JPH08281293A - Treatment of alcohol-distillation waste liquid - Google Patents
Treatment of alcohol-distillation waste liquidInfo
- Publication number
- JPH08281293A JPH08281293A JP10781695A JP10781695A JPH08281293A JP H08281293 A JPH08281293 A JP H08281293A JP 10781695 A JP10781695 A JP 10781695A JP 10781695 A JP10781695 A JP 10781695A JP H08281293 A JPH08281293 A JP H08281293A
- Authority
- JP
- Japan
- Prior art keywords
- stage
- treatment
- water
- waste liquid
- oiling
- 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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Links
Classifications
-
- Y02W10/12—
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、アルコール蒸留廃液の
新規な処理方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a novel method for treating alcohol distillation waste liquid.
【０００２】[0002]
【従来の技術】糖蜜を原料とするアルコール製造工程か
ら排出されるアルコール蒸留廃液は、黒褐色を呈し、有
機物を高濃度に含有しているために廃水処理は極めて困
難である。一方、同じアルコール蒸留廃液でも、焼酎製
造に起因するアルコール蒸留廃液の多くは海洋投棄さ
れ、ロンドン条約の対象となっている。いずれも廃水処
理が困難であり、低コストで効率良く処理する方法は未
だ見出されてはいない。2. Description of the Related Art Alcohol distillation waste liquid discharged from an alcohol production process using molasses as a raw material has a blackish brown color and contains a high concentration of organic substances, so that it is extremely difficult to treat the wastewater. On the other hand, even with the same alcohol distillation waste liquid, most of the alcohol distillation waste liquid resulting from the production of shochu has been dumped into the ocean and is subject to the London Treaty. In all cases, wastewater treatment is difficult, and a low-cost and efficient treatment method has not yet been found.
【０００３】糖蜜を原料とするアルコール製造工程から
排出されるアルコール蒸留廃液は、１９６０年代には浮
遊性の嫌気性生物を用いた廃水処理装置が計画され実装
置化された。しかし、当時の技術レベルでは安定した処
理が得られずに、その後好気性生物を利用する活性汚泥
法に置き変わった。しかしながら、活性汚泥法でも色の
除去は不可能であり、酸化することによって更に色が濃
くなる傾向にあった。As for the alcohol distillation waste liquid discharged from the alcohol production process using molasses as a raw material, a waste water treatment device using planktonic anaerobic organisms was planned and put into practical use in the 1960s. However, stable treatment was not obtained at the technical level at that time, and the activated sludge method, which uses aerobic organisms, was subsequently replaced. However, the color cannot be removed even by the activated sludge method, and the color tends to be further darkened by oxidation.
【０００４】糖蜜を原料とするアルコールを製造してい
る国は、東南アジアに多い。東南アジアの国々でのアル
コール蒸留廃液の処理は、広大な土地を利用した嫌気ラ
グーン法が多く採用されている。しかしながら、処理は
決して満足に行われてはおらず、不完全な水質のままの
黒色の排水を河川に放流している。Many countries in Southeast Asia produce alcohol using molasses as a raw material. Anaerobic lagoon method, which uses vast land, is widely adopted for the treatment of alcohol distillery waste liquid in Southeast Asian countries. However, the treatment is never satisfactory and it discharges black effluent with incomplete water quality into rivers.
【０００５】１９８０年代になって、ある種の嫌気性生
物が数mmの粒子を形成する性質を工業的に利用してＵＡ
ＳＢ（Ｕｐｆｌｏｗ Ａｎａｅｒｏｂｉｃ Ｓｌｕｄｇ
ｅＢｌａｎｋｅｔ）法と一般に呼ばれる嫌気的処理方式
が開発され、廃水処理装置は、よりコンパクトになり、
コストも大幅に低減できるようになった。この技術を利
用することによりアルコール蒸留廃液処理装置も同様に
コンパクトかつ低コストが可能になると考えられる。し
かし、未だ実装置化には至っていない。[0005] In the 1980s, UA was industrially used to take advantage of the property that certain anaerobic organisms form particles of several mm.
