JP2000153259A - Methane fermentation method of easily degradable organic waste - Google Patents
Methane fermentation method of easily degradable organic wasteInfo
- Publication number
- JP2000153259A JP2000153259A JP10331823A JP33182398A JP2000153259A JP 2000153259 A JP2000153259 A JP 2000153259A JP 10331823 A JP10331823 A JP 10331823A JP 33182398 A JP33182398 A JP 33182398A JP 2000153259 A JP2000153259 A JP 2000153259A
- Authority
- JP
- Japan
- Prior art keywords
- fermentation
- methane
- sludge
- acid
- 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.)
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Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- 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)
- Treatment Of Sludge (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、易分解性有機性廃
棄物のメタン発酵方法に関する。The present invention relates to a method for methane fermentation of easily decomposable organic waste.
【０００２】[0002]
【従来の技術】有機性廃棄物の再資源化において、生ご
み等の易分解性有機性廃棄物は通常、破砕し、プラスチ
ック袋やトレーなどの発酵不適物を分別した後にメタン
発酵させて、メタンガスを回収するようにしており、そ
の際に発生する余剰の発酵汚泥は引抜いて薬注した上で
脱水し、コンポスト化等している。2. Description of the Related Art In the recycling of organic waste, easily decomposable organic waste such as garbage is usually crushed, and methane fermentation is performed after separating unsuitable fermentation products such as plastic bags and trays. Methane gas is recovered, and excess fermented sludge generated at that time is extracted, injected with chemicals, dehydrated, and composted.
【０００３】[0003]
【発明が解決しようとする課題】ところで、発酵汚泥を
脱水した際の脱水濾液は水処理系へ送って処理している
ため、ＳＳ濃度を低くしなければならず、脱水時にポリ
マー等の凝集助剤の添加が不可欠であった。生ごみのみ
を発酵対象物とした時の発酵汚泥はアルカリ度が高いた
めに脱水性が悪く、ポリマーが大量に必要であった。By the way, since the dewatered filtrate from the dewatering of the fermented sludge is sent to the water treatment system for treatment, the SS concentration must be reduced, and the coagulation of polymers and the like during the dehydration is reduced. Addition of the agent was essential. When only garbage was used as the fermentation target, the fermented sludge was poor in dehydration due to high alkalinity, and required a large amount of polymer.
【０００４】また、メタン発酵に際しては、酸発酵過程
とメタン発酵過程とを別途の発酵槽で行い、酸発酵を促
進するために、メタン発酵過程から引抜いた発酵汚泥も
しくはその脱水濾液を酸発酵過程に返送するようにして
いるが、発酵汚泥そのものを返送すると、汚泥中に含ま
れている砂分などが次第に槽内に蓄積してくるため発酵
効率の面で理想的ではなく、ポリマー添加した脱水濾液
を返送すると、槽内のＳＳ濃度を高く維持するのが困難
であった。生ごみ等の易分解性有機物をメタン発酵槽に
直接投入すると、メタン発酵槽内の水素分圧が上昇し、
プロピオン酸の分解が妨げられるという問題もあった。In methane fermentation, the acid fermentation process and the methane fermentation process are performed in separate fermenters, and the fermented sludge extracted from the methane fermentation process or the dehydrated filtrate thereof is subjected to acid fermentation in order to promote acid fermentation. However, if the fermented sludge itself is returned, sand contained in the sludge gradually accumulates in the tank, which is not ideal in terms of fermentation efficiency. When the filtrate was returned, it was difficult to keep the SS concentration in the tank high. When easily decomposable organic matter such as garbage is directly injected into the methane fermentation tank, the hydrogen partial pressure in the methane fermentation tank increases,
There was also a problem that decomposition of propionic acid was hindered.
【０００５】本発明は上記問題を解決するもので、易分
解性有機性廃棄物を効率よくメタン発酵させることがで
き、かつ余剰の発酵汚泥を効率よく処理できるようにす
ることを目的とするものである。An object of the present invention is to solve the above-mentioned problems, and an object of the present invention is to enable methane fermentation of easily decomposable organic wastes efficiently and to treat excess fermented sludge efficiently. It is.
