JP2587301B2 - Methane fermentation treatment method - Google Patents
Methane fermentation treatment methodInfo
- Publication number
- JP2587301B2 JP2587301B2 JP3234790A JP3234790A JP2587301B2 JP 2587301 B2 JP2587301 B2 JP 2587301B2 JP 3234790 A JP3234790 A JP 3234790A JP 3234790 A JP3234790 A JP 3234790A JP 2587301 B2 JP2587301 B2 JP 2587301B2
- Authority
- JP
- Japan
- Prior art keywords
- water
- acid
- acid fermentation
- tank
- treatment
- 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
- 238000000855 fermentation Methods 0.000 title claims description 111
- 230000004151 fermentation Effects 0.000 title claims description 111
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims description 94
- 238000000034 method Methods 0.000 title claims description 14
- 239000002253 acid Substances 0.000 claims description 68
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 67
- 239000002351 wastewater Substances 0.000 claims description 27
- 239000007788 liquid Substances 0.000 claims description 19
- 235000014113 dietary fatty acids Nutrition 0.000 claims description 7
- 229930195729 fatty acid Natural products 0.000 claims description 7
- 239000000194 fatty acid Substances 0.000 claims description 7
- 150000004665 fatty acids Chemical class 0.000 claims description 7
- 238000010979 pH adjustment Methods 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 7
- 239000000126 substance Substances 0.000 claims description 6
- 150000001875 compounds Chemical class 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 12
- 239000010802 sludge Substances 0.000 description 7
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 description 7
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 6
- 241000894006 Bacteria Species 0.000 description 4
- 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
- 239000000203 mixture Substances 0.000 description 3
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Chemical compound CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 description 2
- 150000002632 lipids Chemical class 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
- 240000005979 Hordeum vulgare Species 0.000 description 1
- 235000007340 Hordeum vulgare Nutrition 0.000 description 1
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 150000001298 alcohols Chemical class 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
- 238000005119 centrifugation Methods 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
- -1 containing proteins Chemical class 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000010586 diagram 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
- 238000002156 mixing Methods 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 150000004965 peroxy acids Chemical class 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000003672 processing method Methods 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
- 238000004062 sedimentation Methods 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 229940005605 valeric acid Drugs 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)
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、紙パ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。The present invention relates to a methane fermentation treatment method for organic wastewater discharged from food, chemical, pulp and paper industries and the like.
近年、メタン菌を高濃度に維持し高負荷処理を可能と
したリアクター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, reactors capable of maintaining high concentrations of methane bacteria and enabling high-load processing have been actively developed, and methane fermentation processing has attracted attention.
メタン発酵処理を行う場合、廃水の性状即ち廃水中に
含まれる有機物の形態が重要な因子となる。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）。When performing the methane fermentation treatment, the properties of the wastewater, that is, the form of organic substances contained in the wastewater are important factors. 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 substances such as proteins and lipids, the acid fermentation treatment is rate-determining, so it is necessary to apply a two-phase treatment method in which an acid fermentation tank is provided before the methane fermentation tank ( (See FIG. 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 an acid fermentation tank is specially provided, and in many cases, the acid fermentation tank is also used as an adjustment tank. This is because acid fermentation proceeds in the adjustment tank in order to take a 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 soluble carbohydrates,
Wastewater mainly containing proteins, etc., and wastewater containing much SS is insufficient.
この原因としては、調整槽内の反応条件（pH、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 due to the reaction conditions (pH, water temperature,
This is because the amount of acid-producing bacteria, the liquid residence time, etc.) 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 Anaerobic Slu
dge Blanket Process）以後UASBと記す。固定床等〕に
通水するとUASBでは、スラッジベッド部でSSの蓄積が起
こり、グラニュ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 wastewater containing a large amount of SS, even after acid fermentation, the treated water contains a large amount of SS. Therefore, the methane fermentation tank [Upflow Anaerobic Slud Bed Method (Upflow Anaerobic Slud
dge Blanket Process). In the UASB, SS accumulates in the sludge bed when water flows through the fixed bed, etc., and often becomes scum with the granular sludge and flows out of the system. On the other hand, in the fixed bed method, the accumulation of SS between the filter media is increased, and the filter media are blocked, so that the treatment efficiency often decreases. Further, if an acid fermentation tank is separately provided in addition to the adjustment tank, the number of incidental facilities increases, the overall equipment arrangement becomes large, and the merit of high-speed methane fermentation treatment decreases.