SB (Upflow Anaeroic Sludge
An anaerobic treatment system generally called the eBlanket method has been developed, and the wastewater treatment equipment has become more compact,
The cost can also be reduced significantly. By utilizing this technology, it is considered that the alcohol distillation waste liquid treatment device can be similarly compact and low cost. However, it has not yet become a real device.
【０００６】アルコール蒸留廃液にＵＡＳＢ法を適用す
ることによって、より合理的な廃水処理装置が可能には
なったが、アルコール蒸留廃液が有する黒褐色の色は生
物処理で除去することはできない。色を除去する方法と
して油化処理技術を応用する手段が考えられる。油化処
理とは有機物を高温高圧処理することで、これを油分に
変える処理方法であり、これまで活性汚泥等の有機性汚
泥に対して実績を有している。By applying the UASB method to the alcohol distillation waste liquid, a more rational waste water treatment apparatus has become possible, but the blackish brown color of the alcohol distillation waste liquid cannot be removed by biological treatment. As a method of removing the color, a means of applying oil treatment technology can be considered. The liquefaction treatment is a treatment method in which organic matter is subjected to high-temperature and high-pressure treatment to convert it into oil, and has a track record for organic sludge such as activated sludge so far.
【０００７】高濃度の有機物を含有するアルコール蒸留
廃液に油化処理を適用すると、エネルギー源としての油
分が回収できることは勿論、ＢＯＤを大幅に除去するこ
とができ、さらに黒褐色の色を薄い黄色にまで脱色でき
る。油化処理することによりアルコール蒸留廃液の濃度
を大幅に低減することができるため、廃水処理の前処理
として効果的である。By applying an oil treatment to an alcohol distillation waste liquid containing a high concentration of organic matter, not only the oil content as an energy source can be recovered but also the BOD can be largely removed, and the blackish brown color can be changed to a light yellow color. Can be decolorized. Since the concentration of the alcohol distillation waste liquid can be significantly reduced by the oil treatment, it is effective as a pretreatment for the wastewater treatment.
【０００８】油化処理及びＵＡＳＢ法が開発される前に
は、水質、外観ともにとても満足できる処理法は期待で
きず、あえてＢＯＤ２０mg／Ｌ以下の処理水を得ようと
すると、広大な設置面積、多大な設備投資、そして労力
を必要とする維持管理に膨大なランニングコスト及び人
工を必要としていた。しかし、油化処理技術とＵＡＳＢ
法を組み合わせることにより脱色が可能で、コンパクト
な廃水処理装置が可能となった。Before the oilification treatment and the UASB method were developed, a treatment method which is very satisfactory in terms of water quality and appearance could not be expected, and when it was attempted to obtain treated water having a BOD of 20 mg / L or less, a vast installation area, A large amount of running cost and man-made were required for maintenance that requires a large amount of capital investment and labor. However, oil treatment technology and UASB
By combining the methods, decolorization is possible and a compact wastewater treatment system is possible.
【０００９】[0009]
【発明が解決しようとする課題】しかしながら、前記の
方法においても、アルコール廃液中の有機物を十分に分
解し、ＢＯＤを十分に低下せしめるには至っていなかっ
た。この原因として、油化処理中にフェノール類が生成
し、このフェノール類が、次の嫌気的生物処理を妨害す
るためであることが明らかになった。したがって、本発
明は、フェノール類の妨害を除去することによって、ア
ルコール廃液を十分に分解処理することができる方法を
提供しようとするものである。However, even in the above-mentioned method, it has not been possible to sufficiently decompose the organic substances in the alcohol waste liquid and sufficiently reduce the BOD. It was revealed that the cause of this is that phenols are produced during the oil treatment and the phenols interfere with the subsequent anaerobic biological treatment. Therefore, the present invention aims to provide a method capable of sufficiently decomposing an alcohol waste liquid by removing the interference of phenols.