【０００６】[0006]
【課題を解決するための手段】上記問題を解決するため
に、本発明は、生ごみなどの易分解性有機性廃棄物を酸
発酵槽とメタン発酵槽とに順次に送ってメタン発酵させ
るに際し、前記メタン発酵槽内の余剰の発酵汚泥を引抜
くとともに、槽内の発酵汚泥中の液状分を膜分離手段に
よって抽出することにより、メタン発酵槽内に適当濃度
の発酵汚泥を保持し、前記引抜いた発酵汚泥を無薬注に
て脱水手段で脱水し、脱水濾液を前記酸発酵槽へ返送す
ることにより、酸発酵槽内の酸発酵物を調質するように
したものである。SUMMARY OF THE INVENTION In order to solve the above-mentioned problems, the present invention relates to a method for sequentially feeding easily decomposable organic waste such as garbage to an acid fermentation tank and a methane fermentation tank for methane fermentation. While extracting the excess fermented sludge in the methane fermentation tank, and extracting the liquid component in the fermentation sludge in the tank by membrane separation means, to maintain the fermentation sludge of the appropriate concentration in the methane fermentation tank, The extracted fermented sludge is dewatered by a dewatering means without chemical injection, and the dehydrated filtrate is returned to the acid fermentation tank to condition the acid fermentation product in the acid fermentation tank.
【０００７】上記した構成によれば、膜分離手段によっ
てＳＳ濃度の低い液状分を抽出できるので、メタン発酵
槽において槽内ＳＳ濃度を容易に調整できるだけでな
く、抽出した液状分を直接に水処理工程へ送って処理す
ることが可能となる。[0007] According to the above-mentioned structure, since the liquid component having a low SS concentration can be extracted by the membrane separation means, not only the SS concentration in the methane fermentation tank can be easily adjusted, but also the extracted liquid component can be directly treated with water. It can be sent to the process for processing.
【０００８】したがって、引抜いた発酵汚泥を脱水する
際に、脱水濾液のＳＳ濃度を低減することを考慮する必
要はなく、そのためのポリマー、ｐＨ調整剤を添加する
ことなく脱水できる。Therefore, it is not necessary to consider reducing the SS concentration of the dewatered filtrate when dewatering the extracted fermented sludge, and the dewatering can be performed without adding a polymer and a pH adjuster therefor.
【０００９】その結果、汚泥中の砂分などを脱水ケーキ
側に移行させて系外に排出できるとともに、ＳＳ濃度お
よびアルカリ度の高い脱水濾液を得ることができ、この
脱水濾液を酸発酵槽に返送することで、槽内のＳＳ濃度
を著しく低下させることなく酸性度を低下させて酸発酵
を促進することができ、それによりメタン発酵も促進で
きる。As a result, sand and the like in the sludge can be transferred to the dewatering cake side and discharged out of the system, and a dehydrated filtrate having a high SS concentration and alkalinity can be obtained. By returning it, acidity can be reduced and acid fermentation can be promoted without significantly lowering the SS concentration in the tank, whereby methane fermentation can also be promoted.
【００１０】[0010]
【発明の実施の形態】以下、本発明の実施形態を図面を
参照しながら説明する。図１は、性状や濃度が異なる有
機性廃棄物を同一システムで処理し、有用物質を回収す
るフローを示し、し尿、浄化槽汚泥などのスラッジ状有
機性廃棄物１は、細目スクリーン２などでし渣３を分離
した後に水処理工程へ送り、脱窒素槽４、硝化槽５、二
次脱窒素槽６、膜分離槽７に順次導入して、生物処理に
よりＢＯＤ分解並びに脱窒素し、膜分離装置８により活
性汚泥などの浮遊物を分離し、膜分離水９を高度処理設
備（図示せず）に導入して、ＣＯＤや色素成分や鉄・マ
ンガンなどの重金属類を除去し、消毒して放流する。Embodiments of the present invention will be described below with reference to the drawings. Fig. 1 shows the flow of treating organic wastes with different properties and concentrations with the same system and recovering useful substances. Sludge-like organic wastes 1 such as human waste and septic tank sludge are treated with a fine screen 2 or the like. After the residue 3 is separated, it is sent to a water treatment step, and is sequentially introduced into a denitrification tank 4, a nitrification tank 5, a secondary denitrification tank 6, and a membrane separation tank 7, where BOD decomposition and denitrification are performed by biological treatment, and membrane separation is performed. The suspended matter such as activated sludge is separated by the apparatus 8, and the membrane separation water 9 is introduced into an advanced treatment facility (not shown) to remove COD, pigment components, and heavy metals such as iron and manganese, and disinfect them. Release.
