JPH03238091A - Methane fermentation - Google Patents
Methane fermentationInfo
- Publication number
- JPH03238091A JPH03238091A JP2032347A JP3234790A JPH03238091A JP H03238091 A JPH03238091 A JP H03238091A JP 2032347 A JP2032347 A JP 2032347A JP 3234790 A JP3234790 A JP 3234790A JP H03238091 A JPH03238091 A JP H03238091A
- Authority
- JP
- Japan
- Prior art keywords
- acid fermentation
- acid
- water
- tank
- fermentation tank
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000000855 fermentation Methods 0.000 title claims abstract description 109
- 230000004151 fermentation Effects 0.000 title claims abstract description 109
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 96
- 239000002253 acid Substances 0.000 claims abstract description 76
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 69
- 239000002351 wastewater Substances 0.000 claims abstract description 28
- 239000007788 liquid Substances 0.000 claims abstract description 19
- 238000000034 method Methods 0.000 claims abstract description 19
- 238000000926 separation method Methods 0.000 claims abstract description 9
- 235000014113 dietary fatty acids Nutrition 0.000 claims description 6
- 229930195729 fatty acid Natural products 0.000 claims description 6
- 239000000194 fatty acid Substances 0.000 claims description 6
- 150000004665 fatty acids Chemical class 0.000 claims description 6
- 239000005416 organic matter Substances 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 4
- 150000001875 compounds Chemical class 0.000 claims 1
- 241000894006 Bacteria Species 0.000 abstract description 5
- 238000004134 energy conservation Methods 0.000 abstract 1
- 230000000717 retained effect Effects 0.000 abstract 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 12
- 239000010802 sludge Substances 0.000 description 12
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 6
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 4
- 238000002347 injection Methods 0.000 description 4
- 239000007924 injection Substances 0.000 description 4
- 102000004169 proteins and genes Human genes 0.000 description 4
- 108090000623 proteins and genes Proteins 0.000 description 4
- 235000011121 sodium hydroxide Nutrition 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000010979 pH adjustment Methods 0.000 description 3
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Chemical compound CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 description 2
- 235000013405 beer Nutrition 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 150000002632 lipids Chemical class 0.000 description 2
- 150000003384 small molecules Chemical class 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- NQPDZGIKBAWPEJ-UHFFFAOYSA-N valeric acid Chemical compound CCCCC(O)=O NQPDZGIKBAWPEJ-UHFFFAOYSA-N 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 1
- 241000209140 Triticum Species 0.000 description 1
- 235000021307 Triticum Nutrition 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229920001222 biopolymer Polymers 0.000 description 1
- 150000001720 carbohydrates Chemical class 0.000 description 1
- 235000014633 carbohydrates Nutrition 0.000 description 1
- 229920006317 cationic polymer Polymers 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005188 flotation Methods 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- OOYGSFOGFJDDHP-KMCOLRRFSA-N kanamycin A sulfate Chemical group OS(O)(=O)=O.O[C@@H]1[C@@H](O)[C@H](O)[C@@H](CN)O[C@@H]1O[C@H]1[C@H](O)[C@@H](O[C@@H]2[C@@H]([C@@H](N)[C@H](O)[C@@H](CO)O2)O)[C@H](N)C[C@@H]1N OOYGSFOGFJDDHP-KMCOLRRFSA-N 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 235000019260 propionic acid Nutrition 0.000 description 1
- IUVKMZGDUIUOCP-BTNSXGMBSA-N quinbolone Chemical compound O([C@H]1CC[C@H]2[C@H]3[C@@H]([C@]4(C=CC(=O)C=C4CC3)C)CC[C@@]21C)C1=CCCC1 IUVKMZGDUIUOCP-BTNSXGMBSA-N 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 229940005605 valeric acid Drugs 0.000 description 1
- 239000002699 waste material 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】
〔産業上の利用分野〕
本発明は食品、化学、紙バルプ工業等より排出される有
機性廃水を対象としたメタン発酵処理法に関するもので
ある。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention relates to a methane fermentation treatment method for organic wastewater discharged from food, chemical, pulp and paper industries, etc.
近年、メタン菌を高濃度に維持し高負荷処理を可能とし
たりアクタ−の開発が盛んであり、メタン発酵処理が注
目されている。In recent years, there has been active development of actors that maintain methane bacteria at a high concentration and enable high-load processing, and methane fermentation processing is attracting attention.
