JPS62201697A - Anaerobic treatment of organic waste liquid - Google Patents
Anaerobic treatment of organic waste liquidInfo
- Publication number
- JPS62201697A JPS62201697A JP61043648A JP4364886A JPS62201697A JP S62201697 A JPS62201697 A JP S62201697A JP 61043648 A JP61043648 A JP 61043648A JP 4364886 A JP4364886 A JP 4364886A JP S62201697 A JPS62201697 A JP S62201697A
- Authority
- JP
- Japan
- Prior art keywords
- acid
- acetic acid
- carbon dioxide
- producing bacteria
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000007788 liquid Substances 0.000 title claims description 15
- 239000010815 organic waste Substances 0.000 title claims description 7
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims abstract description 120
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 64
- 239000002253 acid Substances 0.000 claims abstract description 58
- 239000007789 gas Substances 0.000 claims abstract description 58
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 52
- 241000894006 Bacteria Species 0.000 claims abstract description 50
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 26
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 26
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 22
- 235000014113 dietary fatty acids Nutrition 0.000 claims abstract description 8
- 229930195729 fatty acid Natural products 0.000 claims abstract description 8
- 239000000194 fatty acid Substances 0.000 claims abstract description 8
- 150000004665 fatty acids Chemical class 0.000 claims abstract description 8
- 230000001651 autotrophic effect Effects 0.000 claims abstract description 6
- 239000002002 slurry Substances 0.000 claims abstract description 4
- 239000002699 waste material Substances 0.000 claims abstract description 4
- 239000000126 substance Substances 0.000 claims abstract description 3
- 238000000034 method Methods 0.000 claims description 21
- 239000002994 raw material Substances 0.000 claims description 10
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 claims description 8
- 239000008103 glucose Substances 0.000 claims description 8
- 239000005416 organic matter Substances 0.000 claims description 6
- 229920000642 polymer Polymers 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims 1
- 230000029087 digestion Effects 0.000 abstract description 9
- 229910052739 hydrogen Inorganic materials 0.000 abstract 3
- 239000001257 hydrogen Substances 0.000 abstract 3
- 241000589220 Acetobacter Species 0.000 abstract 2
- 238000010438 heat treatment Methods 0.000 abstract 1
- 238000004519 manufacturing process Methods 0.000 description 28
- 238000000855 fermentation Methods 0.000 description 16
- 230000004151 fermentation Effects 0.000 description 16
- 238000006243 chemical reaction Methods 0.000 description 9
- 230000001580 bacterial effect Effects 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- 238000007796 conventional method Methods 0.000 description 3
- 238000010907 mechanical stirring Methods 0.000 description 3
- 230000000696 methanogenic effect Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Chemical compound CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 238000013019 agitation Methods 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 239000000758 substrate Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 241001468161 Acetobacterium Species 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 235000011389 fruit/vegetable juice Nutrition 0.000 description 1
- 230000023597 hemostasis Effects 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 230000002503 metabolic effect Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229920001592 potato starch Polymers 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000011550 stock solution Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Treatment Of Sludge (AREA)
Abstract
Description
【発明の詳細な説明】
主ｌ上生■且分肚
本発明は、有機性廃液を二相式嫌気性消化方法によって
処理方法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for treating organic wastewater by a two-phase anaerobic digestion method.
従来立伎血
二相式嫌気性消化方法は、酸生成槽に酸生成菌を、メタ
ン生成槽にメタン生成菌を各々主として存在させるか、
又は一つの槽内を主として酸生成菌が存在する酸生成部
と主としてメタン生成菌が存在するメタン生成部とに分
け、酸生成槽（又は酸生成部）では、主として有機物を
酸生成菌群によって脂肪酸及びアルコール等に転換する
酸生成反応を行い、メタン生成槽（又はメタン生成部）
では、酸生成槽（又は部）で得られた脂肪酸やアルコー
ルをメタン生成菌群によりメタンガスや炭酸ガスに分解
させるものである。即ち、二相式嫌気性消化方法は、２
つの反応を分離し、それぞれに適した条件下でそれぞれ
の菌体を効率良く増殖させ、菌体の基質代謝能力を最大
限に利用するものである。この方法によれば、酸生成反
応とメタン生成反応を同一槽内で行う方法より消化日数
が短縮され、メタンガス発生量が向上する。In the conventional two-phase anaerobic digestion method, acid-producing bacteria are mainly present in the acid-producing tank and methane-producing bacteria are mainly present in the methane-producing tank, or
Alternatively, one tank can be divided into an acid-producing section where acid-producing bacteria mainly exist and a methane-producing section where mainly methanogenic bacteria exist, and in the acid-producing tank (or acid-producing section), organic matter is mainly absorbed by the group of acid-producing bacteria. A methane generation tank (or methane generation section) that performs an acid generation reaction that converts into fatty acids and alcohol, etc.
