JPH0312960B2 - - Google Patents
Info
- Publication number
- JPH0312960B2 JPH0312960B2 JP59060318A JP6031884A JPH0312960B2 JP H0312960 B2 JPH0312960 B2 JP H0312960B2 JP 59060318 A JP59060318 A JP 59060318A JP 6031884 A JP6031884 A JP 6031884A JP H0312960 B2 JPH0312960 B2 JP H0312960B2
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- methane
- zone
- liquefaction
- fermenter
- 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.)
- Expired - Lifetime
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
- Treatment Of Sludge (AREA)
Description
【発明の詳細な説明】
産業上の利用分野
本発明は、汚泥の局部循環によるメタン発酵方
法に関し、さらに詳しくは、嫌気性発酵槽を使用
して湿性有機廃棄物またはバイオマスをメタン発
酵するに際し、発酵の各段階に最適の菌種を付与
するために、汚泥の局部的返送を行う嫌気性発酵
方法に関する。DETAILED DESCRIPTION OF THE INVENTION Field of Industrial Application The present invention relates to a method for methane fermentation by local circulation of sludge, and more particularly, for methane fermentation of wet organic waste or biomass using an anaerobic fermenter. This invention relates to an anaerobic fermentation method in which sludge is locally returned in order to provide optimal bacterial species to each stage of fermentation.
従来技術とその問題点
メタン発酵においては、多くの有機物が下記の
三段階の分解によりメタン転化することが知られ
ている。Prior art and its problems In methane fermentation, it is known that many organic substances are converted to methane through the following three-stage decomposition.
(1) 液化（低分子化分解）
(2) 酸生成（低分子有機酸の生成）
(3) メタン生成（メタンガス発生、主に脱炭酸反
応）
これらの各段階に関与する菌種は、それぞれ異
なつている。菌を移植することにより発酵促進を
図るために、発酵残渣の一部を返送・循環するこ
とは、常法の手段である。しかしながら、従来一
般に行われている様に、(3)メタン生成段階を終え
た最終残渣を発酵槽前端の(1)液化段階に返送する
ことは、種々の問題を生ずる。即ち、最終残渣に
含まれる菌種は、(3)メタン生成段階に最適化され
ているため、返送後直ちに(1)液化段階の菌種に適
合することは、出来ない。また、(3)メタン生成段
階は、最も弱い偏性嫌気性菌により維持されてい
るので、(1)液化段階および(2)酸生成段階の液性
（弱酸性）では、偏性嫌気性菌が生存し難く、返
送された最終残渣中の菌種が(3)メタン生成段階ま
で辿り着くことは、容易ではない。(1) Liquefaction (decomposition into low molecular weight molecules) (2) Acid production (generation of low molecular weight organic acids) (3) Methane production (methane gas generation, mainly decarboxylation reaction) The bacterial species involved in each of these steps are different from each other. It's different. In order to promote fermentation by transplanting bacteria, it is a common method to return and circulate a portion of the fermentation residue. However, returning the final residue from the (3) methane production stage to the (1) liquefaction stage at the front end of the fermenter, as has been conventionally done, causes various problems. That is, since the bacterial species contained in the final residue is optimized for the (3) methane production stage, it is not possible to immediately match the bacterial species for the (1) liquefaction stage after return. In addition, (3) the methane production stage is maintained by the weakest obligate anaerobes, so in the (1) liquefaction stage and (2) acid production stage (weakly acidic), obligate anaerobes It is difficult for the bacterial species in the returned final residue to reach the (3) methane production stage.
問題点を解決するための手段
本発明者は、上記の従来技術の問題点に鑑みて
研究を進めた結果、上記(1)〜(3)の各段階で最適化
された菌種をそれぞれの段階で返送することによ
り、返送菌群を最も有効に作用させることに成功
した。Means for Solving the Problems As a result of conducting research in view of the problems of the prior art described above, the present inventor has developed bacterial strains optimized in each step of (1) to (3) above. By returning the bacteria in stages, we succeeded in making the returned bacteria most effective.
即ち、本発明は、下記のメタン発酵方法を提供
するものである：
「嫌気性発酵槽を使用して湿性有機廃棄物また
はバイオマスをメタン発酵するに際し、発酵槽内
の液化域、酸生成域およびメタン化域のそれぞれ
において汚泥の局部循環を行うことを特徴とする
汚泥の局部循環によるメタン発酵方法。」
以下添付図面を参照しつつ、本発明をさらに詳
細に説明する。 That is, the present invention provides the following methane fermentation method: "When methane fermenting wet organic waste or biomass using an anaerobic fermenter, a liquefaction zone, an acid production zone and a A methane fermentation method by local circulation of sludge, characterized in that the sludge is locally circulated in each of the methanation zones.'' The present invention will be described in more detail below with reference to the accompanying drawings.
