which is characterized in that the organic waste is returned to the digestion tank and circulated.
【０００８】（第２発明）また上記の問題は、第２発明
であるところの、有機廃棄物を酸発酵槽において酸発酵
し、排出した酸発酵汚泥を次工程に送るようにした嫌気
性発酵システムであって、その酸発酵汚泥の一部をアル
カリ処理工程、次いでアンモニア除去工程の各工程で処
理した後、当該酸発酵槽に返送して循環させることを特
徴とする、本発明の有機廃棄物の嫌気性発醗酵システム
によって解決され得る。(Second invention) The above problem is the anaerobic fermentation according to the second invention in which the organic waste is acid-fermented in an acid fermentation tank and the discharged acid-fermented sludge is sent to the next step. The organic waste of the present invention, which is a system, wherein a part of the acid fermentation sludge is treated in each step of an alkali treatment step and then an ammonia removal step, and then returned to the acid fermentation tank for circulation. Can be solved by an anaerobic fermentation system of things.
【０００９】この第２発明は、前記酸発酵汚泥を次工程
のメタン発酵工程でメタン発酵させ消化ガスを取り出す
ようにした形態の有機廃棄物の嫌気性発酵システムとし
て具体化でき、さらに、アンモニア除去したアルカリ処
理汚泥スラリに、前記消化ガス中の炭酸ガスを吸収、移
行させる炭酸ガス吸収工程を付加した形態の有機廃棄物
の嫌気性発酵システムといして、好ましく具体化され
る。The second invention can be embodied as an anaerobic fermentation system of organic waste in a form in which the acid fermentation sludge is methane-fermented in the next methane fermentation step to take out digested gas, and further, ammonia removal It is preferably embodied as an anaerobic fermentation system for organic waste in a form in which a carbon dioxide absorption step of absorbing and transferring carbon dioxide in the digestion gas is added to the alkali-treated sludge slurry.
【００１０】（第３発明）また、上記の問題は、第３発
明であるところの、有機廃棄物を酸発酵槽において酸発
酵させ、次いでメタン発酵槽でメタン発酵させ、消化ガ
スを取り出すとともに、排出したメタン発酵汚泥を次工
程に送るようにした嫌気性発酵システムであって、その
メタン発酵汚泥の一部をアルカリ処理工程、次いでアン
モニア除去工程の各工程で処理した後、前記メタン発酵
槽に返送して循環させることを特徴とする、本発明の有
機廃棄物の嫌気性発酵システムによって解決することが
できる。この第３発明は、アンモニアを除去したアルカ
リ処理汚泥スラリに、前記消化ガス中の炭酸ガスを吸
収、移行させる炭酸ガス吸収工程を付加した形態に具体
化するのが好ましい。(Third invention) Further, the above-mentioned problem is that, in the third invention, the organic waste is acid-fermented in the acid fermentation tank and then methane-fermented in the methane fermentation tank to remove the digested gas, An anaerobic fermentation system in which discharged methane fermentation sludge is sent to the next step, a part of the methane fermentation sludge is treated in each step of an alkali treatment step and then an ammonia removal step, and then in the methane fermentation tank. It can be solved by the anaerobic fermentation system for organic waste of the present invention, which is characterized by returning and circulating. This third invention is preferably embodied in a form in which a carbon dioxide absorption step of absorbing and transferring carbon dioxide in the digestion gas is added to the alkali-treated sludge slurry from which ammonia has been removed.
【００１１】（第４発明）さらに、上記の問題は、第４
発明であるところの、有機廃棄物を酸発酵槽において酸
発酵させ、次いでメタン発酵させ、消化ガスを取り出す
とともに、排出したメタン発酵汚泥を次工程に送るよう
にした嫌気性発酵システムであって、そのメタン発酵汚
泥の一部をアルカリ処理工程、次いでアンモニア除去工
程の各工程で処理した後、当該酸発酵槽に返送して循環
させることを特徴とする、本発明の有機廃棄物の嫌気性
発酵システムによって解決できる。そして、この発明
は、アンモニアを除去したアルカリ処理汚泥スラリに、
前記消化ガス中の炭酸ガスを吸収、移行させる炭酸ガス
吸収工程を付加した形態に好ましく具体化される。(Fourth Invention) Further, the above-mentioned problem is caused by the fourth problem.
The invention is an anaerobic fermentation system in which the organic waste is acid-fermented in an acid fermenter, then methane-fermented, and the digested gas is taken out, and the discharged methane-fermented sludge is sent to the next step, Anaerobic fermentation of the organic waste of the present invention, characterized in that a part of the methane fermentation sludge is treated in each step of an alkali treatment step and then an ammonia removal step, and then returned to the acid fermentation tank for circulation. Can be solved by the system. And, this invention is an alkali-treated sludge slurry from which ammonia has been removed,
It is preferably embodied in a form to which a carbon dioxide absorption step of absorbing and transferring carbon dioxide in the digestive gas is added.
【００１２】以上の本発明によれば、いずれも嫌気性酸
発酵、メタン発酵の少なくとも一方に発酵処理汚泥をア
ルカリ処理し、アンモニア除去する循環工程を付加した
ので、アルカリ処理工程で発生するアンモニアのみなら
ず、前記酸発酵あるいはメタン発酵で発生するアンモニ
アについても、アンモニア除去工程で除去することがで
きるので、アンモニア性窒素による嫌気性発酵に対する
障害が緩和される結果、処理有機物の高濃度化が可能と
なるのである。According to the present invention as described above, since at least one of anaerobic acid fermentation and methane fermentation is added with a circulation step of subjecting the fermented sludge to alkali treatment and removing ammonia, only ammonia generated in the alkali treatment step is added. Not only that, ammonia generated in the acid fermentation or methane fermentation can also be removed in the ammonia removal step, so that the obstacle to anaerobic fermentation due to ammonia nitrogen can be mitigated, and the concentration of treated organic matter can be increased. It becomes.