In this method, fatty acids and alcohol obtained in an acid generation tank (or section) are decomposed into methane gas and carbon dioxide gas by a group of methane-producing bacteria. That is, the two-phase anaerobic digestion method consists of two
The method involves separating the two reactions, efficiently growing each bacterial cell under conditions suitable for each, and making the most of the substrate metabolic ability of the bacterial cell. According to this method, the number of days required for digestion is shortened and the amount of methane gas generated is improved compared to a method in which the acid production reaction and the methane production reaction are performed in the same tank.
（η′ し ゛と一° 口 占
しかしながら、酸生成槽から発生するガスはエネルギー
として用いるには、低発熱量であり、メタン生成槽から
発生するガスと比較して少量であるため、単独では使用
できない。そこで、メタン生成槽から発生するガスと混
合して回収しているのが現状である。However, the gas generated from the acid generation tank has a low calorific value to be used as energy, and the amount is small compared to the gas generated from the methane generation tank, so it cannot be used alone. It cannot be used, so currently it is collected by mixing it with the gas generated from the methane production tank.
このように、メタン生成槽から発生するガスに酸生成槽
から発生するガスを混合すると、ガスの発熱量を低下し
、エネルギーの価値を低めるという欠点を招来する。As described above, when the gas generated from the acid generation tank is mixed with the gas generated from the methane generation tank, the disadvantage is that the calorific value of the gas decreases and the value of energy decreases.
従って、本発明は、メタン生成槽から発生するガスの熱
量を保持し、酸生成槽から発生するガスをエネルギー価
値の高いものにしうる嫌気性消化方法を提供することを
目的とする。Therefore, an object of the present invention is to provide an anaerobic digestion method capable of retaining the calorific value of the gas generated from the methane generating tank and making the gas generated from the acid generating tank high in energy value.
。 占 、： るための
本発明は、有機性廃液を二相式嫌気性消化方法で処理す
る場合、酸生成槽から発生する水素ガスと炭酸ガスを独
立栄養細菌である酢酸生産菌と嫌気条件下で接触させる
ことにより、水素ガスと炭酸ガスを酢酸に変換すること
によって前記の問題点を解決したものである。. According to the present invention, when organic wastewater is treated by a two-phase anaerobic digestion method, hydrogen gas and carbon dioxide gas generated from an acid generation tank are combined with autotrophic acetic acid producing bacteria under anaerobic conditions. The above problem is solved by converting hydrogen gas and carbon dioxide gas into acetic acid by bringing them into contact with each other.
即ち、本発明方法は、有機性廃液と酸生成菌群とを嫌気
条件下で接触させ、酸生成菌群の作用により高分子物質
を低分子化すると共に、有機成分を揮発性脂肪酸に転換
する第一工程と、第一工程から発生する水素ガスと炭酸
ガスを回収し、これらのガスと独立栄養細菌である酢酸
生産菌群とを混合し、酢酸を生産する第二工程と、第一
工程から得られるスラリー及び第二工程から得られる酢
酸をメタン生成菌群と嫌気条件下に接触させ、メタン生
成菌の作用によりメタンガスと炭酸ガスを発生させる第
三工程からなることを予め調整する。That is, the method of the present invention brings organic waste liquid into contact with acid-producing bacteria under anaerobic conditions, and by the action of acid-producing bacteria, polymer substances are reduced in molecular weight, and organic components are converted into volatile fatty acids. A first step, a second step in which hydrogen gas and carbon dioxide gas generated from the first step are recovered, and these gases are mixed with a group of autotrophic acetic acid-producing bacteria to produce acetic acid, and a first step. The slurry obtained from step 1 and the acetic acid obtained from the second step are brought into contact with a group of methanogens under anaerobic conditions, and methane gas and carbon dioxide gas are generated by the action of the methanogens.