【００１０】[0010]
【課題を解決するための手段】本発明者らは、上記の課
題を解決すべく種々検討した結果、アルコール蒸留廃液
を常法に従って油化処理した後、嫌気的生物処理を少な
くとも２段に分けて行えば、第１段階においてフェノー
ル類が大部分分解除去され、その結果第２段の嫌気的生
物処理において、残留する有機物が極めて効率よく分解
されることを見い出し、この知見に基づいて本発明を完
成した。As a result of various studies to solve the above-mentioned problems, the inventors of the present invention divided the anaerobic biological treatment into at least two stages after liquefying the alcohol distillation waste liquid according to a conventional method. Then, it was found that most of the phenols were decomposed and removed in the first step, and as a result, the remaining organic matter was decomposed extremely efficiently in the anaerobic biological treatment of the second step, and the present invention was based on this finding. Was completed.
【００１１】従って本発明は、アルコール蒸留廃液を油
化処理し、次いで嫌気性生物処理する方法において、該
油化処理により生じたフェノール類を第１段の嫌気性生
物処理により分解除去した後、残留する有機物を次段の
嫌気的生物処理によりさらに分解することを特徴とする
アルコール蒸留廃液の処理方法を提供する。Accordingly, the present invention is a method of oil-treating an alcohol distillation waste liquor and then treating it with an anaerobic organism, after decomposing and removing the phenols produced by the oil-treatment with the first-stage anaerobic organism treatment, Disclosed is a method for treating an alcohol distillation waste liquid, which is characterized in that residual organic matter is further decomposed by the subsequent anaerobic biological treatment.
【００１２】[0012]
【具体的な説明】アルコール蒸留廃液の含有成分や色
は、アルコール発酵原料の種類等により異るが、現在最
も多く使用されている廃糖蜜を主原料として使用する場
合、蒸留廃液は黒褐色〜赤褐色であり、約４０，０００
mg／Ｌ程度のＢＯＤを含有し、フェノール類の含量はご
くわずかである。[Detailed description] The content and color of the alcohol distillation waste liquor vary depending on the type of alcohol fermentation raw material, but when using molasses, which is most commonly used today, as the main raw material, the distillation waste liquor is dark brown to reddish brown. And about 40,000
It contains BOD of about mg / L, and the content of phenols is very small.
【００１３】本発明においては、まず、かかる蒸留廃液
を油化処理する。油化処理技術自体はすでに確立された
技術であり、本発明の特徴を構成するものではない。油
化処理技術は、有機物を含有する廃液を高圧及び高温で
処理することにより該有機物を油化するものであり、こ
れをアルコール蒸留廃液の処理に使用する場合、５０〜
２００気圧、２００〜４００℃にて０．５〜２時間の処
理が行われる。In the present invention, first, such a distillation waste liquid is oiled. The oil treatment technology itself is an established technology and does not constitute a feature of the present invention. The liquefaction treatment technology is to liquefy an organic substance-containing waste liquid by treating it at high pressure and high temperature, and when it is used for treating alcohol distillation waste liquid,
The treatment is performed at 200 atm and 200 to 400 ° C. for 0.5 to 2 hours.
【００１４】この油化処理により、約４０，０００mg／
ＬのＢＯＤはおよそ半減して約２０，０００mg／Ｌとな
る。他方、フェノール類の含量は、アルコール蒸留廃液
の性質や油化処理条件等により異るが、通常、例えばお
よそ１００mg／Ｌに上昇する。他方、色は著しく脱色さ
れて黄色となる。By this oiling treatment, about 40,000 mg /
The BOD of L is approximately halved to about 20,000 mg / L. On the other hand, the content of phenols varies depending on the properties of the alcohol distillation waste liquor, oil treatment conditions, etc., but usually increases to, for example, about 100 mg / L. On the other hand, the color is significantly decolorized to yellow.