【００１３】また、本発明では、アンモニア除去工程後
に炭酸ガス吸収工程を設けた形態では、消化ガス中の炭
酸ガスが除去されるので、ガス中のメタンが濃縮された
状態で取り出される。さらに、炭酸ガスを吸収したアル
カリ処理汚泥スラリは嫌気性発酵工程に返送され、水素
資化メタン生成菌の働きによりメタンに変換されるの
で、メタンの収量が増加するという利点がある。Further, in the present invention, in the mode in which the carbon dioxide absorption step is provided after the ammonia removal step, the carbon dioxide gas in the digestion gas is removed, so that the methane in the gas is taken out in a concentrated state. Furthermore, since the alkali-treated sludge slurry that has absorbed carbon dioxide is returned to the anaerobic fermentation process and converted into methane by the action of the hydrogen-utilizing methanogen, there is an advantage that the yield of methane increases.
【００１４】[0014]
【発明の実施の形態】次に、本発明の有機廃棄物の嫌気
性発酵システムに係る実施形態について、図１〜５を参
照しながら説明する。
（第１発明）先ず、本発明の第１発明は、図１に例示す
るフローで示される。処理対象の有機廃棄物ａを消化槽
２で嫌気性消化処理し、発生するメタンガスなどは消化
ガスｂとして分離し、また処理後の消化汚泥ｃは、次の
処理工程に送られる嫌気性発酵システムであって、消化
槽２から消化汚泥の一部を取り出して、アルカリ処理槽
３に送り、そこでアルカリ処理により有機分の可溶化を
促進し、次いでアンモニア除去装置４においてアルカリ
処理汚泥中のアンモニアを除去する。そしてアンモニア
を除去したアルカリ処理汚泥は前記消化槽２に返送し循
環させるシステムである。このように、第１発明では、
消化槽２、アルカリ処理槽３、アンモニア除去装置４が
循環経路を形成している点に特徴がある。BEST MODE FOR CARRYING OUT THE INVENTION Next, an embodiment of an anaerobic fermentation system for organic waste of the present invention will be described with reference to FIGS. (First Invention) First, the first invention of the present invention is shown by the flow illustrated in FIG. The organic waste a to be treated is subjected to an anaerobic digestion treatment in the digestion tank 2, the generated methane gas or the like is separated as a digestion gas b, and the digested sludge c after the treatment is sent to the next treatment step in an anaerobic fermentation system. That is, a part of the digested sludge is taken out from the digestion tank 2 and sent to the alkali treatment tank 3, where the solubilization of organic components is promoted by the alkali treatment, and then the ammonia in the alkali-treated sludge is removed by the ammonia removal device 4. Remove. The alkali-treated sludge from which ammonia has been removed is returned to the digestion tank 2 and circulated. Thus, in the first invention,
It is characterized in that the digestion tank 2, the alkali treatment tank 3, and the ammonia removing device 4 form a circulation path.
【００１５】かくして、第１発明によれば、アルカリ処
理によって発生するアンモニア分は勿論、嫌気消化処理
で発生するアンモニア分をもアンモニア除去装置４によ
って繰り返し除去されるので、消化効率が低下しないか
ら、高濃度の有機物を処理できるようになる利点が得ら
れるのである。Thus, according to the first aspect of the present invention, not only the ammonia content generated by the alkali treatment but also the ammonia content generated by the anaerobic digestion treatment is repeatedly removed by the ammonia removing device 4, so that the digestion efficiency does not decrease. The advantage is that high concentrations of organic matter can be treated.
【００１６】なお、ここで、本発明の処理対象の有機廃
棄物ａは、下水処理場から発生する初沈汚泥、余剰汚泥
や、し尿汚泥、生ゴミ、食品工場等から発生する蛋白含
有汚泥などの有機性汚泥が該当する。また、アルカリ処
理槽３、あるいはアンモニア除去装置４としては、前述
したような装置が適宜に採用され得る。The organic waste a to be treated according to the present invention is the first settled sludge generated from a sewage treatment plant, surplus sludge, human waste sludge, raw garbage, protein-containing sludge generated from a food factory, etc. The organic sludge of is applicable. Further, as the alkali treatment tank 3 or the ammonia removing device 4, the device described above can be appropriately adopted.
【００１７】（第２発明）次に、本発明の第２発明は、
図２、３に例示するフローで示される。図２のフロー
は、有機廃棄物ａを酸発酵槽２１において酸発酵し、排
出した酸発酵汚泥ｄを次の処理工程に送るようにした嫌
気性発酵システムであって、その酸発酵槽２１から酸発
酵汚泥ｄの一部を抜き出してアルカリ処理槽３でアルカ
リ処理を行い、次いでアンモニア除去装置４で処理汚泥
中のアンモニアを除去した後、前記酸発酵槽２１に返送
して循環させるシステムである。このように、第２発明
においても、酸発酵槽２１、アルカリ処理槽３、アンモ
ニア除去装置４が循環経路を形成している点に特徴があ
る。(Second Invention) Next, the second invention of the present invention is as follows.
This is shown in the flow illustrated in FIGS. The flow of FIG. 2 shows an anaerobic fermentation system in which the organic waste a is acid-fermented in the acid fermentation tank 21 and the discharged acid fermentation sludge d is sent to the next treatment step. This is a system in which a part of the acid fermentation sludge d is extracted, alkali treatment is performed in the alkali treatment tank 3, ammonia in the treated sludge is removed by the ammonia removal device 4, and then the acid fermentation sludge is returned to the acid fermentation tank 21 for circulation. . Thus, the second aspect of the invention is also characterized in that the acid fermentation tank 21, the alkali treatment tank 3, and the ammonia removing device 4 form a circulation path.