【００１１】一方、生ごみなど、固形分を含んだ易分解
性有機性廃棄物１０は、一軸破砕機１１などの粗破砕機
で粒径２０〜１００ｍｍ以下に粗破砕した後に、圧縮破
砕機１２で２００〜２５０ｋｇ／ｃｍ2 の高圧にて圧縮
破砕し、ペースト状有機性廃棄物１３として排出する。
機内に残留した破砕不能なし渣、プラスチック類、金属
類、石・砂などの発酵不適物１４は別途に取り出す。On the other hand, the easily decomposable organic waste 10 containing solids such as garbage is roughly crushed to a particle size of 20 to 100 mm or less by a coarse crusher such as a uniaxial crusher 11 and then compressed and crushed by a compression crusher 12. And compressed and crushed at a high pressure of 200 to 250 kg / cm 2 , and discharged as paste-like organic waste 13.
Unfermentable residue 14 such as non-crushable residue, plastics, metals, stone and sand remaining in the machine is separately taken out.
【００１２】圧縮破砕機１２より排出されたペースト状
有機性廃棄物１３はメタン発酵工程へ送り、後述する脱
水濾液とともに酸発酵槽１６へ導入して攪拌しつつ酸発
酵させる。そして、槽内に所定時間だけ滞留して十分に
酸発酵した酸発酵液１７をヒーター１８で加温し、上述
した膜分離水９で濃度調整してメタン発酵槽１９に送
り、約５５℃、嫌気性条件下に維持する状態においてメ
タン発酵させ、発生したメタンなどのバイオガス２０を
回収する。膜分離水９による濃度調整は酸発酵槽１６で
行ってもよく、メタン発酵槽１９の内容物はバイオガス
２０や窒素ガスなどにより曝気攪拌する。そして、メタ
ン発酵槽１９内の余剰の発酵汚泥２１を引抜き、遠心脱
水機２２などの脱水手段で無薬注にて脱水して、脱水ケ
ーキ２３と脱水濾液２４とに分離する。The paste-like organic waste 13 discharged from the compression crusher 12 is sent to a methane fermentation step, and is introduced into an acid fermentation tank 16 together with a dehydrated filtrate to be described later, and is subjected to acid fermentation with stirring. Then, the acid fermentation solution 17 that has been retained in the tank for a predetermined time and has been sufficiently acid-fermented is heated by the heater 18, the concentration is adjusted by the above-mentioned membrane separation water 9, and sent to the methane fermentation tank 19 at about 55 ° C. Methane fermentation is performed in a state maintained under anaerobic conditions, and biogas 20 such as methane generated is collected. The concentration adjustment with the membrane separation water 9 may be performed in the acid fermentation tank 16, and the contents of the methane fermentation tank 19 are aerated and agitated with biogas 20, nitrogen gas, or the like. Then, the surplus fermented sludge 21 in the methane fermentation tank 19 is drawn out, dewatered by a chemical-free injection using a dehydrating means such as a centrifugal dehydrator 22, and separated into a dehydrated cake 23 and a dehydrated filtrate 24.
【００１３】その際に、易分解性有機性廃棄物１０の予
想分解率および遠心脱水機２２におけるＳＳ（ＴＳ）回
収率よりメタン発酵槽１９内のＳＳ濃度を予想し、適当
な槽内ＳＳ濃度、約２．５％〜６．０％が維持されるよ
うに、余剰の発酵汚泥２１を引抜くとともに、発酵汚泥
２１を膜分離槽２５に循環させて膜分離装置２６によっ
て発酵液２７を抽出することで、溶解性阻害物質（アン
モニア、高濃度の有機酸）を希釈する。抽出した発酵液
２７は水処理工程へ送って処理する。At this time, the SS concentration in the methane fermentation tank 19 is predicted from the expected decomposition rate of the easily decomposable organic waste 10 and the SS (TS) recovery rate in the centrifugal dehydrator 22, and an appropriate SS concentration in the tank is determined. The excess fermented sludge 21 is pulled out so that about 2.5% to 6.0% is maintained, and the fermented sludge 21 is extracted by the membrane separation device 26 by circulating the fermented sludge 21 to the membrane separation tank 25. This dilutes the solubility inhibitor (ammonia, high concentration of organic acid). The extracted fermentation liquid 27 is sent to a water treatment step for processing.