メタン発酵処理を行う場合、廃水の性状ＩＩ！１１ら廃
水中に含まれる有機物の形態が重要な因子となる。When performing methane fermentation treatment, properties of wastewater II! 11 The form of organic matter contained in wastewater is an important factor.
有機酸、アルコール、等の有機物は容易にメタン発酵処
理可能である。しかしながら、蛋白質、脂質等の有機物
を多く含む廃水のメタン発酵処理においては、酸発酵処
理が律速となるためメタン発酵槽の前段に酸発酵槽を設
けた二相処理法を適用する必要がある（第３図参照）。Organic substances such as organic acids and alcohols can be easily subjected to methane fermentation treatment. However, in the methane fermentation treatment of wastewater containing a large amount of organic matter such as proteins and lipids, acid fermentation treatment becomes rate-limiting, so it is necessary to apply a two-phase treatment method in which an acid fermentation tank is installed before the methane fermentation tank ( (See Figure 3).
ところが、実際の処理設備では酸発酵槽を特別に設ける
ケースは少なく、調整槽を兼用する場合が多い。これは
調整槽において、液滞留時間を１〜２日間とるために酸
発酵が進行するためである。However, in actual treatment facilities, there are few cases in which a special acid fermentation tank is provided, and the acid fermentation tank is often used also as a regulating tank. This is because the acid fermentation proceeds in the adjustment tank to allow the liquid residence time of 1 to 2 days.
しかしながら、このような場合は溶解性の炭水化物、蛋
白質等を主に含む廃水であり、ＳＳを多く含む廃水では
不十分である。However, in such cases, wastewater mainly contains soluble carbohydrates, proteins, etc., and wastewater containing a large amount of SS is insufficient.
この原因としては、調整槽内の反応条件（ｐ）Ｉ、水温
、酸生成菌量、液滞留時間等）を一定に保つことが出来
ないためである。This is because the reaction conditions (p)I, water temperature, amount of acid-producing bacteria, liquid residence time, etc. in the adjustment tank cannot be kept constant.
また、ＳＳを多く含む廃水では、酸発酵処理後でも処理
水中にＳＳが多く含まれるため、そのままの状態でメタ
ン発酵槽〔上向流嫌気性汚泥床法（Ｕｐｆｌｏｗ Ａｎ
ａｅｒｏｂｉｃ Ｓｌｕｄｇｅ Ｂｌａｎｋｅｔ Ｐｒ
ｏｃｅｓｓ）以後ＵＡＳＢと記す。固定床等〕に通水す
るとＵＡＳＢでは、スラッジベツド部でＳＳの蓄積が起
こり、グラニユール汚泥と共にスカムとなり系外に流出
することがしばしばある。一方、固定床法では濾材間に
ＳＳの蓄積が多くなり、濾材閉塞が生じ、処理効率が低
下することが多くなる。また、調整槽の他に酸発酵槽を
別途に設けると付帯設備が多くなり、全体設備配置も大
きなものとなり高速メタン発酵処理のメリットが少なく
なる。In addition, wastewater containing a large amount of SS contains a large amount of SS even after acid fermentation treatment, so it is necessary to use a methane fermentation tank [upflow anaerobic sludge bed method] without any treatment.
aerobic Sludge Blanket Pr
(occess) hereinafter referred to as UASB. In UASB, when water is passed through a fixed bed, etc., SS accumulates in the sludge bed, and often forms scum with granule sludge and flows out of the system. On the other hand, in the fixed bed method, a large amount of SS accumulates between filter media, resulting in filter media clogging, which often reduces treatment efficiency. Further, if an acid fermentation tank is provided separately in addition to the adjustment tank, the number of incidental equipment increases, the overall equipment layout becomes large, and the merits of high-speed methane fermentation treatment are reduced.
以上のように従来技術では二相処理を実際的なレベルで
効率的におこなった例はほとんどないと言える。As described above, it can be said that there are almost no examples of two-phase processing being efficiently performed on a practical level in the prior art.
本発明の目的は、上記従来技術の欠点を解消し、酸性発
酵が必要で且つ特に、蛋白質等の生体高分子およびＳＳ
量の大きな廃水系の処理において処理効率および装置の
コンパクト性を改善したメタン発酵処理方法を提供する
ことにある。The purpose of the present invention is to eliminate the drawbacks of the above-mentioned prior art, which require acidic fermentation, and in particular, to solve the problems of biopolymers such as proteins and SS.