【００１８】この第２発明においても、第１発明に同じ
く、各工程で発生するアンモニア分がアンモニア除去装
置４によって繰り返し除去されるので、消化効率が低下
しないから第１発明同様の効果が得られる利点がある。
ここで、酸発酵汚泥ｄは、次の実施形態のようにメタン
発酵工程で消化される他に、水熱処理による完全分解や
触媒を用いた有機化合物の合成に供せられるのである。Also in this second invention, as in the first invention, the ammonia component generated in each step is repeatedly removed by the ammonia removing device 4, so that the digestion efficiency is not lowered and the same effect as the first invention is obtained. There are advantages.
Here, the acid-fermented sludge d is not only digested in the methane fermentation step as in the following embodiment, but is also used for complete decomposition by hydrothermal treatment and synthesis of an organic compound using a catalyst.
【００１９】（第２発明、第２の実施形態）この第２発
明は、図３に示すように、酸発酵汚泥ｄをメタン発酵槽
２２に送って、メタン発酵させる工程を付加したフロー
のシステムに好ましく具体化できる。この場合、アルカ
リ処理槽３、アンモニア除去装置４、酸発酵槽２１の順
の循環経路中において、アンモニア除去装置４と酸発酵
槽２１との間に、炭酸ガス吸収装置５を付加し、この炭
酸ガス吸収装置５には、前記メタン発酵槽２２で発生す
る消化ガスｂを通過させ、消化ガスｂ中に含まれる炭酸
ガスをアンモニア除去したアルカリ処理汚泥スラリに吸
収、移行させるのが、好適である。(Second Invention, Second Embodiment) As shown in FIG. 3, the second invention is a flow system in which a step of sending acid fermentation sludge d to a methane fermentation tank 22 for methane fermentation is added. Can be embodied preferably. In this case, a carbon dioxide gas absorption device 5 is added between the ammonia removal device 4 and the acid fermentation tank 21 in the circulation path in the order of the alkali treatment tank 3, the ammonia removal device 4, and the acid fermentation tank 21, It is preferable that the digestion gas b generated in the methane fermentation tank 22 is passed through the gas absorption device 5, and the carbon dioxide gas contained in the digestion gas b is absorbed and transferred to the alkali-treated sludge slurry from which ammonia has been removed. .
【００２０】ここで、炭酸ガス吸収装置５では、消化ガ
スとアルカリ処理汚泥スラリとを気液接触させる手段、
例えば、消化ガス中にアルカリ処理汚泥スラリを流下さ
せたり、滴下させる、またはアルカリ処理汚泥スラリ中
に消化ガスを吹き込むなどの手段によって、炭酸ガスは
アルカリと反応して容易に液側に移行させることができ
る。Here, in the carbon dioxide absorption device 5, means for bringing the digestion gas and the alkali-treated sludge slurry into gas-liquid contact,
For example, carbon dioxide reacts with alkali and is easily transferred to the liquid side by means such as flowing down or dropping alkali-treated sludge slurry into digestion gas, or blowing digestion gas into alkali-treated sludge slurry. You can
【００２１】この第２発明の実施形態によれば、アルカ
リ処理槽３、アンモニア除去装置４、酸発酵槽２１の順
の循環経路を設けたことによる消化効率の低下防止に加
えて、消化ガス中から炭酸ガスが除去できるので、メタ
ンガスなど有用なガスを高濃度に取り出せる利点と、除
去吸収した炭酸ガスが嫌気性発酵工程に返送されるの
で、発生する消化ガス量が増大するという利点が併せ得
られる。According to the embodiment of the second aspect of the present invention, in addition to the prevention of deterioration of digestion efficiency by providing the circulation route of the alkaline treatment tank 3, the ammonia removing device 4, and the acid fermentation tank 21 in this order, Since carbon dioxide can be removed from the product, useful gas such as methane can be taken out at a high concentration, and the removed and absorbed carbon dioxide can be returned to the anaerobic fermentation process, increasing the amount of digestive gas generated. To be
【００２２】（第３発明）次に、本発明の第３発明は、
図４に例示するフローで示される。第３発明の有機廃棄
物の嫌気性発酵システムは、有機廃棄物ａを酸発酵槽２
１において酸発酵させ、次いでメタン発酵槽２２に送り
込んでメタン発酵させ、消化ガスｂを取り出すととも
に、排出したメタン発酵汚泥ｅを次工程に送るようにし
た嫌気性発酵システムを基本的フローとしている。(Third Invention) Next, the third invention of the present invention will be described.
This is shown in the flow illustrated in FIG. In the anaerobic fermentation system for organic waste of the third invention, the organic waste a is added to the acid fermentation tank 2
The basic flow is an anaerobic fermentation system in which acid fermentation is performed in 1 and then sent to the methane fermentation tank 22 for methane fermentation to take out the digested gas b, and the discharged methane fermentation sludge e is sent to the next step.
【００２３】そして、第３発明は、そのメタン発酵槽２
２からメタン発酵汚泥ｅの一部を抜き出してアルカリ処
理槽３でアルカリ処理した後、アンモニア除去装置４に
おいて処理物中のアンモニアを分離除去して、前記メタ
ン発酵槽２２に返送して循環させる点に特徴付けられ
る。すなわち、メタン発酵槽２２、アルカリ処理槽３、
アンモニア除去装置４が循環経路を形成している点が要
点である。The third invention is the methane fermentation tank 2
After extracting a part of the methane fermentation sludge e from 2 and alkali-treating it in the alkali treatment tank 3, the ammonia in the treated material is separated and removed in the ammonia removing device 4, and is returned to the methane fermentation tank 22 for circulation. Is characterized by That is, the methane fermentation tank 22, the alkali treatment tank 3,
The point is that the ammonia removing device 4 forms a circulation path.