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, in the related art, it can be said that there are almost no examples in which two-phase processing is efficiently performed at a practical level.
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。An object of the present invention is to solve the above-mentioned drawbacks of the prior art and to require acid fermentation and, in particular, 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.
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、メタン発酵を行うと共に該固液分離
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、前記分離水のBOD濃度およびSS濃度が高
い場合には、メタン発酵処理水をメタン発酵槽の前段に
設けられるpH調整槽へ供給し、メタン発酵槽へ循環する
ことを特徴とする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。The present invention supplies wastewater to an acid fermentation tank, and after producing a low molecular weight compound containing at least lower fatty acids by acid fermentation of organic substances contained in the wastewater, introduces acid fermentation treated water into a methane fermentation tank. In the treatment method in which methane fermentation is performed, an amount of the acid fermentation treatment water equivalent to part of the effective capacity of the acid fermentation tank is left in the acid fermentation tank, and the remainder of the acid fermentation treatment water is separated from the solid content by centrifugation. Solid-liquid separation into water, the separated water is supplied into a methane fermentation tank, methane fermentation is performed, and wastewater of the same amount as the amount of the acid fermentation treatment water subjected to the solid-liquid separation is supplied to the acid fermentation tank. When the BOD concentration and the SS concentration of the separated water are high, the methane fermentation treatment water is supplied to a pH adjustment tank provided in a preceding stage of the methane fermentation tank, and circulated to the methane fermentation tank. This is a processing method that achieves the above purpose. Can be.
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, 30 to 70% of the effective amount of the acid fermentation tank in the acid fermentation treatment water, that is, the acid fermentation mixture (wastewater content before fermentation treatment of proteins, lipids, etc., and the fermentation of alcohol, lower fatty acids, etc. The resulting liquid composed of low molecular compounds, BOD, SS, etc.) is left in the acid fermentation tank, the remaining 70-30% of 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・流入のタイミングの制御は、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。In the present invention, the supply of wastewater to the acid fermentation tank and the control of the timing of the outflow and inflow of the treated water from the acid fermentation tank to the solid-liquid separation step and further to the methane fermentation step are not particularly limited as long as the above conditions are satisfied. Automatic, semi-automatic,
Can be controlled manually.
特に、本発明においては、該固液分離される該酸発酵
処理水の量と同程度の量と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ミングを一致させることが好まし
い。Particularly, in the present invention, waste water is supplied to the acid fermentation tank in the same amount as the amount of the acid fermentation treated water to be separated into solid and liquid. In this case, it is preferable that the timing of the outflow of the acid fermentation treatment water and the timing of the inflow of the wastewater into the acid fermentation tank are matched.
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, for example, by detecting the liquid level in the acid fermentation tank, the on / off of the pump (on-of-
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pH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、槽内は水中撹拌機等にて
混合撹拌するのがよい。The acid fermentation treatment water mixture in the acid fermentation tank preferably retains at least 30% or more, particularly preferably 50% to 60%, to maintain the acid-producing bacteria and stabilize the acid fermentation treatment. The internal pH is preferably adjusted to 4.5 to 6.0 to stabilize the acid fermentation treatment. Therefore, for example, it can be adjusted by adding an alkali such as caustic soda into the acid fermentation tank or circulating the methane fermentation treatment water. The inside of the tank is preferably mixed and stirred with a submersible 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/以上ある場合である。この場
合、酸発酵処理水のSS濃度は、5,000mg/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, a treatment system suitable for the present invention is a case where the SS concentration of the wastewater flowing into the acid fermentation tank is 10,000 mg / or more. In this case, the SS concentration of the acid fermentation treated water is often 5,000 mg / or more, and the acid fermentation treated water contains a large amount of volatile lower fatty acids such as acetic acid, propionic acid, butyric acid, and valeric acid. Therefore, the acid fermentation treated water emits a strong odor.