第１図に示す嫌気性発酵槽は、液化域A1、酸
生成域A2およびメタン化域Ｂにより構成されて
いる。嫌気性発酵槽の左端から投入された生汚
泥、バイオマスなどの被処理物Ｓは、液化域A1
内で循環する液化菌を多量に含む返送汚泥R3と
接触して、直ちに低分子化分解発酵（液化）が始
まる。低分子化分解発酵処理された被処理物Ｓ
が、液化域A1を通過する際に、沈殿に富む汚泥
部分（液化菌および未分解残渣を含む）が抽出返
送されるとともに、残余の液体の大部分が、酸生
成域A2へと送られ、酸生成菌に富む返送汚泥R2
に接触して、直ちに酸生成発酵が始まる。酸生成
域A2において、低分子被処理物から可溶性有機
物である低級脂肪酸（主として酢酸からなる）へ
の分解が進行したところで、酸生成菌に富む汚泥
R2が、抽出返送されるとともに、弱酸性の液体
の大部分が、次のメタン化域Ｂに送られる。メタ
ン化域Ｂにおいて、該液体は、メタン菌に富み且
つ弱アルカリ性である返送汚泥R1と接触して、
中和され、メタン発酵が進行する。大部分の分解
性有機物が主としてメタンと炭酸ガスとからなる
ガスＧに転化して稀薄液となつた上澄液は、消化
脱離液Ｌとして系外に排出され、一方、沈殿は、
消化汚泥R0として系外に排出される。 The anaerobic fermentor shown in FIG. 1 is comprised of a liquefaction zone A 1 , an acid production zone A 2 and a methanation zone B. The materials to be treated S such as raw sludge and biomass input from the left end of the anaerobic fermentation tank are transferred to the liquefaction area A1.
Upon contact with the returned sludge R3 containing a large amount of liquefaction bacteria circulating within the sludge, low-molecular decomposition fermentation (liquefaction) immediately begins. Processed material S subjected to low molecular weight decomposition fermentation treatment
When passing through liquefaction zone A 1 , the sludge portion rich in sediment (containing liquefied bacteria and undecomposed residue) is extracted and returned, and most of the remaining liquid is sent to acid production zone A 2 . Returned sludge rich in acid-producing bacteria R 2
upon contact, acid-producing fermentation begins immediately. In acid production zone A 2 , when the decomposition of low-molecular substances to be treated into lower fatty acids (mainly consisting of acetic acid), which are soluble organic substances, has progressed, sludge rich in acid-producing bacteria is produced.
R 2 is extracted and returned, and most of the weakly acidic liquid is sent to the next methanation zone B. In the methanation zone B, the liquid contacts the return sludge R1 , which is rich in methane bacteria and is slightly alkaline,
It is neutralized and methane fermentation progresses. The supernatant liquid, in which most of the decomposable organic matter is converted into gas G mainly consisting of methane and carbon dioxide gas, becomes a dilute liquid, and is discharged outside the system as the digestion and desorption liquid L. On the other hand, the precipitate is
It is discharged outside the system as digested sludge R 0 .
消化脱離剤Ｌおよび消化汚泥R0は、適宜分析
されて、未分解物が多いことが判明した場合に
は、返送汚泥R1の量を増加させて、分解促進を
図る。 The digestive desorption agent L and the digested sludge R 0 are analyzed as appropriate, and if it is found that there are many undecomposed substances, the amount of the returned sludge R 1 is increased to promote decomposition.
消化脱離液Ｌと消化汚泥R0との完全な分離は、
一版に困難であるが、その中間の混濁液を抜き取
り、返送汚泥R1とともに返送することにより、
両者の分離は容易となる。 Complete separation of digested desorbed liquid L and digested sludge R0 is as follows:
Although it is difficult to make one version, by extracting the turbid liquid in between and returning it with return sludge R1 ,
Separation of the two becomes easy.