【００２４】この第３発明は、メタン発酵槽２２、アル
カリ処理槽３、アンモニア除去装置４が形成する循環経
路において、アンモニア除去装置４とメタン発酵槽２２
との間に、炭酸ガス吸収装置５を付加するよう具体化で
きるのは、第２発明に類似している。すなわち、この場
合も炭酸ガス吸収装置５によって、前記メタン発酵槽２
２で発生する消化ガスｂ中に含まれる炭酸ガスをアンモ
ニア除去したアルカリ処理汚泥スラリに、吸収、移行さ
せて、メタンガスなど有用なガスを高濃度に取り出すこ
とができるのである。In the third aspect of the invention, the ammonia removal device 4 and the methane fermentation tank 22 are provided in the circulation path formed by the methane fermentation tank 22, the alkali treatment tank 3 and the ammonia removal device 4.
It is similar to the second invention in that the carbon dioxide gas absorption device 5 can be added between the two. That is, also in this case, the carbon dioxide absorption device 5 is used for the methane fermentation tank 2
The carbon dioxide gas contained in the digestion gas b generated in 2 can be absorbed and transferred to the alkali-treated sludge slurry from which ammonia has been removed, and useful gas such as methane gas can be extracted at a high concentration.
【００２５】（第４発明）次に、本発明の第４発明は、
図５に例示するフローで示される。第４発明の嫌気性発
酵システムは、有機廃棄物ａを酸発酵槽２１において酸
発酵させ、次いでメタン発酵槽２２でメタン発酵させ、
消化ガスｂを取り出すとともに、排出したメタン発酵汚
泥ｅを次工程に送るようにしたシステムを基本的フロー
としている。(Fourth Invention) Next, the fourth invention of the present invention will be described.
This is shown in the flow illustrated in FIG. In the anaerobic fermentation system of the fourth invention, the organic waste a is acid-fermented in the acid fermentation tank 21, and then methane-fermented in the methane fermentation tank 22.
The basic flow is a system in which the digested gas b is taken out and the discharged methane fermentation sludge e is sent to the next step.
【００２６】そして、その特徴とするところは、そのメ
タン発酵槽２２から引き抜かれたメタン発酵汚泥ｅの一
部をアルカリ処理槽３においてアルカリ処理を行い、次
いでアンモニア除去装置４においてアンモニアを除去し
た後、前記酸発酵槽２１に返送して循環させる点にあ
る。このように、メタン発酵槽２２、アルカリ処理槽
３、アンモニア除去装置４、酸発酵槽２１が循環経路を
形成している点がその要点である。The feature is that after a part of the methane fermentation sludge e extracted from the methane fermentation tank 22 is subjected to alkali treatment in the alkali treatment tank 3 and then ammonia is removed in the ammonia removal device 4. The point is that the acid fermenter 21 is returned and circulated. Thus, the point is that the methane fermentation tank 22, the alkali treatment tank 3, the ammonia removing device 4, and the acid fermentation tank 21 form a circulation path.
【００２７】なお、この場合、図５に例示するように、
アンモニア除去装置４と、酸発酵槽２１との間に、炭酸
ガス吸収装置５を付加するよう具体化できるのは、第
２、３発明にも類似している。すなわち、この炭酸ガス
吸収装置５によって、前記メタン発酵槽２２で発生する
消化ガスｂ中に含まれる炭酸ガスをアルカリ処理汚泥ス
ラリに吸収、移行させて、メタンガスなど有用なガスを
高濃度に取り出すことができるようにするのが好まし
い。In this case, as illustrated in FIG.
Similar to the second and third inventions, a carbon dioxide gas absorption device 5 can be added between the ammonia removal device 4 and the acid fermentation tank 21. That is, by using the carbon dioxide absorption device 5, carbon dioxide contained in the digestion gas b generated in the methane fermentation tank 22 is absorbed and transferred to the alkali-treated sludge slurry, and useful gas such as methane is taken out at a high concentration. Is preferable.
【００２８】[0028]
【実施例】次に、本願各発明のそれぞれについて、本発
明外の比較例とともに、実施例を以下に例示する。この
実施例によれば、本発明では、有機物消化率が比較例の
最大45%のものが54%〜61%になるなどの大幅な改善効果
が認められた。かくして、本発明によれば、より高濃度
の有機物を処理できることとなる。EXAMPLES Next, examples of each invention of the present application will be illustrated below together with comparative examples outside the invention. According to this example, in the present invention, a significant improvement effect was observed, such as the organic matter digestibility of the comparative example, which was 45% at the maximum, was 54% to 61%. Thus, according to the present invention, a higher concentration of organic matter can be treated.
【００２９】（実施例１：第１発明、図１参照）10L嫌
気性消化槽にVS 6%の有機性汚泥（下水余剰汚泥を遠心
濃縮して調製）を1L／日で供給する。また、この消化槽
から1L／日の消化汚泥を引き抜き、1Lアルカリ処理槽
（pH10.5、70℃に調整）でアルカリ処理し、次いでアン
モニア除去装置でアンモニアを除去し、それを消化槽に
返送する。(Example 1: First invention, see FIG. 1) An organic sludge of VS 6% (prepared by centrifugally concentrating sewage surplus sludge) is supplied to a 10 L anaerobic digestion tank at 1 L / day. In addition, 1 L / day of digested sludge is extracted from this digestion tank, alkali treated in a 1 L alkali treatment tank (pH 10.5, adjusted to 70 ° C), then ammonia is removed by an ammonia removal device, and it is returned to the digestion tank. To do.