It is an object of the present invention to provide a methane fermentation treatment method that improves treatment efficiency and compactness of equipment in treating a large amount of wastewater.
［課題を解決するための手段］
本発明は、廃水を酸発酵槽に供給し、該廃水に含有され
る有機物を酸発酵することにより少なくとも低級脂肪酸
を含む低分子化合物を生成せしめた後に酸発酵処理水を
メタン発酵槽に導入してメタン発酵を行う処理法におい
て、酸発酵槽有効量の一部相当量の該酸発酵処理水を酸
発酵槽槽内に残し、該酸発酵処理水の残部を遠心分離し
て固形分と分離水に固液分離し、該分離水をメタン発酵
槽内に供給し、メタン発酵を行うメタン発酵処理方法で
あり、これにより上記目的を達成することができる。[Means for Solving the Problems] The present invention provides wastewater to an acid fermenter, organic matter contained in the wastewater to acid fermentation to produce low molecular weight compounds containing at least lower fatty acids, and then acid fermentation. In a treatment method in which treated water is introduced into a methane fermentation tank to perform methane fermentation, an amount of the acid fermentation treated water corresponding to a part of the effective amount of the acid fermentation tank is left in the acid fermentation tank, and the remainder of the acid fermentation treated water is This is a methane fermentation treatment method in which methane fermentation is performed by centrifuging to separate solids into solids and separated water, and then supplying the separated water into a methane fermentation tank to carry out methane fermentation, thereby achieving the above object.
また、本発明における好まし態様としては、該固液分離
される該酸発酵処理水の量と同程度の量の廃水が酸発酵
槽に供給されることである。Further, in a preferred embodiment of the present invention, an amount of wastewater comparable to the amount of the acid fermentation treated water to be subjected to solid-liquid separation is supplied to the acid fermenter.
例えば、酸発酵槽有効量の３０〜７０％相当量の酸発酵
処理水、即ち、酸発酵混合液（蛋白質、脂質等の発酵処
理前の廃水含有物、及び、アルコール、低級脂肪酸等の
発酵により生成した低分子化合物、ＢＯＤ 、 ＳＳ等
からなる液）を酸発酵槽内に残し、残りの７０〜３０％
の酸発酵混合液を遠心分離し、分離水をメタン発酵槽に
供給するものである。For example, an amount of acid fermentation-treated water equivalent to 30 to 70% of the effective amount of the acid fermenter, that is, an acid fermentation mixture (wastewater content before fermentation such as proteins and lipids, and fermentation of alcohol, lower fatty acids, etc.) The remaining 70-30% of the produced liquid (consisting of low molecular weight compounds, BOD, SS, etc.) is left in the acid fermenter.
The acid fermentation mixture is centrifuged and the separated water is supplied to the methane fermentation tank.
本発明において、廃水の酸発酵槽への供給と酸発酵槽か
ら固液分離工程さらにはメタン発酵工程への処理水の流
出・流入のタイ累ングの制？ｆｆ１ｌは、上記条件を満
足するならば特に限定されることはなく、自動的、半自
動的、手動的に制御され得る。また、廃水の酸発酵処理
工程、固液分離工程、メタン発酵処理工程の各処理工程
への廃液および各処理液の移動は連続的、回分的、半回
分的のいずれでも良い。In the present invention, it is possible to control the tie-up of the supply of wastewater to the acid fermentation tank and the outflow/inflow of treated water from the acid fermentation tank to the solid-liquid separation process and further to the methane fermentation process. ff1l is not particularly limited as long as it satisfies the above conditions, and can be controlled automatically, semi-automatically, or manually. Further, the waste liquid and each treatment liquid may be transferred to each of the acid fermentation treatment process, solid-liquid separation process, and methane fermentation treatment process continuously, batchwise, or semi-batchwise.
特に、本発明において好ましい態様は、該固液分離され
る該酸発酵処理水の量と同程度の量の廃水が酸発酵槽に
供給されることである。この場合、酸発酵処理水の流出
と廃水の酸発酵槽への流入のタイピングを一致させるこ
とが好ましい。In particular, a preferred embodiment of the present invention is that the same amount of wastewater as the amount of the acid fermentation treated water to be subjected to solid-liquid separation is supplied to the acid fermenter. In this case, it is preferable to match the type of outflow of the acid fermentation treated water and the inflow of waste water into the acid fermenter.