【００１５】本発明においては、上記のごとく油化法に
より前処理した廃液を少なくとも２段階に分けて嫌気的
生物処理を行う。嫌気的生物処理法としては、任意の常
法を用いることができるが、本発明において特に好まし
い方法は、それ自体すでに確立されている技術であるＵ
ＡＳＢ（Ｕｐｆｌｏｗ Ａｎａｅｒｏｂｉｃ Ｓｌｕｄ
ｇｅ Ｂｌａｎｋｅｔ）法である。上記のごとく油化処
理した液をＵＡＳＢ法にかけるには、ＢＯＤ容積負荷２
〜４kg／ｍ3 ・日程度が好ましく、この範囲でのＢＯＤ
除去率は４０〜５０％程度であり、実用的な運転条件下
でこれ以上のＢＯＤ除去率を得ることはできない。この
様にＢＯＤ除去率に限界がある理由の１つは、油化処理
水にフェノール類が有意量含まれており、このフェノー
ル類が生物処理を妨害するためであると推定される。他
方、この第１段の嫌気処理によりフェノール類は約９０
％除去される。In the present invention, the waste liquid pretreated by the oilification method as described above is divided into at least two stages for anaerobic biological treatment. As the anaerobic biological treatment method, any conventional method can be used, but a particularly preferable method in the present invention is a technique already established per se U
ASB (Upflow Anaerobic Slud
ge Blanket) method. To apply the oil-treated solution as described above to the UASB method, the BOD volume load 2
~ 4kg / m 3 · day is preferable, BOD in this range
The removal rate is about 40 to 50%, and a BOD removal rate higher than this cannot be obtained under practical operating conditions. It is presumed that one of the reasons why the BOD removal rate is limited in this way is that the oil-treated water contains a significant amount of phenols and the phenols interfere with biological treatment. On the other hand, the anaerobic treatment in the first stage reduced the phenol content to about 90%.
% Removed.
【００１６】次に、本発明においては、前記第１段目の
嫌気的生物処理段階に続き、別の段階として、第２段目
の嫌気的生物処理を行う。この処理条件は第１段目の処
理条件と同様でよい。この第２段目の嫌気的生物処理の
後、第１段目及び第２段目の生物処理を合わせたＢＯＤ
除去率は高いものとなり、第１段階において容積負荷を
減少しただけでは得られないＢＯＤ除去率が達成され
る。好ましい態様では除去率は９０〜９５％に達し、フ
ェノールはほぼ完全に除去される。Next, in the present invention, following the first stage of anaerobic biological treatment, the second stage of anaerobic biological treatment is performed as another stage. This processing condition may be the same as the processing condition of the first stage. BOD combining the first and second stage biological treatments after this second stage anaerobic biological treatment
The removal rate is high and a BOD removal rate is achieved which is not obtained by only reducing the volume loading in the first stage. In the preferred embodiment, the removal rate reaches 90 to 95%, and the phenol is almost completely removed.
【００１７】第１段階での容積負荷を低下させただけで
は得られないＢＯＤ除去率が２段階処理により得られる
のが本発明の第一の効果である。すなわち、比較例２に
示すごとく、ＢＯＤ容積負荷を４．０kg／ｍ3 ・日とし
た場合に約４５％のＢＯＤが除去されるのであるから、
ＢＯＤ容積負荷率をその半分の２．０kg／ｍ3 ・日にす
れば除去率は４５％よりはるかに向上（例えば約７５％
まで）するはずであるが、実際には参考例１に示すごと
く、ＢＯＤ除去率はほとんど向上せず約５０％に達しな
い。これに対して、実施例に示すごとく、嫌気的生物処
理を２段階に行えば、平均ＢＯＤ負荷率３．０kg／ｍ3
・日において、ＢＯＤ除去率は９０％以上に達する。こ
れは参考例１（ＢＯＤ容積負荷率４．０kg／ｍ3 ・日で
ＢＯＤ除去率約４５％）及び参考例２（ＢＯＤ容積負荷
率２．０kg／ｍ3 ・日でＢＯＤ除去率約５０％）からは
予想できない高率である。The first effect of the present invention is that the BOD removal rate, which cannot be obtained only by reducing the volume load in the first stage, is obtained by the two-stage treatment. That is, as shown in Comparative Example 2, when the BOD volume load is set to 4.0 kg / m 3 · day, about 45% of BOD is removed.