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/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。Thus, in the present invention, the treatment efficiency in the methane fermentation tank is improved and the odor is reduced by centrifuging the acid fermentation-treated water, removing excess SS and reducing the SS concentration of the separated water to several thousands mg /. It effectively removes them.
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。Further, it is preferable that the separated water subjected to the solid-liquid separation is adjusted to a pH of preferably about 6.5 before flowing into the methane fermentation tank by adding an alkali or the methane fermentation treated water.
本発明では、該固液分離された分離水のBOD濃度およ
びSS濃度が高い場合、通常、BOD濃度が12000〜25000mg/
、SS濃度が1000〜3000mg/の場合、適宜、メタン発
酵処理水をメタン発酵処理前のpH処理槽へ循環、供給し
て希釈すると共にpH調整をすることが処理のメタン発酵
処理の安定化のために好ましい。In the present invention, when the BOD concentration and the SS concentration of the separated water subjected to the solid-liquid separation are high, the BOD concentration is usually 12000 to 25000 mg /
When the SS concentration is 1000 to 3000 mg /, the methane fermentation treatment water is appropriately circulated to the pH treatment tank before the methane fermentation treatment, supplied and diluted, and pH adjustment is performed to stabilize the methane fermentation treatment. Preferred for.
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 subjected to a treatment step provided separately as required, for example, an activated sludge treatment, a coagulation sedimentation treatment, a pressure flotation treatment, and the like, and is discharged as a reference 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。Hereinafter, embodiments of the present invention will be described 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 replacements and the like that can be made by those skilled in the art.
原水18は酸発酵槽８に流入され、原水中の有機物が酸
発酵処理され、少なくとも低級脂肪酸を含む低分子化合
物が生成される。槽液位レベルは、液位レベル計により
表示される。供給ポンプ13のオン・オフを制御して酸発
酵処理水を酸発酵槽内の液量が槽有効容量の30〜70％、
好ましくは50％〜60％になるように、遠心脱水機10に供
給する。該遠心分離処理された酸発酵処理水とほぼ同程
度の量の原水を酸発酵槽へ供給する。The raw water 18 flows into the acid fermentation tank 8 and the organic matter in the raw water is subjected to acid fermentation treatment to produce a low-molecular compound containing at least a lower fatty acid. The tank liquid level is indicated by a liquid level meter. By controlling on / off of the supply pump 13, the acid fermentation treatment water is supplied to the acid fermentation tank so that the liquid volume is 30 to 70% of the tank effective capacity,
It is supplied to the centrifugal dehydrator 10 so that the concentration is preferably 50% to 60%. Raw water is supplied to the acid fermentation tank in substantially the same amount as the centrifuged acid fermentation treatment water.
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、蒸気加温設備29により
槽内温度は35〜40℃に制御する。また、酸発酵槽内では
水中撹拌機31により汚泥を混合する。In the acid fermentation tank, the pH is adjusted to 4.5 to 6.0, preferably by circulating caustic soda injection equipment 16 or methane fermentation treatment water 24.
Adjust to pH = 5.0-5.5. The temperature in the tank is controlled to 35 to 40 ° C. by the steam heating equipment 29. In the acid fermentation tank, the sludge is mixed by the underwater stirrer 31.
酸発酵処理水19は供給ポンプ13により遠心脱水機10に
供給され、遠心分離される。分離水21はpH調整槽11に供
給される。酸発酵処理水19のSS濃度が10,000mg/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0.5〜１％程度で良い。脱水ケーキ2
2は活性汚泥設備28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MLSS濃
度が低い場合は（MLSS＜5000mg/）、脱水ケーキの一
部は酸発酵槽に戻される。The acid fermentation treatment water 19 is supplied to the centrifugal dehydrator 10 by the supply pump 13 and centrifuged. The separated water 21 is supplied to the pH adjustment tank 11. When the SS concentration of the acid fermentation treatment water 19 is as high as 10,000 mg / or more, the polymer injection equipment 20 is provided in front of the centrifugal dehydrator 10.