このための手段として、例えば、酸発酵槽の液位レベル
を検知することによりポンプのオン・オフ（ｏｎ−ｏｆ
ｆ）運転を行うことが挙げられる。As a means for this purpose, for example, the pump can be turned on and off by detecting the liquid level in the acid fermenter.
f) Driving.
酸発酵槽内の酸発酵処理水混合液は好ましくは少なくと
も３０％以上、特に好ましくは５０％〜６０％を残すこ
とで酸生成菌の維持ならびに酸発酵処理の安定化を行い
、さらに酸発酵槽内ｐ＋＋を好ましくは、４．５〜６．
０に調整を行い、酸発酵処理の安定化を計ることができ
る。そのため、例えば、酸発酵槽内へのアルカリ、例え
ば、苛性ソーダ等の添加あるいはメタン発酵処理水の循
環等により調整することができる。また、槽内は水中攪
拌機等にて混合攪拌するのがよい。The acid fermentation treated water mixture in the acid fermentation tank is preferably at least 30% or more, particularly preferably 50% to 60%, to maintain acid-producing bacteria and stabilize the acid fermentation treatment. The inner p++ is preferably 4.5 to 6.
It is possible to stabilize the acid fermentation treatment by adjusting the temperature to 0. Therefore, it can be adjusted, for example, by adding an alkali, such as caustic soda, into the acid fermentation tank or by circulating methane fermentation treated water. In addition, it is preferable to mix and stir the inside of the tank using an underwater stirrer or the like.
特に、本発明が好適な処理系は、酸発酵槽への流入廃水
のＳＳ濃度が１０．０００ｍｇ／ １２以上ある場合で
ある。この場合、酸発酵処理水のＳＳ濃度は、５，００
０ｍｇ／４２以上になる場合が多く、また、酸発酵処理
水中には酢酸、プロピオン酸、酪酸、吉草酸等の揮発性
低級脂肪酸が多く含まれているため、酸発酵処理水は強
い臭気を放つものである。In particular, the present invention is suitable for a treatment system in which the SS concentration in the wastewater flowing into the acid fermenter is 10.000 mg/12 or more. In this case, the SS concentration of the acid fermentation treated water is 5,00
In many cases, the concentration is 0 mg/42 or more, and since the acid fermentation treated water contains a lot of volatile lower fatty acids such as acetic acid, propionic acid, butyric acid, and valeric acid, the acid fermentation treated water has a strong odor. It is something.
しかして、本発明では酸発酵処理水を遠心分離し、過剰
のＳＳを除去して分離水のＳＳ濃度を数千ｍｇ／ｌに低
減せしめることによりメタン発酵槽における処理効率を
改善すると共に該臭気を効果的に除去するものである。Therefore, in the present invention, the acid fermentation treated water is centrifuged to remove excess SS and reduce the SS concentration in the separated water to several thousand mg/l, thereby improving the treatment efficiency in the methane fermentation tank and eliminating the odor. This effectively removes the
また、該固液分離された分離水は、メタン発酵槽流入前
に好ましくはｐＨを６．５前後に、アルカリあるいは、
該メタン発酵処理水を添加することにより調整すること
が好ましい。In addition, the separated water subjected to the solid-liquid separation is preferably adjusted to a pH of around 6.5 before flowing into the methane fermentation tank, and then adjusted to an alkaline or
It is preferable to adjust by adding the methane fermentation treated water.
本発明によってメタン発酵処理された廃水は、所要によ
り更に別途設けられた処理工程、例えば、活性汚泥処理
、凝集沈澱処理、加圧浮上処理等に供され、基準の清澄
な処理水として放流される。The wastewater subjected to the methane fermentation treatment according to the present invention is further subjected to separate treatment steps as required, such as activated sludge treatment, coagulation sedimentation treatment, pressure flotation treatment, etc., and is discharged as standard clear treated water. .