水素ガスと炭酸ガスから酢酸を生産する酢酸生産菌群と
しては、例えばアセトバクテリウム属菌（＾ｃｅｔｏｂ
ａｃｔｅｒｉｕ＋ａ）が知られている〔化学と工業、第
３８巻第４号１２３〜１２５頁（１９８５）参照〕。Examples of acetic acid-producing bacteria that produce acetic acid from hydrogen gas and carbon dioxide include Acetobacterium spp.
acteriu+a) [see Kagaku to Kogyo, Vol. 38, No. 4, pp. 123-125 (1985)].
酢酸生産菌が水素ガス共存下に炭酸ガスを炭素源として
酢酸を生成する反応は、基本的に２Ｃ０２＋４Ｈ２−一
→ＣＨ４Ｃ０ＯＨ＋２Ｈ２０で示される。この反応式か
ら、酸生成槽において酸生成菌の作用により有機成分を
分解する過程で発生するガスから酢酸を生成するには、
そのガス組成が炭酸ガス：水素ガス−１：２前後又は水
素ガスがそれより多いことが望ましい。The reaction in which an acetic acid-producing bacterium uses carbon dioxide gas as a carbon source in the presence of hydrogen gas to produce acetic acid is basically expressed as 2C02+4H2-1→CH4C0OH+2H20. From this reaction equation, in order to generate acetic acid from the gas generated during the process of decomposing organic components by the action of acid-producing bacteria in the acid-producing tank,
It is desirable that the gas composition be around 1:2 of carbon dioxide gas: hydrogen gas, or more hydrogen gas.
有機成分を低分子化して揮発性脂肪酸に転換する酸生成
反応において、水素ガスが生成される成分としては、分
解過程からまず糖分が考えられる。In the acid production reaction that reduces the molecular weight of organic components and converts them into volatile fatty acids, the component that generates hydrogen gas is thought to be sugar from the decomposition process.
そこで、グルコースのみを炭素源とする人工廃液を発酵
原液としてグルコース濃度を種々に変え、各々酸生成菌
と接触させ、酸生成反応を行い、その都度のガス組成を
測定した。その結果を第１図に示す。滞留日数にかかわ
らず、グルコース濃度が高い程、水素ガスの発生量が多
くなる傾向を示した。また、炭酸ガス：水素ガス＝１：
２となるグルコース濃度は７〜８％である。Therefore, an artificial waste solution containing only glucose as a carbon source was used as a fermentation stock solution with various glucose concentrations, brought into contact with acid-producing bacteria, an acid-producing reaction was carried out, and the gas composition was measured each time. The results are shown in FIG. Regardless of the number of days of residence, the higher the glucose concentration, the more hydrogen gas was generated. Also, carbon dioxide gas: hydrogen gas = 1:
The glucose concentration that becomes 2 is 7-8%.
この結果から、有機物をグルコース濃度とじて７％以上
、好ましくは８％以上含む有機性廃液を酸生成槽に供給
すれば、酸生成菌との接触により発生するガス組成を炭
酸ガスの容量ｌに対して水素ガスの容量２以上に保持し
うろことが判った。From this result, if an organic waste liquid containing 7% or more, preferably 8% or more of organic matter including the glucose concentration is supplied to the acid-producing tank, the gas composition generated by contact with acid-producing bacteria can be reduced to the volume of carbon dioxide gas (l). On the other hand, it was found that the hydrogen gas capacity should be maintained at 2 or more.