【００１４】脱水濾液２４は酸発酵槽１５へ返送する
が、この脱水濾液２４は無薬注であるためＳＳ濃度およ
びアルカリ度が高く、返送された酸発酵槽１５で槽内Ｓ
Ｓ濃度の著しい低下を招くことなく酸性度を低下させる
ため酸発酵が促進される。その結果、酸発酵液１７がメ
タン発酵槽１９に送られた時も水素分圧の上昇等の悪影
響は生じず、上述したように適当な槽内ＳＳ濃度が維持
され、また阻害物質濃度が低減されることもあって、メ
タン発酵が促進される。The dehydrated filtrate 24 is returned to the acid fermentation tank 15. Since the dehydrated filtrate 24 is non-chemically injected, the SS concentration and the alkalinity are high.
Acid fermentation is promoted because acidity is reduced without causing a significant decrease in S concentration. As a result, even when the acid fermentation liquid 17 is sent to the methane fermentation tank 19, no adverse effect such as an increase in the hydrogen partial pressure occurs, and as described above, the appropriate SS concentration in the tank is maintained and the inhibitory substance concentration is reduced. In some cases, methane fermentation is promoted.
【００１５】回収したバイオガス２０は脱硫塔２８など
で硫化水素、水分等を除去した後、ガスホルダー２９に
貯溜し、余剰ガス３０は燃焼装置３１で燃焼させて、燃
焼熱をヒータ１８などで利用する。脱水ケーキ２３はコ
ンポスト化して肥料としたり、固形燃料や乾燥汚泥とす
る。The recovered biogas 20 is removed in a desulfurization tower 28 or the like to remove hydrogen sulfide, moisture, etc., and then stored in a gas holder 29. The surplus gas 30 is burned by a combustion device 31 and the combustion heat is heated by a heater 18 or the like. Use. The dewatered cake 23 is composted into fertilizer, solid fuel or dried sludge.
【００１６】なお、上記したフローでは、易分解性有機
性廃棄物１０を圧縮破砕機１２によってペースト状に圧
縮破砕するようにしたため、発酵不適物１４を自動分別
できるとともに、高い生物分解性および有機成分回収率
を確保できるが、無薬注脱水としたことによって、発酵
汚泥２１中に発酵不適物が含まれていた場合も脱水ケー
キ２３に含まれ排出されて槽内に蓄積せず、一方では微
生物はＳＳ分に含まれて残留するため効率的に発酵が行
われることになり、脱水ケーキ２３自体も含水率が低く
なるため、コンポスト化等が容易になる。In the above-mentioned flow, the easily decomposable organic waste 10 is compressed and crushed into a paste by the compression crusher 12, so that unsuitable fermentation products 14 can be automatically separated, and high biodegradability and organic waste can be obtained. Although the component recovery rate can be ensured, due to the non-chemical injection dehydration, even when fermentation unsuitable substances are contained in the fermented sludge 21, they are contained in the dewatered cake 23 and discharged and do not accumulate in the tank. Since the microorganisms are contained in the SS and remain, the fermentation is efficiently performed, and the dewatered cake 23 itself has a low water content, so that composting or the like is facilitated.
【００１７】以下、具体例を示す。表１に示した性状の
原料生ごみを酸発酵槽（容量約０．６ｍ3）で３７℃ま
たは５５℃、滞留時間２日間にて酸発酵させた後、メタ
ン発酵槽（容量約２．５ｍ 3）で５５℃にてメタン発酵
させ、発酵汚泥を無薬注脱水した。Hereinafter, specific examples will be described. The properties shown in Table 1
Raw garbage is converted to acid fermentation tank (capacity approx.Three) To 37 ° C
After acid fermentation at 55 ° C. and a residence time of 2 days,
Fermentation tank (capacity about 2.5m Three) At 55 ° C for methane fermentation
The fermented sludge was dewatered with no chemicals.