If the BOD volume loading rate is half that of 2.0 kg / m 3 · day, the removal rate will be much higher than 45% (eg about 75%).
However, as shown in Reference Example 1, the BOD removal rate is not substantially improved and does not reach about 50%. On the other hand, as shown in the examples, if the anaerobic biological treatment is performed in two stages, the average BOD load factor of 3.0 kg / m 3
-The BOD removal rate reaches 90% or more in a day. This is Reference Example 1 (BOD volume loading rate of 4.0 kg / m 3 · day with BOD removal rate of about 45%) and Reference Example 2 (BOD volume loading rate of 2.0 kg / m 3 · day with BOD removal rate of about 50%). ) Is a high rate that cannot be predicted.
【００１８】また、仮に、第２段の処理において、第１
段階と同様の除去効率が得られると仮定しても、本発明
の方法においては、その仮定よりもはるかに高い除去効
率が得られ、２段階処理を行うことにより相乗効果も得
られる。Further, tentatively, in the processing of the second stage, the first
Even if it is assumed that the removal efficiency similar to that of the step is obtained, the method of the present invention obtains a much higher removal efficiency than that assumption, and a synergistic effect is also obtained by performing the two-step treatment.
【００１９】すなわち、１段階当りの除去率を、フェノ
ールでは９０％、ＢＯＤでは５０％とすれば、同じ除去
効率２段階の処理を行えば、フェノールについては約９
９％が除去されることになり、ほぼ完全に除去されると
予想されるが、ＢＯＤは約７５％が除去されると予想さ
れる。しかも、生物処理においては、それに関与する微
生物により資化・分解されやすい物質が優先的に分解・
除去されると予想されるから、第２段階目の除去効率は
第１段目の除去効率より劣ると予想するのが当業者の常
識であり、そうであれば、第１段及び第２段の嫌気的生
物処理を合わせたＢＯＤ除去率は７５％に達しないと予
想される。That is, if the removal rate per step is 90% for phenol and 50% for BOD, the same removal efficiency of about 2 steps will result in about 9 for phenol.
BOD is expected to be removed at about 75%, while 9% will be removed and is expected to be almost completely removed. Moreover, in biological treatment, substances that are easily assimilated / decomposed by microorganisms involved in the treatment are preferentially decomposed / decomposed.
Since it is expected to be removed, it is common sense for those skilled in the art to expect that the removal efficiency of the second stage is inferior to that of the first stage. The combined BOD removal rate of anaerobic biotreatment is expected not to reach 75%.
【００２０】しかしながら実際には、全く予想外のこと
に、ＢＯＤ除去率は９０〜９５％に達し、予想された値
よりはるかに高い。すなわち、嫌気的生物処理を２回行
うことによる相乗効果が明らかに認められる。In practice, however, quite unexpectedly, the BOD removal rate reaches 90-95%, which is much higher than expected. That is, the synergistic effect of performing the anaerobic biological treatment twice is clearly recognized.
【００２１】次に、本発明の実施に使用する装置の典型
的な１例を図２に示し、そしてこれに対応する従来技術
の装置を図１に示し、これらの図に言及しながら本発明
の方法及びそれに用いる装置を説明する。Next, a typical example of the apparatus used for carrying out the present invention is shown in FIG. 2, and the corresponding prior art apparatus is shown in FIG. The method and apparatus used therefor will be described.