酢酸生産菌によって得られた酢酸は、メタン生成菌が利
用しやすい基質であり、メタン生成槽に供給され、メタ
ン生成菌の作用によりメタンガスと炭酸ガスに転換され
る。これにより、酸生成槽で発生する炭酸ガスと水素ガ
スを、酢酸を経てメタンガス及び炭酸ガスに転換でき、
メタン生成槽からのガス発生量を増加することができる
。Acetic acid obtained by acetic acid-producing bacteria is a substrate that can be easily used by methanogens, is supplied to a methanogen tank, and is converted into methane gas and carbon dioxide by the action of methanogens. This allows carbon dioxide and hydrogen gas generated in the acid generation tank to be converted into methane gas and carbon dioxide through acetic acid.
The amount of gas generated from the methane production tank can be increased.
次に、図面に基づいて本発明方法を詳述する。Next, the method of the present invention will be explained in detail based on the drawings.
第２図及び第３図はそれぞれ本発明の実施態様を示すフ
ローシートである。FIGS. 2 and 3 are flow sheets showing embodiments of the present invention, respectively.
第２図において、発酵原料である有機性廃液は必要に応
じて破砕した後、酸生成槽１内に供給され、酸生成菌と
接触する。供給前に、第３図に示したように、前処理槽
５において発酵成分の抽出、加水分解等の前処理を行っ
てもよい。そして、酸生成槽１を嫌気条件下で攪拌しな
がら水理学的滞留日数０．１〜３．０日保持する。酸生
成槽１内の温度は、５０〜６０℃、３４〜３７℃、又は
３３℃以下、ｐｉｆは５．０〜６．０であるのが最適で
ある。発酵原料中の有機成分は、酸生成菌の作用により
低分子化され、酢酸や酪酸等の揮発性脂肪酸及びアルコ
ール等に分解される。また、有機物の分解と並行して、
水素ガス及び炭酸ガスが発生する。In FIG. 2, organic waste liquid, which is a raw material for fermentation, is crushed if necessary and then supplied into an acid-producing tank 1, where it comes into contact with acid-producing bacteria. Before supplying, as shown in FIG. 3, pretreatment such as extraction and hydrolysis of fermentation components may be performed in a pretreatment tank 5. Then, the acid generation tank 1 is maintained under anaerobic conditions for a hydraulic retention period of 0.1 to 3.0 days while stirring. Optimally, the temperature in the acid generation tank 1 is 50 to 60°C, 34 to 37°C, or 33°C or less, and pif is 5.0 to 6.0. The organic components in the fermented raw materials are reduced in molecular weight by the action of acid-producing bacteria and decomposed into volatile fatty acids such as acetic acid and butyric acid, alcohol, and the like. In addition, in parallel with the decomposition of organic matter,
Hydrogen gas and carbon dioxide gas are generated.
酸生成菌と発酵原料との接触は、浮遊状態の酸生成菌と
発酵原料との機械攪拌、ガス攪拌する方法、球状、円柱
状又は多角形状の担体に酸生成菌を付着固定してガス攪
拌する方法、酸生成菌を多孔質無機担体の内、外部に固
定又は高分子ゲル内に固定して流動床又は固定床で接触
させる方法、板状、波板状、繊維状等、表面積の広い充
填材に酸生成菌を付着固定させ、固定床で接触させる方
法、又は、酸生成菌が棲息する汚泥自体を圧密して粒径
１〜２龍の粒状フロックを形成し、固定床で接触させる
方法で行うこともできる。Contact between acid-producing bacteria and fermentation raw materials can be achieved by mechanical stirring of suspended acid-producing bacteria and fermentation raw materials, gas agitation, or gas agitation with acid-producing bacteria attached and fixed on a spherical, cylindrical, or polygonal carrier. A method in which acid-producing bacteria are immobilized inside or outside a porous inorganic carrier or immobilized in a polymer gel and contacted in a fluidized bed or a fixed bed. A method of attaching and fixing acid-producing bacteria to a filler and contacting them in a fixed bed, or consolidating the sludge itself in which acid-producing bacteria live to form granular flocs with a particle size of 1 to 2 yen, and contacting them in a fixed bed. It can also be done by method.