以下、本発明の実施例を添付図面（第１図）に基づいて
説明する。尚、本発明はこの実施例に限定されることは
なく当業者にできる種々の置き換え等の変更を包含する
。Embodiments of the present invention will be described below with reference to the accompanying drawings (FIG. 1). It should be noted that the present invention is not limited to this embodiment, but includes various substitutions and changes that can be made by those skilled in the art.
原水１８が酸発酵槽８に流入する。槽液位レベルは液位
レヘル計により表示され、酸発酵槽内の混合液量が槽有
効容量の３０％〜７０％、好ましくは５０％〜６０％に
なると、供給ポンプ１３により遠心脱水機１０に酸発酵
処理水１９が供給される。Raw water 18 flows into acid fermenter 8 . The tank liquid level is displayed by a liquid level gauge, and when the amount of mixed liquid in the acid fermentation tank reaches 30% to 70%, preferably 50% to 60% of the tank effective capacity, the centrifugal dehydrator 10 is activated by the supply pump 13. Acid fermentation treated water 19 is supplied to the tank.
酸発酵槽内は苛性ソーダ注入設備１６、あるいはメタン
発酵処理水２４を循環することでｐＨを４゜５〜６．０
好ましくはｐＨ・５．０〜５．５に調整する。また、蒸
気加温設置Ｊ！２９により槽内湯度は３５〜４０″Ｃに
制御する。また、酸発酵槽内では水中攪拌機３１により
汚泥を混合する。Inside the acid fermentation tank, the pH is maintained at 4°5 to 6.0 by circulating the caustic soda injection equipment 16 or the methane fermentation treated water 24.
Preferably, the pH is adjusted to 5.0 to 5.5. Also, steam heating installation J! 29 to control the hot water temperature in the tank to 35 to 40''C. In addition, in the acid fermentation tank, sludge is mixed by an underwater agitator 31.
酸発酵処理水１９は供給ポンプ１３により遠心脱水機１
０に供給され、遠心分離される。分離水２１はｐｉ調整
槽１１に供給される。酸発酵処理水１９のＳＳ濃度が１
０，０００ｍｇ＃２以上と高い場合は、遠心脱水機１０
の前でポリマー注入設備２０によりカチオン系ポリマー
の添加を行う。添加量は酸発酵処理水対ＳＳ当たり０．
５〜１χ程度で良い。脱水ケーキ２２は活性汚泥膜（Ｉ
ｌｉｉ２Ｂに供給され、安定化処理され余剰汚泥と共に
系外に排出される。また、酸発酵槽内のＭＬＳＳＩ度が
低い場合は（ＭＬＳＳ＜５０００ｍｇ／ ｌ ） 、脱
水ケーキの一部は酸発酵槽に戻される。The acid fermentation treated water 19 is sent to the centrifugal dehydrator 1 by the supply pump 13.
0 and centrifuged. The separated water 21 is supplied to the pi adjustment tank 11. SS concentration of acid fermentation treated water 19 is 1
If it is high (0,000mg #2 or more), use a centrifugal dehydrator 10
The cationic polymer is added by the polymer injection equipment 20 in front of. The amount added is 0.0% per SS to acid fermentation treated water.
Approximately 5 to 1χ is sufficient. The dewatered cake 22 is an activated sludge membrane (I
The sludge is supplied to lii2B, stabilized, and discharged from the system together with excess sludge. Also, if the MLSSI degree in the acid fermenter is low (MLSS<5000 mg/l), a part of the dehydrated cake is returned to the acid fermenter.
ｐＨ調整槽１１にて分離水２１は、苛性ソーダ注入設置
ｉ’１１７、あるいはメタン発酵処理水を循環水２６と
して利用することによりｐＨ＝６．５前後に調整される
。蒸気加温設備２９により水温を３５〜４０°Ｃに調整
する。In the pH adjustment tank 11, the pH of the separated water 21 is adjusted to around 6.5 by using caustic soda injection installation i'117 or by using methane fermentation treated water as the circulating water 26. The water temperature is adjusted to 35-40°C using steam heating equipment 29.