【００２２】図１はアルコール蒸留廃液の油化処理水を
ＵＡＳＢリアクター１段で処理した時の処理フローであ
り、従来技術に属するものである。油化処理水受槽１に
入れた油化処理水を揚水ポンプ２で一定量揚水し、中和
槽３に導き、撹拌機４で撹拌しながらpH計５を用いて、
油化処理水のpHを６．５〜７になるように、ＮａＯＨ貯
槽６のＮａＯＨをＮａＯＨ供給ポンプ７で送る。中和し
た油化処理水を供給ポンプ８でＵＡＳＢリアクター９に
送り込み、処理を行なう。ＵＡＳＢリアクターには粒状
の嫌気性生物１０が充填されており、嫌気性生物１０に
よって油化処理水を処理した。処理水は処理水槽１１で
受ける。FIG. 1 shows a processing flow when the oil-treated water of the alcohol distillation waste liquid is processed in one stage of the UASB reactor, which belongs to the prior art. A certain amount of the oil-treated water in the oil-treated water receiving tank 1 is pumped up by the pump 2, which is guided to the neutralization tank 3 and stirred by the stirrer 4 while using the pH meter 5.
The NaOH supply pump 7 sends the NaOH in the NaOH storage tank 6 so that the pH of the oil-treated water becomes 6.5 to 7. The neutralized liquefied treated water is sent to the UASB reactor 9 by the supply pump 8 and treated. The UASB reactor was packed with granular anaerobic organisms 10, and the anaerobic organisms 10 treated the oil-treated water. The treated water is received by the treated water tank 11.
【００２３】図２はアルコール蒸留廃液の油化処理水を
ＵＡＳＢリアクター２段で処理したときの処理フローで
あり、本発明に属するものである。油化処理水受槽１に
入れた油化処理水を、揚水ポンプ２で一定量揚水し、中
和槽３に導き、撹拌機４で撹拌しながらpH計５を用い
て、油化処理水のpHを６．５〜７になるように、ＮａＯ
Ｈ貯槽６のＮａＯＨをＮａＯＨ供給ポンプ７で送る。中
和した油化処理水を供給ポンプ８でＵＡＳＢリアクター
９に送り込み、処理を行なう。ＵＡＳＢリアクターには
粒状の嫌気性生物１０が充填されており、嫌気性生物１
０によって油化処理水を処理する。処理水は処理水槽１
１で受けた後、２段目供給ポンプ１２で２段目のＵＡＳ
Ｂリアクター１３に送る。２段目のＵＡＳＢリアクター
１３には１段目と同様に、粒状の嫌気性生物１４が充填
されており、２段目のＵＡＳＢリアクター１３で処理さ
れる。処理した上澄水は放流槽１５に受ける。FIG. 2 shows a processing flow when the oil-treated water of the alcohol distillation waste liquid is processed in two stages of the UASB reactor, and belongs to the present invention. A certain amount of oil-treated water in the oil-treated water receiving tank 1 is pumped up by the pump 2, which is then introduced into the neutralization tank 3 and stirred by the stirrer 4 using the pH meter 5 while using the oil-treated water. NaO to adjust pH to 6.5-7
The NaOH in the H storage tank 6 is sent by the NaOH supply pump 7. The neutralized liquefied treated water is sent to the UASB reactor 9 by the supply pump 8 and treated. The UASB reactor is packed with granular anaerobic organisms 10 and anaerobic organisms 1
0 to treat the oil-treated water. Treated water is treated water tank 1
After receiving at 1, the second-stage supply pump 12 at the second-stage UAS
Send to B reactor 13. Similar to the first stage, the second-stage UASB reactor 13 is filled with granular anaerobic organisms 14 and is treated in the second-stage UASB reactor 13. The treated supernatant water is received in the discharge tank 15.
【００２４】[0024]
【実施例】次に、実施例及び比較例により、本発明をさ
らに具体的に説明する。比較例１． EXAMPLES Next, the present invention will be described more specifically by way of Examples and Comparative Examples. Comparative Example 1.