酸生成槽１から発生した炭酸ガス及び水素ガスは、酢酸
生産槽２に供給され、酢酸生産菌と嫌気条件下で接触さ
せる。この気液混合を効率よ（するために、加圧等によ
って酢酸生産菌の培養液への気相の溶解を促進してもよ
い。酢酸生産槽２内の温度は、２０〜３０℃、ｐＨは６
．５〜７．５であるのが最適である。また、酢酸生産菌
の培養液の滞留時間は０．５〜３．０日とする。この条
件下で、独立栄養細菌である酢酸生産菌は、炭酸ガスと
水素ガスを利用して酢酸を生産する。Carbon dioxide and hydrogen gas generated from the acid production tank 1 are supplied to the acetic acid production tank 2 and brought into contact with acetic acid producing bacteria under anaerobic conditions. In order to make this gas-liquid mixing efficient, the dissolution of the gas phase into the culture solution of the acetic acid producing bacteria may be promoted by applying pressure or the like. is 6
．． Optimally, it is between 5 and 7.5. Further, the residence time of the culture solution of the acetic acid-producing bacteria is 0.5 to 3.0 days. Under these conditions, acetic acid-producing bacteria, which are autotrophic bacteria, produce acetic acid using carbon dioxide and hydrogen gas.
生産された酢酸は、酢酸生産菌の培養液とともに系外に
出され、第３図に示したように、酢酸生産槽２内の菌体
を多量に保持するため固液分離槽６を設けて菌体と分離
してもよい。また、酢酸生産槽２内の菌体を多量に保持
するために、酢酸生産菌を担体に固定してもよい。The produced acetic acid is taken out of the system together with the culture solution of the acetic acid producing bacteria, and as shown in FIG. It may be separated from the bacterial body. Furthermore, in order to maintain a large amount of bacterial cells in the acetic acid production tank 2, the acetic acid producing bacteria may be immobilized on a carrier.
酢酸生産槽２で生産された酢酸と酸生成槽１内で酸生成
反応を終えた発酵原料は、メタン生成槽３に供給される
。メタン生成槽３に供給する前に、第３図に示したよう
に、沈澱槽７において酸生成発酵液と未酸生成発酵残渣
とに分離し、未酸生成発酵残渣は酸生成槽１に返送して
もよい。The acetic acid produced in the acetic acid production tank 2 and the fermentation raw material that has undergone the acid production reaction in the acid production tank 1 are supplied to the methane production tank 3. Before being supplied to the methane production tank 3, as shown in FIG. 3, the acid production fermentation liquid and the non-acid production fermentation residue are separated in the settling tank 7, and the non-acid production fermentation residue is returned to the acid production tank 1. You may.
メタン生成槽３内では、酸生成発酵液をメタン生成菌と
固定床又は流動床で嫌気条件下に接触又は混合しながら
１〜１５日保持する。混合には、ガス攪拌、機械攪拌等
を適用することができる。In the methanogenic tank 3, the acid-producing fermentation liquid is kept in contact with or mixed with methanogenic bacteria in a fixed bed or a fluidized bed for 1 to 15 days under anaerobic conditions. For mixing, gas stirring, mechanical stirring, etc. can be applied.
メタン生成槽３内の温度は５０〜６０℃、３４〜３７℃
、３３“Ｃ以下、ｐＨは６．８〜８．０であるのが最適
である。The temperature inside the methane generation tank 3 is 50-60℃, 34-37℃
, 33"C or less, and the pH is optimally between 6.8 and 8.0.
酢酸生産菌により炭酸ガスと水素ガスから生産された酢
酸と、酸生成菌により低分子化され、揮発性脂肪酸等の
液状まで分解された発酵原料は、メタン生成槽３内のメ
タン生成菌と接触し、その作用により液状からガス状に
分解され、メタンガスと炭酸ガスが発生する。発生した
ガスはガスホルダ４に貯留される。メタン生成槽３内か
ら排出されるスラリーは別途処理される。Acetic acid produced from carbon dioxide and hydrogen gas by the acetic acid-producing bacteria, and fermentation raw materials that have been reduced in molecular weight by the acid-producing bacteria and decomposed into liquids such as volatile fatty acids, come into contact with the methane-producing bacteria in the methane-producing tank 3. However, due to this action, the liquid state is decomposed into the gas state, and methane gas and carbon dioxide gas are generated. The generated gas is stored in the gas holder 4. Slurry discharged from the methane generation tank 3 is treated separately.