メタン発酵原水２３は供給ポンプ１４によりメタン発酵
槽９に供給される。メタン発酵槽９では酢酸等の揮発性
低級脂肪酸は、メタン菌により処理されメタンを７０〜
８０χ含む発生ガス２７が生成され、発生ガスは、通常
ボイラーで燃焼し、蒸気に変換し熱源（主にプラント加
温用。）として有効利用される。また、余ったガスは、
余剰ガス燃焼装置で燃やす。メタン発酵槽９はＵＡＳＢ
法、固定床法、流動床が適用できる。The methane fermentation raw water 23 is supplied to the methane fermentation tank 9 by the supply pump 14 . In the methane fermentation tank 9, volatile lower fatty acids such as acetic acid are processed by methane bacteria and methane is
Generated gas 27 containing 80χ is generated, and the generated gas is usually combusted in a boiler, converted to steam, and effectively used as a heat source (mainly for heating the plant). In addition, the remaining gas
Burn the surplus gas in a combustion device. Methane fermentation tank 9 is UASB
method, fixed bed method, and fluidized bed method can be applied.
尚、メタン発酵処理水は、処理水分配槽１２により循環
水２６および処理水２５に分配され、循環水２６は所望
により酸発酵槽、ｐＨ調整槽に送られ、処理水２５は、
活性汚泥設備２８に供給され更に処理に付される。The methane fermentation treated water is distributed into circulating water 26 and treated water 25 by the treated water distribution tank 12, the circulating water 26 is sent to an acid fermentation tank and a pH adjustment tank as required, and the treated water 25 is
The sludge is supplied to activated sludge equipment 28 for further treatment.
以下、上記フローを実廃水（ビール工場の高濃度有機性
廃水）に適用した処理例を示す。An example of treatment in which the above flow is applied to actual wastewater (highly concentrated organic wastewater from a beer factory) will be shown below.
表−１に原水性状を示す。本廃水は、ビール工場の中で
高ＢＯＤ濃度の酵母、麦かすしぼり液等である。廃水Ｂ
ＯＤ ２０．０００〜４０．０００ｍｇ／ １である
。Table 1 shows the raw water properties. This wastewater is yeast, wheat residue, etc. with high BOD concentration in the beer factory. Wastewater B
OD is 20.000-40.000mg/1.
表−２に酸発酵槽における反応条件を示す。槽有効容量
の５０％以上になると供給ポンプ１３がオン（ｏｎ）に
なる。Table 2 shows the reaction conditions in the acid fermenter. When the effective capacity of the tank reaches 50% or more, the supply pump 13 is turned on.
表−３に酸発酵処理水の性状を示す。原水ＳＳの約５０
χは可溶化している。溶解性ＢＯＤの７０〜８０％を揮
発性低級脂肪酸が占めており、酸発酵が順調に進んでい
る。Table 3 shows the properties of the acid fermentation treated water. About 50 raw water SS
χ is solubilized. Volatile lower fatty acids account for 70-80% of the soluble BOD, and acid fermentation is proceeding smoothly.
表−１原水性状
表−２
酸発酵における反応条件
表−３酸発酵処理水性状
上記酸発酵処理水を遠心脱水処理した分離水性状はＢＯ
Ｄ１２．０００〜２５．０００ＩＩ１ｇ／ １、ＳＳ
１，０００〜３，０００であった。Table 1 Raw water properties Table 2 Reaction conditions for acid fermentation Table 3 Acid fermentation treated water properties Separated water obtained by centrifugal dehydration of the above acid fermentation treated water has BO
D12.000~25.000II1g/1, SS
It was 1,000-3,000.
この液にＵＡＳＢ処理水の循環液を混合した液（ＵＡＳ
Ｂ原水）をＩＩＡｓＢ槽にて処理を行った。第２図に処
理成績を示す。液通水後、ＢＯＤ負荷を徐々にに上げた
。約１０日経過後、ＢＯＤ負荷１０ｋｇ／ｍ・ｄてＵＡ
ＳＢ原水ＢＯＤ １，３００ ｍｇ＃！に対しＵＡＳＢ
処理水ＢＯＤ ５００ｍｇ＃２、ＢＯＤ除去率９６％以
上の良好な結果を示している。その後も約３ケ月間安定
した処理成績が得られている。This liquid is mixed with the circulating liquid of UASB treated water (UASB
B raw water) was treated in the IIAsB tank. Figure 2 shows the treatment results. After water flow, the BOD load was gradually increased. After about 10 days, UA with BOD load of 10 kg/m・d
SB raw water BOD 1,300 mg#! against UASB
Treated water BOD 500mg #2 shows good results with a BOD removal rate of 96% or more. After that, stable treatment results were obtained for about 3 months.