【００１８】生ごみ投入量を１３７ｋｇ／日とした時の
酸発酵状態は表２に示したようなものとなった。ただし
この時、発酵汚泥からの脱離液はＴＳ３〜４．５
（％）、アルカリ度約８０００〜１００００（ｍｇ／
Ｌ）であり、脱水ケーキの含水率は８０〜８５（％）と
なった。ＶＦＡはＣＯＤ（Ｃｒ）換算値である。The state of acid fermentation when the input amount of garbage was 137 kg / day was as shown in Table 2. However, at this time, the liquid desorbed from the fermented sludge was TS3 to 4.5.
(%), Alkalinity of about 8000 to 10,000 (mg /
L), and the water content of the dehydrated cake was 80 to 85 (%). VFA is a COD (Cr) converted value.
【００１９】また生ごみ投入量１７８ｋｇ／日、酸発酵
槽への脱離液返送率０．９３（ｋｇ／脱離液／ｋｇ生ご
み）、発酵汚泥ＴＳ５２０００（ｍｇ／Ｌ）とした時、
発生ガス量１２．３（ｍ3Ｎ／ｄ）、メタンガス濃度５
９．５（％）、ＴＳ分解率７９．０（％）、ＣＯＤ分解
率８０．２（％）となった。Further, when the garbage input amount is 178 kg / day, the rate of returning the desorbed liquid to the acid fermentation tank is 0.93 (kg / desorbed liquid / kg garbage), and the fermented sludge is TS52000 (mg / L),
Generated gas volume 12.3 (m 3 N / d), methane gas concentration 5
9.5 (%), TS decomposition rate was 79.0 (%), and COD decomposition rate was 80.2 (%).
【００２０】[0020]
【表１】 [Table 1]
【００２１】[0021]
【表２】 [Table 2]
【００２２】し尿、浄化槽汚泥などのスラッジ状有機性
廃棄物１については、除渣した後に造粒濃縮、ドラムス
クリーンなどで濃縮して液状分を水処理工程へ送り、濃
縮物をメタン発酵過程に導入して有機成分を回収するよ
うにしてもよい。For sludge-like organic waste 1 such as night soil and septic tank sludge, after removing the residue, it is concentrated by granulation and concentration, by a drum screen, etc., and the liquid content is sent to a water treatment process, and the concentrate is subjected to methane fermentation. The organic component may be recovered by introduction.
【００２３】水処理工程やメタン発酵工程で使用する膜
分離装置８，２６としては、管状セラミック膜や平板状
有機膜などの膜エレメントを配列した槽内浸漬型のもの
が、槽内に活性汚泥や発酵汚泥を維持でき、清澄な膜分
離水が得られるため好都合であるが、その他のタイプの
膜分離装置の使用も可能である。As the membrane separation devices 8 and 26 used in the water treatment process and the methane fermentation process, a immersion type in a tank in which membrane elements such as a tubular ceramic membrane and a flat organic membrane are arranged is used. This is advantageous because it can maintain the fermentation sludge and fermented sludge and obtain clear membrane separation water, but other types of membrane separation devices can be used.
【００２４】[0024]
【発明の効果】以上のように、本発明によれば、生ごみ
などの易分解性有機性廃棄物を酸発酵槽とメタン発酵槽
とに順次に送ってメタン発酵させるに際し、メタン発酵
槽において膜分離手段を利用するようにしたことによ
り、ＳＳ分の少ない液状分を抽出することができ、槽内
ＳＳ濃度を容易に調整できるとともに、抽出した液状分
を水処理工程へ送って処理できる。As described above, according to the present invention, when easily decomposable organic wastes such as garbage are sequentially sent to an acid fermentation tank and a methane fermentation tank for methane fermentation, the methane fermentation tank is used. By using the membrane separation means, it is possible to extract a liquid component having a small amount of SS, to easily adjust the SS concentration in the tank, and to send the extracted liquid component to a water treatment step for treatment.