裏止血
次に、実施例に基づいて本発明を詳述するが、本発明は
これに限定されるものではない。Back hemostasis Next, the present invention will be described in detail based on Examples, but the present invention is not limited thereto.
実施例１
バレイショデンブンを回収する際に発生する汁液を発酵
原料として第２図に示したフローシートに従うて嫌気性
消化した。発酵原料は有機物濃度２．５％、有機物光た
りの糖分（グルコースとして）４５％の性状であった。Example 1 The juice generated when collecting potato starch was used as a fermentation raw material and was subjected to anaerobic digestion according to the flow sheet shown in FIG. The fermentation raw material had an organic matter concentration of 2.5% and an organic matter content of 45% sugar (as glucose).
酸生成槽１には、発酵温度５３℃、ｐｕｓ、ｓ〜６．０
で嫌気条件下で十分馴養した浮遊状態の酸生成菌を保持
しておいた。酢酸生産槽２内には、温度３０℃、ｐＨ７
，０で嫌気条件下に維持し、良好な酸生産菌を保持した
。また、メタン生成槽３内には、発酵温度５３℃、ｐＨ
７，２〜７．５で嫌気条件下で十分馴養した浮遊状態の
メタン生成菌を保持した。Acid generation tank 1 has a fermentation temperature of 53°C, pus, s ~ 6.0
Acid-producing bacteria that were sufficiently acclimated under anaerobic conditions were maintained in suspension. Inside the acetic acid production tank 2, the temperature is 30°C and the pH is 7.
, 0 to maintain good acid-producing bacteria under anaerobic conditions. In addition, the methane generation tank 3 has a fermentation temperature of 53°C and a pH of 53°C.
7.2 to 7.5, the methanogens in a suspended state that were sufficiently acclimatized under anaerobic conditions were retained.
酸生成槽１、酢酸生産槽２及びメタン生成槽３における
菌群と供給原料との接触は、攪拌羽根を利用して機械攪
拌によって行った。なお、酢酸生産槽２内の壁に邪魔板
を設け、気液混合が激しく起こるようにした。The bacteria in the acid production tank 1, the acetic acid production tank 2, and the methane production tank 3 were brought into contact with the feedstock by mechanical stirring using a stirring blade. Note that a baffle plate was provided on the wall inside the acetic acid production tank 2 so that gas-liquid mixing occurred vigorously.
上記条件下で、発酵原料の滞留時間を、酸生成槽１では
０．５日、酢酸生産槽２では３日、メタン生成槽３では
５日間として処理を行った。結果を下記の表に示す。Under the above conditions, the treatment was carried out with the residence time of the fermentation raw material being 0.5 days in the acid production tank 1, 3 days in the acetic acid production tank 2, and 5 days in the methane production tank 3. The results are shown in the table below.
なお、比較のため、酸生成槽から得られる炭酸ガスと水
素ガスを酢酸生産菌群と接触させず、メタン生成槽３か
ら発生するガスと一緒に回収する従来法を実施し、その
結果も下記の表に示す。For comparison, we conducted a conventional method in which carbon dioxide and hydrogen gas obtained from the acid production tank were not brought into contact with the acetic acid production bacteria group, and were recovered together with the gas generated from methane production tank 3. The results are also shown below. It is shown in the table below.
表に示した結果から明らかなとおり、本発明によれば、
ガス発生量及び発生ガス中の可燃性ガスが占める割合が
、従来法に比較して著しく条い。As is clear from the results shown in the table, according to the present invention,
The amount of gas generated and the proportion of flammable gas in the generated gas are significantly lower than with conventional methods.