本法を適用せずに従来法を用いた場合は、高ＳＳが含ま
れる本廃水では処理不能となった。すなわち、本法の適
用により、高ＢＯＤ 、 ＳＳ廃水に対しても高負荷な
メタン発酵処理の実現が可能となったと言える。When the conventional method was used without applying this method, it became impossible to treat this wastewater containing high SS. In other words, it can be said that by applying this method, it has become possible to realize high-load methane fermentation treatment even for high BOD and SS wastewater.
〔発明の効果〕
以上のように、高ＳＳを含む有機廃水に本発明を適用す
ることで、高速のメタン発酵処理が可能となった。[Effects of the Invention] As described above, by applying the present invention to organic wastewater containing high SS, high-speed methane fermentation treatment has become possible.
しかも、本発明は低コストで省エネルギー的に実施でき
、コンパクトな廃水処理設備になり、工業的に価値の高
いものである。Moreover, the present invention can be implemented at low cost and in an energy-saving manner, resulting in a compact wastewater treatment facility, and is of high industrial value.
１
２
第１図は、本発明の一実施例を説明するためのフローシ
ートを示す図、第２図は、本発明の実施例の結果を示す
グラフである。第３図は、従来の有機廃水処理の一例を
説明するためのフローシートを示す図である。
符号の説明
１．８：酸発酵槽 ２，９：メタン発酵槽１０：遠心脱
水機 １１ｐＨ調整槽
１３：酸発酵処理水供給ポンプ
１６．１７： 苛性ソーダ注入設備 ２■：分離水２
２：脱水ケーキ ２４：メタン発酵処理水２８：活性
汚泥設備 ２９：蒸気加熱設備券
８、叶懇時埼
９；メタン襞ａ％槽
１０家ＩすＩＩＬ水鐵“
１１、ＰＨ桶誉樺
１２、熟捏氷／７）記譜
１３：ぼＶ：＃！慈理都杖忰ホ・シフ゛１４；メ９Ｓ／
膚１を糟弧ＩＨす！ン７′１５、洟イ會し〜１し計
１６：苛（）ｔリータ゛シ主人１隻４甑１７：ｌ／
１８・ 取未
１９；酸瞥ＩＩＳ処理七
２０、寸（リマー〉主入録庫
２１：倚１電本
２２；駁氷チー斗
２３；Ｘ９ン窄９藺り電未
２４； メタン箒１隊処冑水、
２５：飢理七
２６：鴫壇水
２７ｚ竪生山・・ス
２８：第４・主シＳｋ録庫
３１、水＋攪特磯・1 2 FIG. 1 is a diagram showing a flow sheet for explaining one embodiment of the present invention, and FIG. 2 is a graph showing the results of the embodiment of the present invention. FIG. 3 is a diagram showing a flow sheet for explaining an example of conventional organic wastewater treatment. Explanation of symbols 1.8: Acid fermentation tank 2, 9: Methane fermentation tank 10: Centrifugal dehydrator 11 pH adjustment tank 13: Acid fermentation treated water supply pump 16.17: Caustic soda injection equipment 2 ■: Separated water 2
2: Dehydrated cake 24: Methane fermentation treated water 28: Activated sludge equipment 29: Steam heating equipment ticket 8, Kano Konjisaki 9; Methane fold a% tank 10 Isu IIL Suitetsu" 11, PH Oke Homare 12, Mature ice / 7) Notation 13: BO V: #!
The skin 1 is the arc IH! 7'15, 1st meeting - 1 total 16: 1 ship, 1 ship, 17: l/18, 19 unreceived; 720, 20, main storage with IIS processing 21: 倚1 den book 22; Piao Chi-to 23; : 4th Main Sk Recording Room 31, Water + Stirring Tokiso・
Claims (2)
機物を酸発酵することにより少なくとも低級脂肪酸を含
む低分子化合物を生成せしめた後に酸発酵処理水をメタ
ン発酵槽に導入してメタン発酵を行う処理法において、
酸発酵槽有効容量の一部相当量の該酸発酵処理水を酸発
酵槽槽内に残し、該酸発酵処理水の残部を遠心分離して
固形分と分離水に固液分離し、該分離水をメタン発酵槽
内に供給し、メタン発酵を行うメタン発酵処理方法。(1) Wastewater is supplied to an acid fermentation tank, organic matter contained in the wastewater is acid-fermented to produce low-molecular compounds containing at least lower fatty acids, and then the acid-fermented water is introduced into the methane fermentation tank. In a treatment method that performs methane fermentation,
A portion of the acid fermentation treated water equivalent to a part of the effective capacity of the acid fermentation tank is left in the acid fermentation tank tank, and the remainder of the acid fermentation treated water is centrifuged to perform solid-liquid separation into solid content and separated water. A methane fermentation treatment method in which water is supplied into a methane fermentation tank and methane fermentation occurs.