To add a cationic polymer. The addition amount may be about 0.5 to 1% per acid fermentation treatment water / SS. Dehydrated cake 2
2 is supplied to an activated sludge facility 28, where it is subjected to stabilization treatment and discharged out of the system together with excess sludge. When the MLSS concentration in the acid fermenter is low (MLSS <5000 mg /), a part of the dehydrated cake is returned to the acid fermenter.
pH調整槽11にて分離水21は、苛性ソーダ注入設備17、
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℃に調整する。Separated water 21 in the pH adjustment tank 11 is converted into caustic soda injection equipment 17,
Alternatively, the pH is adjusted to about 6.5 by using the methane fermentation treated water as the circulating water 26. The water temperature is adjusted to 35 to 40 ° C. by the 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70〜80％
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 raw methane fermentation water 23 is supplied to the methane fermentation tank 9 by the supply pump 14. In the methane fermenter 9, volatile lower fatty acids such as acetic acid are treated by methane bacteria to reduce methane to 70-80%.
Generated gas 27 is generated, and the generated gas is usually burned in a boiler, converted into steam, and used as a heat source (mainly for plant heating).
It is effectively used as The surplus gas is burned by a surplus gas combustion device. The methane fermentation tank 9 can apply the UASB method, the fixed bed method, or the fluidized bed.
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 to the circulating water 26 and the treated water 25 by the treated water distribution tank 12, and the circulating water 26 is sent to an acid fermentation tank and a pH adjustment tank as required. It is supplied to 28 for further processing.
以下、上記フローを実廃水（ビーム工業の高濃度有機
性廃水）に適用した処理例を示す。Hereinafter, a processing example in which the above flow is applied to actual wastewater (high-concentration organic wastewater of Beam Industry) will be described.
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BOD
20,000〜40,000mg/である。表−２に酸発酵槽におけ
る反応条件を示す。酸発酵処理水の残量が槽有効容量の
50％になるように供給ポンプ13のオン・オフを制御し
た。Table 1 shows the raw water properties. This wastewater is a high BOD concentration yeast, barley squeezer, etc. in a brewery. Wastewater BOD
It is 20,000-40,000 mg /. Table 2 shows the reaction conditions in the acid fermentation tank. The remaining amount of acid fermentation treatment water is
On / off of the supply pump 13 was controlled so as to be 50%.
表−３に酸発酵処理水の性状を示す。原水SSの約50％
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 treatment water. About 50% of raw water SS
Is solubilized. Volatile lower fatty acids account for 70-80% of the soluble BOD, and acid fermentation is proceeding smoothly.
上記酸発酵処理水を遠心脱水処理した分離水性状はBO
D12,000〜25,000mg/、SS 1,000〜3,000mg/であっ
た。 The separated aqueous state obtained by centrifugally dehydrating the above acid fermentation treatment water is BO
D12,000 to 25,000 mg / SS, and 1,000 to 3,000 mg / SS.
この液にUASB処理水の循環液を混合した液（UASB原
水）をUASB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/m3・ｄでUASB原水BOD 13,000mg/に
対しUASB処理水BOD 500mg/、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ヶ月間安定した処
理成績が得られている。A liquid (UASB raw water) obtained by mixing this liquid with a circulating liquid of UASB treated water was treated in a UASB tank. FIG. 2 shows the processing results. After passing the liquid, the BOD load was gradually increased. After about 10 days, at a BOD load of 10 kg / m 3 · d, the UASB raw water BOD was 13,000 mg /, the UASB treated water BOD was 500 mg /, and the BOD removal rate was 96% or more. After that, stable processing results were obtained for about three 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, the wastewater containing high SS could not be treated. In other words, it can be said that the application of this method has enabled the realization of high-load methane fermentation treatment even for high BOD and SS wastewater.
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。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。In addition, the present invention can be implemented at low cost and in an energy-saving manner, becomes a compact wastewater treatment facility, and has high industrial value.