光所圓凱果
本発明によれば、酸生成槽で発生するガスを可燃性ガス
に転換しうるので、全発生ガス中の可燃性ガスの割合が
著しく高くなり、嫌気性消化法によって発生するガスの
高エネルギー化が可能になる。また、ガス発生量を従来
より増加させることができる。According to the present invention, the gas generated in the acid generation tank can be converted into flammable gas, so the proportion of flammable gas in the total gas generated is significantly increased, and the gas generated by anaerobic digestion is significantly increased. It becomes possible to increase the energy of gas. Further, the amount of gas generated can be increased compared to the conventional method.
第１図はグルコース濃度と酸生成菌による水素ガス及び
炭酸、ガスの発生量との関係図、第２図は本発明方法の
一実施態様を示すフローシート、第３図は本発明方法の
別の実施態様を示すフローシートである。Fig. 1 is a diagram showing the relationship between glucose concentration and the amount of hydrogen gas, carbon dioxide, and gas generated by acid-producing bacteria, Fig. 2 is a flow sheet showing one embodiment of the method of the present invention, and Fig. 3 is another example of the method of the present invention. 1 is a flow sheet showing an embodiment of the present invention.
Claims (2)
せ、酸生成菌群の作用により高分子物質を低分子化する
と共に、有機成分を揮発性脂肪酸に転換する第一工程と
、第一工程から発生する水素ガスと炭酸ガスを回収し、
これらのガスと独立栄養細菌である酢酸生産菌群とを混
合し、酢酸を生産する第二工程と、第一工程から得られ
るスラリー及び第二工程から得られる酢酸をメタン生成
菌群と嫌気条件下に接触させ、メタン生成菌の作用によ
りメタンガスと炭酸ガスを発生させる第三工程からなる
ことを特徴とする有機性廃液の嫌気性処理方法。(1) A first step in which organic waste liquid and acid-producing bacteria are brought into contact with each other under anaerobic conditions, and by the action of the acid-producing bacteria, polymer substances are reduced in molecular weight, and organic components are converted into volatile fatty acids. , recover hydrogen gas and carbon dioxide gas generated from the first step,
A second step in which these gases are mixed with acetic acid-producing bacteria, which are autotrophic bacteria, to produce acetic acid, and a slurry obtained from the first step and acetic acid obtained from the second step are mixed with a group of methanogen-producing bacteria under anaerobic conditions. A method for anaerobic treatment of organic waste liquid, characterized by comprising a third step of bringing the organic waste into contact with the liquid under water and generating methane gas and carbon dioxide gas through the action of methane-producing bacteria.
有するように原料廃液を予め調整する特許請求の範囲第
１項記載の処理方法。(2) The treatment method according to claim 1, wherein the raw waste liquid is adjusted in advance so that the raw material waste liquid contains 7% or more of sugar based on the organic matter as glucose.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61043648A JPS62201697A (en) | 1986-02-28 | 1986-02-28 | Anaerobic treatment of organic waste liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61043648A JPS62201697A (en) | 1986-02-28 | 1986-02-28 | Anaerobic treatment of organic waste liquid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS62201697A true JPS62201697A (en) | 1987-09-05 |
Family
ID=12669682
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61043648A Pending JPS62201697A (en) | 1986-02-28 | 1986-02-28 | Anaerobic treatment of organic waste liquid |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS62201697A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7617756B2 (en) | 2004-04-14 | 2009-11-17 | Makoto Noguchi, et al. | Index cutter |
| CN113716688A (en) * | 2021-10-08 | 2021-11-30 | 合肥工业大学 | Anaerobic treatment method for coal chemical industry wastewater |
| JP2022515625A (en) * | 2018-12-26 | 2022-02-21 | オレージュ | Improved methods and equipment for anaerobic digestion |
-
1986
- 1986-02-28 JP JP61043648A patent/JPS62201697A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7617756B2 (en) | 2004-04-14 | 2009-11-17 | Makoto Noguchi, et al. | Index cutter |
| JP2022515625A (en) * | 2018-12-26 | 2022-02-21 | オレージュ | Improved methods and equipment for anaerobic digestion |
| CN113716688A (en) * | 2021-10-08 | 2021-11-30 | 合肥工业大学 | Anaerobic treatment method for coal chemical industry wastewater |
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