また、土砂に富む残渣は消化汚泥の下部に集ま
り、菌体を多く含む軽い残渣はその上部に集まる
傾向にあるので、菌体の返送循環には、沈殿槽の
中部から抽出返送するのが好ましいことは、すで
に本発明者が見出している（特開昭59−105896号
公報）。但し、該出願の発明は、発酵槽の終端部
から抽出した返送汚泥を発酵槽の前端部に返送し
ており、発酵槽の各段階毎に最適化された状態で
汚泥の返送を行う本発明とは、明確に区別される
ものである。 Additionally, residue rich in earth and sand tends to collect at the bottom of the digested sludge, and light residue containing many bacterial cells tends to collect at the top, so it is preferable to extract and return the bacterial cells from the middle of the settling tank for return circulation. This fact has already been discovered by the present inventor (Japanese Patent Laid-Open No. 105896/1983). However, the invention of the application returns the return sludge extracted from the end of the fermenter to the front end of the fermenter, and the present invention returns the sludge in an optimized state for each stage of the fermenter. are clearly distinguishable.
本発明方法を実施するために使用する発酵槽と
しては、特に制限はない。例えば、仕切板Ｗを備
えた発酵槽（第２図）、仕切りネツトＮを備えた
発酵槽（第３図）、嫌気性回転円板Ｄを備えた発
酵槽（第４図）などの他に、最も簡易な静置型長
槽（第１図）であつても良い。なお、Ｐは、返送
ポンプである。 There are no particular limitations on the fermenter used to carry out the method of the present invention. For example, in addition to a fermenter equipped with a partition plate W (Fig. 2), a fermenter equipped with a partition net N (Fig. 3), a fermenter equipped with an anaerobic rotating disk D (Fig. 4), etc. , the simplest stationary type long tank (Fig. 1) may be used. Note that P is a return pump.
発酵槽内での混合は、各域の独立した特性を失
わせる様な前後方向での混合を生じない様に、換
言すれば、各域内での混合のみを生じる様に、緩
やかに行うことが好ましい。この様な緩やかな混
合は、全体的な被処理物の流れによつても、汚泥
の返送流によつても、或いは第４図に示す様な回
転板による撹拌によつても、行うことができる。
撹拌が不十分である場合には、発酵槽内で発生
し、系外に排出されるガスを送入して撹拌を促進
しても良い。 Mixing in the fermenter should be done slowly so as not to cause mixing in the front-rear direction that would cause the independent characteristics of each zone to be lost, in other words, to only cause mixing within each zone. preferable. Such gentle mixing can be achieved by the overall flow of the material to be treated, by the return flow of sludge, or by stirring with a rotating plate as shown in Figure 4. can.
If stirring is insufficient, stirring may be promoted by introducing gas generated within the fermenter and discharged outside the system.
汚泥R1，R2およびR3の返送は、吸引ポンプ、
流送ポンプなどの公知の手段を使用することが出
来る。 Sludge R 1 , R 2 and R 3 are returned using suction pumps,
Known means such as flow pumps can be used.
汚泥R1，R2およびR3の返送量は、分解処理対
象である原料の組成、分解性などにより大きく異
なる。例えば、平均的な下水汚泥の場合には、流
入量の50±25％程度とすることが適当である。原
料の分解性が低い程、返送率を高くすべきこと
は、言うまでもない。 The amount of sludge R 1 , R 2 and R 3 to be returned varies greatly depending on the composition, degradability, etc. of the raw material to be decomposed. For example, in the case of average sewage sludge, it is appropriate to set the amount to about 50±25% of the inflow amount. It goes without saying that the lower the decomposability of the raw material, the higher the return rate should be.
発明の効果
本発明方法によれば、下記の様な効果が達成さ
れる。Effects of the Invention According to the method of the present invention, the following effects can be achieved.
(1) 一般に、メタン菌は、その濃度を高く維持す
ることが困難であるとされている。しかるに、
本発明においては、発酵槽内の液化域、酸生成
域およびメタン化域という各段階毎に最適化さ
れた状態で汚泥の返送を行うので、メタン菌の
濃度を高レベルに維持管理することは、容易で
ある。(1) Generally, it is difficult to maintain a high concentration of methane bacteria. However,
In the present invention, sludge is returned in an optimized state for each stage of the liquefaction zone, acid production zone, and methanation zone in the fermenter, so it is difficult to maintain and manage the concentration of methane bacteria at a high level. , is easy.
(2) また、液化菌および酸生成菌も、その活動域
において循環されるので、有機物の分解速度を
高めて、発酵槽の容積を減少させることがで
き、メタン収率を高くなる。(2) In addition, since liquefaction bacteria and acid-producing bacteria are also circulated in their active areas, the rate of decomposition of organic matter can be increased, the volume of the fermenter can be reduced, and the methane yield can be increased.