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。 符合の説明 1,8:酸発酵槽、2,9:メタン発酵槽 10:遠心脱水機、11:pH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、21:分離水 22: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 view showing a flow sheet for explaining an example of conventional organic wastewater treatment. 1,8: Acid fermentation tank, 2,9: Methane fermentation tank 10: Centrifugal dehydrator, 11: pH adjustment tank 13: Acid fermentation treatment water supply pump 16, 17: Caustic soda injection equipment, 21: Separated water 22 : Dewatered cake, 24: Methane fermentation treated water 28: Activated sludge equipment, 29: Steam heating equipment
フロントページの続き (72)発明者 三田 新 東京都港区港南１丁目６番27号 荏原イ ンフィルコ株式会社内 (72)発明者 塩野 俊一 東京都港区港南１丁目６番27号 荏原イ ンフィルコ株式会社内 (56)参考文献 特開 昭52−8657（ＪＰ，Ａ)Continuing from the front page (72) Inventor Mita Shin Ebara Infilco Co., Ltd., 1-6-27 Konan, Minato-ku, Tokyo (72) Inventor Shunichi Shiono 1-6-27 Konan, Minato-ku, Tokyo Ebara Infilco Co., Ltd. In-house (56) References JP-A-52-8657 (JP, A)
Claims (1)
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、メタン発酵を行うと共に該固液分離
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、前記分離水のBOD濃度およびSS濃度が高
い場合には、メタン発酵処理水をメタン発酵槽の前段に
設けられるpH調整槽へ供給し、メタン発酵槽へ循環する
ことを特徴とするメタン発酵処理方法。1. A wastewater is supplied to an acid fermentation tank, and an organic substance contained in the wastewater is acid-fermented to produce a low-molecular compound containing at least a lower fatty acid. In the treatment method in which methane fermentation is performed, the acid fermentation treatment water corresponding to a part of the effective capacity of the acid fermentation tank is left in the acid fermentation tank, and the remainder of the acid fermentation treatment water is centrifuged to obtain a solid content. Solid-liquid separation into separated water, the separated water is supplied into a methane fermentation tank, and methane fermentation is performed, and waste water of the same amount as the amount of the acid fermentation treated water separated by solid-liquid separation is supplied to the acid fermentation tank. Supplied, when the BOD concentration and the SS concentration of the separated water are high, the methane fermentation treatment water is supplied to a pH adjustment tank provided in a preceding stage of the methane fermentation tank, and is circulated to the methane fermentation tank. Fermentation treatment method.
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 JPH03238091A (en) | 1991-10-23 |
| JP2587301B2 true 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 (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100883676B1 (en) * | 2008-07-17 | 2009-02-18 | 김현욱 | Abnormal anaerobic digestion apparatus with pH control through real-time pH monitoring |
| JP2016185515A (en) * | 2015-03-27 | 2016-10-27 | 住友重機械エンバイロメント株式会社 | Water treatment system and water treatment method |
| KR20200114992A (en) * | 2019-03-27 | 2020-10-07 | 문성우 | A circulation type biogas production facility through inorganic acid control |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4945035B2 (en) * | 2001-07-24 | 2012-06-06 | 三機工業株式会社 | Methane gas generation system |
| JP2006247601A (en) * | 2005-03-14 | 2006-09-21 | Tokyo Gas Co Ltd | Methane generation method and methane generator |
| JP5140980B2 (en) * | 2006-09-28 | 2013-02-13 | 栗田工業株式会社 | Biological treatment equipment |
| JP2010194491A (en) * | 2009-02-26 | 2010-09-09 | Yanmar Co Ltd | Wastewater treatment apparatus |
| JP5696372B2 (en) * | 2010-04-23 | 2015-04-08 | 東京電力株式会社 | Sewage treatment system |
| JP5730120B2 (en) * | 2011-05-09 | 2015-06-03 | 日本エコ電力株式会社 | Methane fermentation system |
| JPWO2023171006A1 (en) * | 2022-03-08 | 2023-09-14 |
Family Cites Families (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
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100883676B1 (en) * | 2008-07-17 | 2009-02-18 | 김현욱 | Abnormal anaerobic digestion apparatus with pH control through real-time pH monitoring |
| JP2016185515A (en) * | 2015-03-27 | 2016-10-27 | 住友重機械エンバイロメント株式会社 | Water treatment system and water treatment method |
| KR20200114992A (en) * | 2019-03-27 | 2020-10-07 | 문성우 | A circulation type biogas production facility through inorganic acid control |
| KR102311041B1 (en) * | 2019-03-27 | 2021-10-12 | 문성우 | A circulation type biogas production facility through inorganic acid control |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH03238091A (en) | 1991-10-23 |
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