【００２５】アルコール蒸留廃液の油化処理水を水道水
で１０倍希釈した液を処理対象水とした。１０倍希釈し
た目的は、フェノールの阻害性を極力排除するためであ
る。図１に示した処理フローでＵＡＳＢ１段処理を行な
った。ＢＯＤ容積負荷は２．０kg／ｍ3 ・日と設定し
た。その結果フェノールは９０．１％の除去率が得られ
たが、ＢＯＤの除去率は４８．６％であった。結果を表
１に示す。A solution obtained by diluting the oil-treated water of the alcohol distillation waste liquid by 10 times with tap water was used as the water to be treated. The purpose of 10-fold dilution was to eliminate the inhibitory effect of phenol as much as possible. The UASB one-stage process was performed in the process flow shown in FIG. The BOD volume load was set to 2.0 kg / m 3 · day. As a result, the removal rate of phenol was 90.1%, but the removal rate of BOD was 48.6%. The results are shown in Table 1.
【００２６】[0026]
【表１】 [Table 1]
【００２７】比較例２． Comparative Example 2.
【００２８】図１の処理フローで比較例１と同様に１０
倍希釈水を用いて処理を行った。ただし、ＢＯＤ容積負
荷は２倍の４．０kg／ｍ3 ・日とした。その結果フェノ
ールは９５．２％の高除去率を得ることができたが、Ｂ
ＯＤは実施例その１の結果とほぼ同じ除去率で４４．７
％であった。結果を表２に示す。In the processing flow of FIG.
The treatment was carried out with double dilution water. However, the BOD volume load was doubled to 4.0 kg / m 3 · day. As a result, phenol was able to obtain a high removal rate of 95.2%.
OD was 44.7 with almost the same removal rate as the result of Example 1.
%Met. Table 2 shows the results.
【００２９】[0029]
【表２】 [Table 2]
【００３０】実施例 図２のフローで処理を行った。処理対象水は比較例１及
び２と同様の、１０倍に希釈した油化処理水を用いた。
ＢＯＤ容積負荷は１段目６．０kg／ｍ3 ・日、１段目＋
２段目の平均ＢＯＤ容積負荷は３．０kg／ｍ3 ・日とし
て実施した。その結果１段目では実施例その１および実
施例その２と同様の除去率が得られたが、１段目＋２段
目の除去率はフェノール１００％ＢＯＤ９４．２％と大
幅に高い値が得られた。結果を表３に示す。 Example Processing was performed according to the flow of FIG. As the water to be treated, the same 10-fold diluted oil-treated water as in Comparative Examples 1 and 2 was used.
BOD volume load is 1st stage 6.0kg / m 3 · day, 1st stage +
The average BOD volume load of the second step was 3.0 kg / m 3 · day. As a result, in the 1st stage, the removal rate similar to that in Example 1 and Example 2 was obtained, but the removal rate in the 1st stage + 2nd stage was phenol 100% BOD94.2%, which was a significantly high value. Was given. The results are shown in Table 3.
【００３１】[0031]
【表３】 [Table 3]
【００３２】[0032]
【発明の効果】比較例１及び２並びに実施例の結果から
明白なように、１段処理ではＢＯＤ容積負荷を２kg／ｍ
3 ・日に下げて運転してみたが、ＵＡＳＢリアクター内
部の嫌気性生物に対するフェノールの阻害が生じて低除
去率であった。しかし、２段処理した結果１段目ではフ
ェノールの影響が出てＢＯＤの処理性は向上しないが、
１段目でフェノールの大半が除去されてしまったため
に、２段目の嫌気性生物の活性が活発になって総合的に
１段目＋２段目のＢＯＤ容積負荷３．０kg／ｍ3 ・日と
高い条件下においてＢＯＤの高除去率を得ることが可能
になった。As is clear from the results of Comparative Examples 1 and 2 and Examples, the BOD volume load is 2 kg / m in the one-step treatment.