量の廃水が酸発酵槽に供給されることを特徴とする請求
項１記載のメタン発酵処理方法。(2) The methane fermentation treatment method according to claim 1, wherein an amount of wastewater comparable to the amount of the acid fermentation treated water to be separated into solid and liquid is supplied to the acid fermentation tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3234790A JP2587301B2 (en) | 1990-02-15 | 1990-02-15 | Methane fermentation treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3234790A JP2587301B2 (en) | 1990-02-15 | 1990-02-15 | Methane fermentation treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH03238091A true JPH03238091A (en) | 1991-10-23 |
| JP2587301B2 JP2587301B2 (en) | 1997-03-05 |
Family
ID=12356426
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3234790A Expired - Lifetime JP2587301B2 (en) | 1990-02-15 | 1990-02-15 | Methane fermentation treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2587301B2 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003033781A (en) * | 2001-07-24 | 2003-02-04 | Sanki Eng Co Ltd | System for methane gas production |
| JP2006247601A (en) * | 2005-03-14 | 2006-09-21 | Tokyo Gas Co Ltd | Methanation method and apparatus |
| JP2008080274A (en) * | 2006-09-28 | 2008-04-10 | Kurita Water Ind Ltd | Biological treatment apparatus |
| JP2010194491A (en) * | 2009-02-26 | 2010-09-09 | Yanmar Co Ltd | Wastewater treatment apparatus |
| JP2011230007A (en) * | 2010-04-23 | 2011-11-17 | Tokyo Electric Power Co Inc:The | Sewage treatment system |
| JP2012236115A (en) * | 2011-05-09 | 2012-12-06 | Eco Power Corp | Methane fermentation system |
| WO2023171006A1 (en) * | 2022-03-08 | 2023-09-14 | 株式会社サピエナント | Organic matter treatment system and organic matter treatment method |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100883676B1 (en) * | 2008-07-17 | 2009-02-18 | 김현욱 | Apparatus for the two phase anaerobicdigestion |
| JP6385872B2 (en) * | 2015-03-27 | 2018-09-05 | 住友重機械エンバイロメント株式会社 | Water treatment system and water treatment method |
| KR102311041B1 (en) * | 2019-03-27 | 2021-10-12 | 문성우 | A circulation type biogas production facility through inorganic acid control |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS528657A (en) * | 1975-07-09 | 1977-01-22 | Hitachi Ltd | Method for the anaerobic digestion of organic waste liquor |
-
1990
- 1990-02-15 JP JP3234790A patent/JP2587301B2/en not_active Expired - Lifetime
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS528657A (en) * | 1975-07-09 | 1977-01-22 | Hitachi Ltd | Method for the anaerobic digestion of organic waste liquor |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003033781A (en) * | 2001-07-24 | 2003-02-04 | Sanki Eng Co Ltd | System for methane gas production |
| JP2006247601A (en) * | 2005-03-14 | 2006-09-21 | Tokyo Gas Co Ltd | Methanation method and apparatus |
| JP2008080274A (en) * | 2006-09-28 | 2008-04-10 | Kurita Water Ind Ltd | Biological treatment apparatus |
| JP2010194491A (en) * | 2009-02-26 | 2010-09-09 | Yanmar Co Ltd | Wastewater treatment apparatus |
| JP2011230007A (en) * | 2010-04-23 | 2011-11-17 | Tokyo Electric Power Co Inc:The | Sewage treatment system |
| JP2012236115A (en) * | 2011-05-09 | 2012-12-06 | Eco Power Corp | Methane fermentation system |
| WO2023171006A1 (en) * | 2022-03-08 | 2023-09-14 | 株式会社サピエナント | Organic matter treatment system and organic matter treatment method |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2587301B2 (en) | 1997-03-05 |
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