【００３０】その結果を次に要約する。 有機物負荷 ：6kg／(m3日) 消化槽条件 ：pH 7.5、37℃ アンモニア除去量：2560mg-N／日 有機物の消化率 ：56% 発生消化ガス ：CH4 18.7L／日、CO2 3.3L／日 （CH4濃度 85.0%）The results are summarized below. Organic matter load: 6 kg / (m 3 days) Digestion tank conditions: pH 7.5, 37 ° C Ammonia removal amount: 2560 mg-N / day Organic matter digestibility: 56% Emitted digestion gas: CH 4 18.7 L / day, CO 2 3.3 L / Day (CH 4 concentration 85.0%)
【００３１】（実施例２：第２発明、図２参照）2Lの嫌
気性酸発酵槽にVS 6%の有機性汚泥（下水余剰汚泥を遠
心濃縮して調製）を1L／日で供給し、また、この酸発酵
槽から1L／日の消化汚泥を引き抜き、1Lのアルカリ処理
槽（pH10.5、70℃に調整）でアルカリ処理し、次いでア
ンモニア除去装置でアンモニアを除去し、それを酸発酵
槽に返送する。(Example 2: Second invention, see FIG. 2) VS 6% organic sludge (prepared by centrifugally concentrating sewage surplus sludge) was supplied to a 2 L anaerobic acid fermentation tank at 1 L / day, In addition, 1 L / day of digested sludge is drawn from this acid fermentation tank, alkali-treated in a 1 L alkali treatment tank (pH 10.5, adjusted to 70 ° C), and then ammonia is removed by an ammonia removal device, which is then acid-fermented. Return to the tank.
【００３２】その結果を次に要約する。 有機物負荷 ：30 kg／(m3日) 酸発酵槽条件 ：pH 6.8、50℃ アンモニア除去量 ：2490mg-N／日 有機物の酸発酵率 ：58% 酸発酵汚泥中有機酸濃度：34800mg/LThe results are summarized below. Organic matter load: 30 kg / (m 3 days) Acid fermenter conditions: pH 6.8, 50 ° C Ammonia removal amount: 2490 mg-N / day Acid fermentation rate of organic matter: 58% Organic acid concentration in acid fermentation sludge: 34800 mg / L
【００３３】（実施例３：第２発明、図３参照）2Lの嫌
気性酸発酵槽にVS 6%の有機性汚泥（下水余剰汚泥を遠
心濃縮して調製）を1L／日で供給し、また、この酸発酵
槽から1L／日の汚泥を引き抜き、1Lのアルカリ処理槽
（pH10.5、70℃に調整）でアルカリ処理し、次いでアン
モニア除去装置アンモニアを除去した後、炭酸ガス吸収
装置で消化ガスと気液接触させて、消化ガス中の炭酸ガ
スを吸収させ、それを酸発酵槽に返送する。酸発酵槽か
ら得られた酸発酵汚泥1L／日を8Lの嫌気性メタン発酵槽
で処理する。(Example 3: Second invention, see FIG. 3) 1 L / day of VS 6% organic sludge (prepared by centrifugally concentrating sewage surplus sludge) was fed to a 2 L anaerobic acid fermentation tank, In addition, 1 L / day of sludge was drawn from this acid fermentation tank, alkali-treated in a 1 L alkali treatment tank (pH 10.5, adjusted to 70 ° C), and then ammonia removal device After removing ammonia, use a carbon dioxide absorption device. It makes gas-liquid contact with the digestion gas to absorb the carbon dioxide gas in the digestion gas and returns it to the acid fermentation tank. 1 L / day of acid-fermented sludge obtained from the acid fermenter is treated in an 8 L anaerobic methane fermenter.
【００３４】その結果を次に要約する。 有機物負荷 ：酸発酵：30kg／(m3日)、メタン発酵：7.5kg／(m3日) 酸発酵槽条件 ：pH 6.8、50℃ メタン発酵槽条件：pH 7.2、37℃ アンモニア除去量：2790mg-N／日 有機物の消化率 ：61% CH4濃縮消化ガス：CH4 ：21.6L／日、CO2 ：2.4L／日（CH4濃度：90.0%）The results are summarized below. Organic matter load: Acid fermentation: 30 kg / (m 3 days), Methane fermentation: 7.5 kg / (m 3 days) Acid fermentation tank conditions: pH 6.8, 50 ° C Methane fermentation tank conditions: pH 7.2, 37 ° C Ammonia removal amount: 2790 mg -N / day organic matter digestibility: 61% CH 4 concentration biogas: CH 4: 21.6 L / day, CO 2: 2.4 L / day (CH 4 concentration: 90.0%)
【００３５】（実施例４：第３発明、図４参照）2Lの嫌
気性酸発酵槽にVS 6%の有機性汚泥（下水余剰汚泥を遠
心濃縮して調製）を1L／日で供給し、得られた酸発酵汚
泥1L／日を8L嫌気性メタン発酵槽で処理する。また、こ
のメタン発酵槽から1L／日の汚泥を引き抜き、1Lのアル
カリ処理槽（pH10.5、70℃に調整）でアルカリ処理し、
次いでアンモニア除去装置でアンモニアを除去した後、
それをメタン発酵槽に返送する。(Example 4: Third invention, see FIG. 4) VS 6% organic sludge (prepared by centrifugally concentrating sewage surplus sludge) was fed to a 2 L anaerobic acid fermentation tank at 1 L / day, 1 L / day of the obtained acid-fermented sludge is treated in an 8 L anaerobic methane fermentation tank. In addition, 1 L / day of sludge is drawn from this methane fermentation tank, and alkali treated in a 1 L alkali treatment tank (pH 10.5, adjusted to 70 ° C),
Next, after removing ammonia with an ammonia removing device,
Return it to the methane fermenter.