【００２５】したがって、メタン発酵槽より引抜いた余
剰の発酵汚泥はポリマー、ｐＨ調整剤を用いることなく
脱水すればよく、汚泥中の砂分などを脱水ケーキ側に移
行させて系外へ排出できるとともに、汚泥より脱離した
ＳＳ濃度およびアルカリ度の高い脱水濾液を酸発酵槽に
返送することで酸発酵を促進することができ、それによ
りメタン発酵をも促進できる。ポリマー、ｐＨ調整剤が
不要な分、コストも削減できる。Therefore, the excess fermented sludge extracted from the methane fermentation tank may be dewatered without using a polymer and a pH adjuster, and the sand and the like in the sludge can be transferred to the dewatering cake side and discharged out of the system. The acid fermentation can be promoted by returning the dehydrated filtrate having high SS concentration and high alkalinity desorbed from the sludge to the acid fermentation tank, thereby also promoting methane fermentation. Since the polymer and the pH adjuster are unnecessary, the cost can be reduced.
【図１】本発明の一実施形態における有機性廃棄物の処
理方法を説明するフローチャートである。FIG. 1 is a flowchart illustrating a method for treating organic waste according to an embodiment of the present invention.
10 易分解性有機性廃棄物 16 酸発酵槽 19 メタン発酵槽 20 メタンガス 21 発酵汚泥 22 遠心脱水機 24 脱水濾液 26 膜分離装置 27 発酵液 10 easily decomposable organic waste 16 acid fermentation tank 19 methane fermentation tank 20 methane gas 21 fermentation sludge 22 centrifugal dehydrator 24 dehydration filtrate 26 membrane separator 27 fermentation liquid
───────────────────────────────────────────────────── フロントページの続き (72)発明者 柴田 敏行 大阪府大阪市浪速区敷津東一丁目２番47号 株式会社クボタ内 (72)発明者 間處 威俊 大阪府大阪市浪速区敷津東一丁目２番47号 株式会社クボタ内 (72)発明者 上野 将 大阪府大阪市浪速区敷津東一丁目２番47号 株式会社クボタ内 (72)発明者 添田 祐二 大阪府大阪市浪速区敷津東一丁目２番47号 株式会社クボタ内 Ｆターム(参考） 4D059 AA01 AA02 AA07 AA23 BA05 BA13 BA15 BA17 BA56 BE11 BE38 BE42 BE49 BE51 BK09 BK11 BK17 CA07 CA14 CC01 CC03 ──────────────────────────────────────────────────続 き Continuing from the front page (72) Inventor Toshiyuki Shibata 2-47, Shizitsuhigashi 1-chome, Namiwa-ku, Osaka-shi, Osaka (72) Inventor Taketoshi Majo Shikitsu, Naniwa-ku, Osaka-shi, Osaka 1-47 Higashi-Chome 2-47, Kubota Co., Ltd. (72) Inventor Masaru Ueno 1-2-47 Shikitsu Higashi, Naniwa-ku, Osaka, Osaka Prefecture (72) Inventor Yuji Soeda Nami-ku, Osaka, Osaka 1-47 Shishitsu Higashi 2-chome F-term in Kubota Corporation (reference) 4D059 AA01 AA02 AA07 AA23 BA05 BA13 BA15 BA17 BA56 BE11 BE38 BE42 BE49 BE51 BK09 BK11 BK17 CA07 CA14 CC01 CC03
Claims (1)
発酵槽とメタン発酵槽とに順次に送ってメタン発酵させ
るに際し、前記メタン発酵槽内の余剰の発酵汚泥を引抜
くとともに、槽内の発酵汚泥中の液状分を膜分離手段に
よって抽出することにより、メタン発酵槽内に適当濃度
の発酵汚泥を保持し、前記引抜いた発酵汚泥を無薬注に
て脱水手段で脱水し、脱水濾液を前記酸発酵槽へ返送す
ることにより、酸発酵槽内の酸発酵物を調質することを
特徴とする易分解性有機性廃棄物のメタン発酵方法。Claims: 1. When an easily decomposable organic waste such as garbage is sequentially sent to an acid fermentation tank and a methane fermentation tank for methane fermentation, while extracting excess fermentation sludge in the methane fermentation tank, By extracting the liquid component in the fermentation sludge in the tank by a membrane separation means, to hold the fermentation sludge of the appropriate concentration in the methane fermentation tank, dewater the extracted fermentation sludge by dehydration means with no chemical injection, A method for methane fermentation of easily decomposable organic waste, comprising refining an acid fermentation product in an acid fermentation tank by returning a dehydrated filtrate to the acid fermentation tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP10331823A JP2000153259A (en) | 1998-11-24 | 1998-11-24 | Methane fermentation method of easily degradable organic waste |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP10331823A JP2000153259A (en) | 1998-11-24 | 1998-11-24 | Methane fermentation method of easily degradable organic waste |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JP2000153259A true JP2000153259A (en) | 2000-06-06 |