Although it was operated for 3 days, the removal rate was low due to the inhibition of phenol with respect to the anaerobic organisms inside the UASB reactor. However, as a result of the two-step treatment, the effect of phenol appears in the first step and the processability of BOD does not improve,
Most of the phenol was removed in the first stage, so the activity of the anaerobic organisms in the second stage became active, and the BOD volume load of the first and second stages was 3.0 kg / m 3 · day in total. It became possible to obtain a high removal rate of BOD under high conditions.
【図１】図１は、従来技術のアルコール蒸留廃液処理装
置の１例を示す図である。FIG. 1 is a diagram showing an example of a conventional alcohol distillation waste liquid treatment apparatus.
【図２】図２は、本発明のアルコール蒸留廃液の処理法
を実施するための装置の１例を示す図である。FIG. 2 is a diagram showing an example of an apparatus for carrying out the method for treating an alcohol distillation waste liquid according to the present invention.
１…油化処理水受槽 ２…揚水ポンプ ３…中和槽 ４…撹拌機 ５…pH計 ６…ＮａＯＨ貯槽 ７…ＮａＯＨ供給ポンプ ８…供給ポンプ ９…ＵＡＳＢリアクター １０…嫌気性生物 １１…処理水槽 １２…２段目供給ポンプ １３…２段目のＵＡＳＢリアクター １４…嫌気性生物 １５…放流槽 1 ... Oil-treated water receiving tank 2 ... Pumping pump 3 ... Neutralizing tank 4 ... Stirrer 5 ... pH meter 6 ... NaOH storage tank 7 ... NaOH supply pump 8 ... Supply pump 9 ... UASB reactor 10 ... Anaerobic organism 11 ... Treated water tank 12 ... Second-stage supply pump 13 ... Second-stage UASB reactor 14 ... Anaerobic organism 15 ... Discharge tank
───────────────────────────────────────────────────── フロントページの続き (72)発明者 細井 健二 神奈川県平塚市高村26番地高村団地27− 301 (72)発明者 和田 吉郎 神奈川県横浜市磯子区杉田７丁目１番地 722号 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Kenji Hosoi, 26, Takamura, Hiratsuka, Kanagawa 27-301 (72) Inventor, Yoshiro Wada, 7-1, Sugita, 7-chome, Isogo-ku, Yokohama, Kanagawa
Claims (1)
で嫌気性生物処理する方法において、該油化処理により
生じたフェノール類を第１段の嫌気的生物処理により分
解除去した後、残留する有機物を次段の嫌気的生物処理
により、更に分解することを特徴とするアルコール蒸留
廃液の処理方法。1. A method in which an alcohol distillation waste liquor is subjected to an oil treatment and then to an anaerobic biological treatment, and the phenols produced by the oil treatment are decomposed and removed by the first-stage anaerobic biological treatment, and then the remaining organic substances are left. Is further decomposed by the anaerobic biological treatment in the next step, which is a method for treating an alcohol distillation waste liquid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP10781695A JP2718467B2 (en) | 1995-04-10 | 1995-04-10 | Treatment of alcohol distillation waste liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP10781695A JP2718467B2 (en) | 1995-04-10 | 1995-04-10 | Treatment of alcohol distillation waste liquid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH08281293A true JPH08281293A (en) | 1996-10-29 |
| JP2718467B2 JP2718467B2 (en) | 1998-02-25 |
Family
ID=14468767
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP10781695A Expired - Lifetime JP2718467B2 (en) | 1995-04-10 | 1995-04-10 | Treatment of alcohol distillation waste liquid |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2718467B2 (en) |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5710390A (en) * | 1980-06-23 | 1982-01-19 | Agency Of Ind Science & Technol | Methane-fermenting method for thermally decomposed oil of municipal waste |
-
1995
- 1995-04-10 JP JP10781695A patent/JP2718467B2/en not_active Expired - Lifetime
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5710390A (en) * | 1980-06-23 | 1982-01-19 | Agency Of Ind Science & Technol | Methane-fermenting method for thermally decomposed oil of municipal waste |
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| Publication number | Publication date |
|---|---|
| JP2718467B2 (en) | 1998-02-25 |
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