【００３６】その結果を次に要約する。 有機物負荷 ：酸発酵：30kg／(m3日)、メタン発酵：7.5kg／(m3日) 酸発酵槽条件 ：pH 6.8、50℃ メタン発酵槽条件：pH 7.2、37℃ アンモニア除去量：2470mg-N／日 有機物の消化率 ：54% CH4濃縮消化ガス ：CH4 ：17.6L／日、CO2 ：3.4L／日（CH4濃度 83.8%）The results are summarized below. Organic matter load: Acid fermentation: 30 kg / (m 3 days), Methane fermentation: 7.5 kg / (m 3 days) Acid fermentation tank conditions: pH 6.8, 50 ° C Methane fermentation tank conditions: pH 7.2, 37 ° C Ammonia removal amount: 2470 mg digestibility of -N / day organics: 54% CH 4 concentration digestion gas: CH 4: 17.6L / day, CO 2: 3.4L / day (CH 4 concentration 83.8%)
【００３７】（実施例５：第４発明、図５参照）2Lの嫌
気性酸発酵槽にVS 6%の有機性汚泥（下水余剰汚泥を遠
心濃縮して調製）を1L／日で供給し、得られた酸発酵汚
泥1L／日を8L嫌気性メタン発酵槽で処理する。また、こ
のメタン発酵槽から1L／日の汚泥を引き抜き、1Lのアル
カリ処理槽（pH10.5、70℃に調整）でアルカリ処理し、
次いでアンモニア除去装置でアンモニアを除去した後、
炭酸ガス吸収装置で消化ガスと気液接触させて、消化ガ
ス中の炭酸ガスを吸収させ、それを酸発酵槽に返送す
る。(Example 5: Fourth invention, see FIG. 5) An organic sludge of VS 6% (prepared by centrifugally concentrating excess sewage sludge) was supplied to a 2 L anaerobic acid fermentation tank at 1 L / day, 1 L / day of the obtained acid-fermented sludge is treated in an 8 L anaerobic methane fermentation tank. In addition, 1 L / day of sludge is drawn from this methane fermentation tank, and alkali treated in a 1 L alkali treatment tank (pH 10.5, adjusted to 70 ° C),
Next, after removing ammonia with an ammonia removing device,
The carbon dioxide absorption device is brought into gas-liquid contact with the digestion gas to absorb the carbon dioxide gas in the digestion gas and return it to the acid fermentation tank.
【００３８】その結果を次に要約する。 有機物負荷 ：酸発酵：30kg／(m3日)、メタン発酵：7.5kg／(m3日) 酸発酵槽条件 ：pH 6.8、50℃ メタン発酵槽条件：pH 7.2、37℃ アンモニア除去量：2600mg-N／日 有機物の消化率 ：59% CH4濃縮消化ガス ：CH4 ：19.6L／日、CO2 ：3.5L／日（CH4濃度 84.8%）The results are summarized below. Organic matter load: Acid fermentation: 30 kg / (m 3 days), Methane fermentation: 7.5 kg / (m 3 days) Acid fermentation tank conditions: pH 6.8, 50 ° C Methane fermentation tank conditions: pH 7.2, 37 ° C Ammonia removal amount: 2600 mg digestibility of -N / day organics: 59% CH 4 concentration digestion gas: CH 4: 19.6L / day, CO 2: 3.5L / day (CH 4 concentration 84.8%)
【００３９】（比較例１：記述した先願記載の方法、図
６参照）1Lのアルカリ処理槽にVS 6%の有機性汚泥（下
水余剰汚泥の遠心濃縮により調製）を1L／日で供給し、
pH10.5、70℃に調整してアルカリ処理し、次いでアンモ
ニア除去装置でアンモニアを除去し、それを10Lの消化
槽で嫌気性発酵する。その結果を次に要約する。
有機物負荷 ：6kg／(m3日)
消化槽条件 ：pH 8、37℃
アンモニア除去量：650mg-N／日
有機物の消化率 ：45%
発生消化ガス ：CH4 ：15.3L／日、CO2 ：1.7 L／日（CH4濃度 90.0%）(Comparative Example 1: Method described in the above-mentioned prior application, see FIG. 6) VS 1% organic sludge (prepared by centrifugal concentration of sewage surplus sludge) was supplied at 1 L / day to a 1 L alkali treatment tank. ,
The pH is adjusted to 10.5 and 70 ° C., alkali treatment is performed, and then ammonia is removed by an ammonia removing device, which is anaerobically fermented in a 10 L digester. The results are summarized below. Organic matter load: 6 kg / (m 3 days) Digestion tank conditions: pH 8, 37 ° C Ammonia removal amount: 650 mg-N / day Organic matter digestibility: 45% Digested gas: CH 4 : 15.3 L / day, CO 2 : 1.7 L / day (CH 4 concentration 90.0%)
【００４０】（比較例２：図６例示のフローからアンモ
ニア除去を行わない公知のアルカリ消化の場合）1Lのア
ルカリ処理槽にVS 6%の有機性汚泥（下水余剰汚泥を遠
心濃縮して調製）を1L／日で供給し、pH10.5、70℃に調
製してアルカリ処理し、次いで10Lの消化槽で直接、嫌
気性発酵する。その結果を次に要約する。
有機物負荷 ：6kg／(m3日)
消化槽条件 ：pH 8、37℃
アンモニア除去量：0mg-N／日
有機物の消化率 ：25%
発生消化ガス ：CH4 ：8.3L／日、CO2 ：1.0L／日（CH4濃度 89.2%）(Comparative Example 2: In the case of known alkali digestion without ammonia removal from the flow shown in FIG. 6) VS 6% organic sludge (prepared by centrifugally concentrating excess sewage sludge) in a 1 L alkali treatment tank Is supplied at 1 L / day, adjusted to pH 10.5, 70 ° C., treated with alkali, and then anaerobically fermented directly in a 10 L digester. The results are summarized below. Organic matter load: 6 kg / (m 3 days) Digestion tank conditions: pH 8, 37 ° C Ammonia removal amount: 0 mg-N / day Organic matter digestibility: 25% Digested gas: CH 4 : 8.3 L / day, CO 2 : 1.0L / day (CH 4 concentration 89.2%)