Family
ID=18248049
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP10331823A Pending JP2000153259A (en) | 1998-11-24 | 1998-11-24 | Methane fermentation method of easily degradable organic waste |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2000153259A (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002336825A (en) * | 2001-05-17 | 2002-11-26 | Kubota Corp | Method for recycling organic waste |
| WO2003004423A1 (en) * | 2001-07-05 | 2003-01-16 | Nkk Corporation | Method of anaerobically treating organic material and anaerobic treatment apparatus |
| JP2003094021A (en) * | 2001-09-27 | 2003-04-02 | Shimizu Corp | Denitrification and methane fermentation system |
| GB2407088A (en) * | 2003-10-17 | 2005-04-20 | Christopher Paul Reynell | Anaerobic waste treatment process and apparatus |
| JP2007117948A (en) * | 2005-10-31 | 2007-05-17 | Ebara Corp | Method and apparatus for treating high-concentration organic waste liquid |
| JP2008029903A (en) * | 2006-07-26 | 2008-02-14 | Maezawa Ind Inc | Treatment apparatus of drainage and waste material |
| JP2011183393A (en) * | 2011-05-23 | 2011-09-22 | Mitsubishi Heavy Industries Environmental & Chemical Engineering Co Ltd | Apparatus for post-treatment of methane fermentation, system for post-treatment of methane fermentation, and method thereof |
| JP2011230100A (en) * | 2010-04-30 | 2011-11-17 | Osaka Prefecture | Method and apparatus for methane fermentation |
| JP2013013896A (en) * | 2012-09-20 | 2013-01-24 | Swing Corp | Anaerobiotic treatment method and device of organic waste |
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-
1998
- 1998-11-24 JP JP10331823A patent/JP2000153259A/en active Pending
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002336825A (en) * | 2001-05-17 | 2002-11-26 | Kubota Corp | Method for recycling organic waste |
| WO2003004423A1 (en) * | 2001-07-05 | 2003-01-16 | Nkk Corporation | Method of anaerobically treating organic material and anaerobic treatment apparatus |
| JP2003094021A (en) * | 2001-09-27 | 2003-04-02 | Shimizu Corp | Denitrification and methane fermentation system |
| JP4527325B2 (en) * | 2001-09-27 | 2010-08-18 | 清水建設株式会社 | Denitrification and methane fermentation equipment |
| GB2407088A (en) * | 2003-10-17 | 2005-04-20 | Christopher Paul Reynell | Anaerobic waste treatment process and apparatus |
| JP2007117948A (en) * | 2005-10-31 | 2007-05-17 | Ebara Corp | Method and apparatus for treating high-concentration organic waste liquid |
| JP4642635B2 (en) * | 2005-10-31 | 2011-03-02 | 荏原エンジニアリングサービス株式会社 | High concentration organic waste liquid treatment method and apparatus |
| JP2008029903A (en) * | 2006-07-26 | 2008-02-14 | Maezawa Ind Inc | Treatment apparatus of drainage and waste material |
| JP2011230100A (en) * | 2010-04-30 | 2011-11-17 | Osaka Prefecture | Method and apparatus for methane fermentation |
| JP2011183393A (en) * | 2011-05-23 | 2011-09-22 | Mitsubishi Heavy Industries Environmental & Chemical Engineering Co Ltd | Apparatus for post-treatment of methane fermentation, system for post-treatment of methane fermentation, and method thereof |
| JP2013176746A (en) * | 2012-02-29 | 2013-09-09 | Swing Corp | Treatment method and treatment device for organic wastewater |
| JP2013013896A (en) * | 2012-09-20 | 2013-01-24 | Swing Corp | Anaerobiotic treatment method and device of organic waste |
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