(3) さらに、メタン発酵槽の失調の主な原因とな
る負荷の急増、有機酸の急増などの現象も、返
送汚泥R2およびR3の段階で観測できるので、
失調に至る前に適確な対策（例えば、中和量の
石灰の投入など）を取ることができる。(3) In addition, phenomena such as rapid increases in load and rapid increase in organic acids, which are the main causes of malfunction in methane fermenters, can be observed at the stages of return sludge R 2 and R 3 .
Appropriate measures (for example, adding a neutralizing amount of lime) can be taken before ataxia occurs.
第１図は、本発明の基本的構成を説明するため
の概念的フロー図を示し、第２図乃至第４図は、
本発明において使用することが出来る種々の形式
の発酵槽を示す。
Ｓ……生汚泥、バイオマスなどの原料、Ｇ……
ガス、Ｌ……消化脱離液、R0……消化残渣、R1，
R2，R3……返送汚泥、A1……液化域、A2……酸
生成域、Ｂ……メタン化域、Ｐ……返送ポンプ、
Ｗ……仕切り板、Ｎ……ネツト、Ｄ……回転板。
FIG. 1 shows a conceptual flow diagram for explaining the basic configuration of the present invention, and FIGS. 2 to 4 show
1 shows various types of fermenters that can be used in the present invention. S... Raw materials such as raw sludge and biomass, G...
Gas, L...Digestion desorption liquid, R0 ...Digestion residue, R1 ,
R 2 , R 3 ... Return sludge, A 1 ... Liquefaction region, A 2 ... Acid generation region, B ... Methanization region, P ... Return pump,
W: Partition plate, N: Net, D: Rotating plate.
Claims (1)
はバイオマスをメタン発酵するに際し、発酵槽内
の液化域、酸生成域およびメタン化域のそれぞれ
において汚泥の局部循環を行うことを特徴とする
汚泥の局部循環によるメタン発酵方法。1. A sludge characterized by local circulation of sludge in each of the liquefaction zone, acid generation zone, and methanation zone in the fermentation tank when methane fermenting wet organic waste or biomass using an anaerobic fermentation tank. Methane fermentation method using local circulation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59060318A JPS60202798A (en) | 1984-03-27 | 1984-03-27 | Methane fermentation apparatus utilizing composite local recirculation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59060318A JPS60202798A (en) | 1984-03-27 | 1984-03-27 | Methane fermentation apparatus utilizing composite local recirculation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS60202798A JPS60202798A (en) | 1985-10-14 |
| JPH0312960B2 true JPH0312960B2 (en) | 1991-02-21 |
Family
ID=13138705
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP59060318A Granted JPS60202798A (en) | 1984-03-27 | 1984-03-27 | Methane fermentation apparatus utilizing composite local recirculation |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS60202798A (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2740508B2 (en) * | 1987-12-28 | 1998-04-15 | ヴァロルガ | Biogas production equipment |
| JPH09168798A (en) * | 1996-12-04 | 1997-06-30 | Valorga | Biogas production method |
| JP2002307098A (en) * | 2001-04-13 | 2002-10-22 | Mitsubishi Heavy Ind Ltd | Anaerobic digestion method and anaerobic digester for organic sludge |
| FR2994441B1 (en) * | 2012-08-13 | 2017-02-10 | Michel Bonhomme | MAINLY ANAEROBIC, CONTINUOUS, MULTI-PHASE, POLYSUBTRAT, FERMENTATION PROCESS AND PLANT IN THICK MATERIAL |
| JP2017209614A (en) * | 2016-05-24 | 2017-11-30 | 日本プライスマネジメント株式会社 | Methane fermentation apparatus |
| JP7292535B1 (en) * | 2022-04-08 | 2023-06-16 | 三菱電機株式会社 | ORGANIC WASTE TREATMENT SYSTEM AND ORGANIC WASTE TREATMENT METHOD |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5814278A (en) * | 1981-07-17 | 1983-01-27 | Nec Corp | Bar code reader |
| JPS59384A (en) * | 1982-06-26 | 1984-01-05 | Kubota Ltd | Anaerobic digestion of organic waste liquor |
-
1984
- 1984-03-27 JP JP59060318A patent/JPS60202798A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS60202798A (en) | 1985-10-14 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EXPY | Cancellation because of completion of term |