【００４１】（比較例３：アルカリ処理を行わない通常
の消化方法でVSが高濃度(6%)の場合）10Lの嫌気性消化
槽にVS 6%の有機性汚泥（下水余剰汚泥の遠心濃縮によ
り調製）を1L／日で供給する。その結果を次に要約す
る。
有機物負荷 ：6kg／(m3日)
アンモニア除去量：0mg-N／日
有機物の消化率 ：13%
発生消化ガス ：CH4 ：3.1L／日、CO2 ：2.0L／日（CH4濃度：60.8%）(Comparative Example 3: When the VS concentration is high (6%) by the usual digestion method without alkali treatment) VS 6% organic sludge (centrifugal concentration of excess sewage sludge in a 10 L anaerobic digestion tank) Prepared at 1 L / day. The results are summarized below. Organic matter load: 6 kg / (m 3 days) Ammonia removal amount: 0 mg-N / day Digestibility of organic matter: 13% Emitted digestion gas: CH 4 : 3.1 L / day, CO 2 : 2.0 L / day (CH 4 concentration: 60.8%)
【００４２】（比較例４：比較例３の通常消化でVSが通
常濃度(2%)の場合）
・10L嫌気性消化槽にVS 2%の有機性汚泥を1L／日で供
給。その結果を次に要約する。
有機物負荷 ：2kg／(m3日)
アンモニア除去量：0mg-N／日
有機物の消化率 ：45%
発生消化ガス ：CH4 ：3.5L／日、CO2 ：2.4L／日（CH4濃度：59.3%）(Comparative Example 4: When VS has a normal concentration (2%) in the normal digestion of Comparative Example 3) ・ VS 2% organic sludge was supplied at 1 L / day to a 10 L anaerobic digestion tank. The results are summarized below. Organic matter load: 2 kg / (m 3 day) Ammonia removal rate: 0 mg-N / day Digestibility of organic matter: 45% Digested gas: CH 4 : 3.5 L / day, CO 2 : 2.4 L / day (CH 4 concentration: 59.3%)
【００４３】[0043]
【発明の効果】本発明の有機廃棄物の嫌気性発酵システ
ムは、以上説明したように構成されているので、嫌気性
発酵工程の障害となるアンモニア態窒素が系外に除去で
きるので、発酵処理有機物の濃度を高めることができ、
嫌気性発酵システムのより効率的な運転が可能となる。
また、炭酸ガス吸収工程を付加すれば、消化ガス中のメ
タンを濃縮してメタン成分の濃度の高い消化ガスを得る
ことができる、さらに吸収した炭酸ガスを発酵工程に返
送してメタンの収量を増加できるなどという優れた効果
がある。よって本発明は、従来の問題点を解消した有機
廃棄物の嫌気性発酵システムとして、工業的価値はきわ
めて大なるものがある。EFFECT OF THE INVENTION Since the anaerobic fermentation system for organic waste of the present invention is configured as described above, the ammonia nitrogen which is an obstacle to the anaerobic fermentation process can be removed to the outside of the system. Can increase the concentration of organic matter,
It enables more efficient operation of the anaerobic fermentation system.
Also, if a carbon dioxide absorption step is added, it is possible to concentrate methane in the digested gas to obtain digested gas with a high concentration of methane components. Furthermore, the absorbed carbon dioxide is returned to the fermentation step to increase the methane yield. It has an excellent effect that it can be increased. Therefore, the present invention has an extremely great industrial value as an anaerobic fermentation system for organic waste that solves the conventional problems.
【図１】本願第１発明を説明するための要部フロー図。FIG. 1 is a flow chart of a main part for explaining a first invention of the present application.
【図２】本願第２発明を説明するための要部フロー図。FIG. 2 is a main part flowchart for explaining a second invention of the present application.
【図３】本願第２発明を説明するための要部フロー図。FIG. 3 is a main part flowchart for explaining the second invention of the present application.
【図４】本願第３発明を説明するための要部フロー図。FIG. 4 is a main part flowchart for explaining the third invention of the present application.
【図５】本願第４発明を説明するための要部フロー図。FIG. 5 is a main part flowchart for explaining a fourth invention of the present application.
【図６】本発明の基礎となる嫌気性消化方法の要部フロ
ー図。FIG. 6 is a main part flow chart of the anaerobic digestion method which is the basis of the present invention.
２ 消化槽、２１ 酸発酵槽、２２ メタン発酵槽、３
アルカリ処理槽、４アンモニア除去装置、５ 炭酸ガ
ス吸収装置、ａ 有機廃棄物、ｂ 消化ガス、ｃ 消化
汚泥、ｄ 酸発酵汚泥。2 digestion tanks, 21 acid fermentation tanks, 22 methane fermentation tanks, 3
Alkali treatment tank, 4 ammonia removal device, 5 carbon dioxide absorption device, a organic waste, b digested gas, c digested sludge, d acid fermentation sludge.
───────────────────────────────────────────────────── フロントページの続き (72)発明者 吉田 修一 愛知県名古屋市瑞穂区須田町２番56号 日 本碍子株式会社内 (72)発明者 坪井 博和 愛知県名古屋市瑞穂区須田町２番56号 日 本碍子株式会社内 (72)発明者 池田 裕一 愛知県名古屋市瑞穂区須田町２番56号 日 本碍子株式会社内 Ｆターム(参考） 4D004 AA03 CA18 CB04 CC01 CC12 4D011 AA15 AD03 4D059 AA01 AA03 AA05 AA07 BA13 BA17 BA21 BK12 BK15 BK16 CC03 DA01 DA37 ─────────────────────────────────────────────────── ─── Continued front page (72) Inventor Shuichi Yoshida 2-56, Sudacho, Mizuho-ku, Nagoya-shi, Aichi Inside Hon insulator Co., Ltd. (72) Inventor Hirokazu Tsuboi 2-56, Sudacho, Mizuho-ku, Nagoya-shi, Aichi Inside Hon insulator Co., Ltd. (72) Inventor Yuichi Ikeda 2-56, Sudacho, Mizuho-ku, Nagoya-shi, Aichi Inside Hon insulator Co., Ltd. F-term (reference) 4D004 AA03 CA18 CB04 CC01 CC12 4D011 AA15 AD03 4D059 AA01 AA03 AA05 AA07 BA13 BA17 BA21 BK12 BK15 BK16 CC03 DA01 DA37
Claims (8)
し、消化ガスを取り出すとともに、排出した消化汚泥を
次工程に送るようにした嫌気性発酵システムであって、
その消化汚泥の一部をアルカリ処理工程、次いでアンモ
ニア除去工程の各工程で処理した後、当該消化槽に返送
して循環させることを特徴とする有機廃棄物の嫌気性発
酵システム。1. An anaerobic fermentation system in which organic waste is anaerobically digested in a digestion tank, digested gas is taken out, and the discharged digested sludge is sent to the next step.
An anaerobic fermentation system for organic waste, wherein a part of the digested sludge is treated in each step of an alkali treatment step and then an ammonia removal step, and then returned to the digestion tank for circulation.
し、排出した酸発酵汚泥を次工程に送るようにした嫌気
性発酵システムであって、その酸発酵汚泥の一部をアル
カリ処理工程、次いでアンモニア除去工程の各工程で処
理した後、当該酸発酵槽に返送して循環させることを特
徴とする有機廃棄物の嫌気性発酵システム。2. An anaerobic fermentation system in which an organic waste is acid-fermented in an acid fermenter and the discharged acid-fermented sludge is sent to the next step, wherein a part of the acid-fermented sludge is treated with an alkali, An anaerobic fermentation system for organic waste, which is characterized by being returned to the acid fermentation tank for circulation after being treated in each step of the ammonia removal step.
システムにおいて、前記酸発酵汚泥を次工程のメタン発
酵工程でメタン発酵させ消化ガスを取り出すようにした
有機廃棄物の嫌気性発酵システム。3. The anaerobic fermentation system for organic waste according to claim 2, wherein the acid-fermented sludge is methane-fermented in a methane fermentation step of the next step to extract digested gas. .
システムにおいて、アンモニア除去したアルカリ処理汚
泥スラリに、前記消化ガス中の炭酸ガスを吸収、移行さ
せる炭酸ガス吸収工程を付加した有機廃棄物の嫌気性発
酵システム。4. The organic waste anaerobic fermentation system according to claim 3, wherein the ammonia-removed alkali-treated sludge slurry has a carbon dioxide absorption step for absorbing and transferring carbon dioxide in the digestion gas. Anaerobic fermentation system for things.
せ、次いでメタン発酵槽でメタン発酵させ、消化ガスを
取り出すとともに、排出したメタン発酵汚泥を次工程に
送るようにした嫌気性発酵システムであって、そのメタ
ン発酵汚泥の一部をアルカリ処理工程、次いでアンモニ
ア除去工程の各工程で処理した後、当該メタン発酵槽に
返送して循環させることを特徴とする有機廃棄物の嫌気
性発酵システム。5. An anaerobic fermentation system in which organic waste is acid-fermented in an acid fermenter and then methane-fermented in a methane fermenter to take out digested gas and send discharged methane-fermented sludge to the next step. An anaerobic fermentation system for organic waste, characterized in that a part of the methane fermentation sludge is treated in each step of an alkali treatment step and then an ammonia removal step, and then returned to the methane fermentation tank for circulation. .
システムにおいて、アンモニアを除去したアルカリ処理
汚泥スラリに、前記消化ガス中の炭酸ガスを吸収、移行
させる炭酸ガス吸収工程を付加した有機廃棄物の嫌気性
発酵システム。6. The organic waste anaerobic fermentation system according to claim 5, wherein an ammonia-removed alkali-treated sludge slurry is added with a carbon dioxide absorption step for absorbing and transferring carbon dioxide in the digestion gas. Anaerobic fermentation system for waste.
せ、次いでメタン発酵させ、消化ガスを取り出すととも
に、排出したメタン発酵汚泥を次工程に送るようにした
嫌気性発酵システムであって、そのメタン発酵汚泥の一
部をアルカリ処理工程、次いでアンモニア除去工程の各
工程で処理した後、当該酸発酵槽に返送して循環させる
ことを特徴とする有機廃棄物の嫌気性発酵システム。7. An anaerobic fermentation system in which an organic waste is acid-fermented in an acid fermenter and then methane-fermented to take out digested gas and send the discharged methane-fermented sludge to the next step. An anaerobic fermentation system for organic waste, wherein a part of methane fermentation sludge is treated in each step of an alkali treatment step and then an ammonia removal step, and then returned to the acid fermentation tank for circulation.
システムにおいて、アンモニアを除去したアルカリ処理
汚泥スラリに、前記消化ガス中の炭酸ガスを吸収、移行
させる炭酸ガス吸収工程を付加した有機廃棄物の嫌気性
発酵システム。8. The organic waste anaerobic fermentation system according to claim 7, wherein an ammonia-removed alkali-treated sludge slurry is added with a carbon dioxide absorption step for absorbing and transferring carbon dioxide in the digestion gas. Anaerobic fermentation system for waste.
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| JP2004195454A (en) * | 2002-12-04 | 2004-07-15 | Ngk Insulators Ltd | Method for recovering energy from ammonia derived from waste |
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