JP2010207700A - Methane fermentation apparatus and methane fermentation method - Google Patents

Methane fermentation apparatus and methane fermentation method Download PDF

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JP2010207700A
JP2010207700A JP2009055794A JP2009055794A JP2010207700A JP 2010207700 A JP2010207700 A JP 2010207700A JP 2009055794 A JP2009055794 A JP 2009055794A JP 2009055794 A JP2009055794 A JP 2009055794A JP 2010207700 A JP2010207700 A JP 2010207700A
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methane fermentation
membrane
tank
membrane permeate
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Tomoko Matsuzaki
智子 松▲崎▼
Toshihiro Komatsu
敏宏 小松
Junji Akita
淳司 秋田
Tetsuya Yamamoto
哲也 山本
Shinichiro Wakahara
慎一郎 若原
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Kubota Corp
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    • 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
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Abstract

<P>PROBLEM TO BE SOLVED: To provide a methane fermentation apparatus of low cost, suppressing deposition of MAP (magnesium ammonium phosphate) in a membrane permeation liquid leading out pipe, while keeping the inside of a methane fermentation tank at an appropriate pH value suited to methane fermentation. <P>SOLUTION: The methane fermentation apparatus 11 is provided wherein organic substances having higher temperature than digested sludge in the methane fermentation tank 12 and liquefied to be dissolvable is fed to the methane fermentation tank 12, and the digested sludge in the methane fermentation tank 12 is condensed by a membrane separating means 13 to perform the methane fermentation. The apparatus 11 includes the membrane permeation liquid leading out pipe 30 for taking out the membrane permeation liquid having passed through a separation membrane 19 of the membrane separating means 13 to the outside, and a heat exchanging means heat-exchanging between the membrane permeation liquid flowing through the membrane permeation liquid leading out pipe 30 with an organic substance in a solubilization tank 15 for heating the membrane permeation liquid. A coil-like pipe 30a formed at a part of the membrane permeation liquid leading out pipe 30 is provided in the solubilization tank 15 as the heat exchanging means. <P>COPYRIGHT: (C)2010,JPO&INPIT

Description

本発明は、蒸留酒やアルコール製造工程からの蒸留廃液、食品工場廃棄物等のリン、マグネシウム、窒素分を多く含んだ高温の有機性物質をメタン発酵処理するメタン発酵処理装置およびメタン発酵処理方法に関する。   The present invention relates to a methane fermentation treatment apparatus and a methane fermentation treatment method for treating methane fermentation of high-temperature organic substances containing a large amount of phosphorus, magnesium, nitrogen, etc., such as distilled liquor from alcohol and alcohol production processes, food factory waste, etc. About.

従来、この種のメタン発酵処理装置としては、図５に示すように、メタン発酵槽５１内の消化汚泥を膜分離槽５３との間で循環しながら浸漬型の膜分離手段５２で濃縮してメタン発酵処理を行なうものがある。膜分離手段５２は膜分離槽５３内に設置され、膜分離槽５３はメタン発酵槽５１に連通している。メタン発酵槽５１の前段には可溶化槽５４が設置されている。また、メタン発酵槽５１の後段には、膜分離手段５２の分離膜を透過した膜透過液を生物処理する生物処理槽５５が設置されている。   Conventionally, as this type of methane fermentation treatment apparatus, as shown in FIG. 5, the digested sludge in the methane fermentation tank 51 is concentrated by the submerged membrane separation means 52 while circulating between the membrane separation tank 53. Some perform methane fermentation. The membrane separation means 52 is installed in the membrane separation tank 53, and the membrane separation tank 53 communicates with the methane fermentation tank 51. A solubilization tank 54 is installed in the preceding stage of the methane fermentation tank 51. Further, a biological treatment tank 55 for biologically treating the membrane permeate that has permeated through the separation membrane of the membrane separation means 52 is installed at the subsequent stage of the methane fermentation tank 51.

膜分離槽５３と生物処理槽５５との間には、膜透過液を膜分離手段５２から生物処理槽５５へ移送する膜透過液導出配管５６が設けられている。
これによると、可溶化槽５４において液状に可溶化された有機性物質は、メタン発酵槽５１に投入され、通常約３５〜６０℃の温度でメタン発酵処理される。メタン発酵槽５１内の消化汚泥は膜分離手段５２で固液分離されることで濃縮される。この際、膜分離手段５２の分離膜を透過した膜透過液は、吸引ポンプ５７によって吸引され、膜透過液導出配管５６内を流れて生物処理槽５５に送られ、生物処理槽５５において生物処理された後、処理液として河川等に放流される。 Between the membrane separation tank 53 and the biological treatment tank 55, a membrane permeate outlet piping 56 for transferring the membrane permeate from the membrane separation means 52 to the biological treatment tank 55 is provided.
According to this, the organic substance solubilized in a liquid state in the solubilization tank 54 is put into the methane fermentation tank 51, and usually subjected to methane fermentation at a temperature of about 35 to 60 ° C. Digested sludge in the methane fermentation tank 51 is concentrated by solid-liquid separation by the membrane separation means 52. At this time, the membrane permeate that has passed through the separation membrane of the membrane separation means 52 is sucked by the suction pump 57, flows through the membrane permeate outlet piping 56, is sent to the biological treatment tank 55, and is biologically treated in the biological treatment tank 55. After that, it is discharged as a treatment liquid into a river or the like.

また、有機性物質としては例えば焼酎やウイスキー等の蒸留酒を造る際に発生する蒸留廃液等があるが、このような蒸留廃液は、通常約７０〜８０℃の温度を有し、リン、マグネシウム等の無機分と窒素の含有率が高く、メタン発酵処理工程中でリン酸マグネシウムアンモニウム（以下、ＭＡＰと略記する）が生成し易くなる。特に、膜透過液導出配管５６においては膜透過液が外気により冷却されるため、膜透過液導出配管５６の内周面にＭＡＰの無機結晶が生成し易い環境となり、この無機結晶が次第に成長して膜透過液導出配管５６が閉塞するといった問題がある。   In addition, examples of the organic substance include a distillation waste liquid generated when making distilled spirits such as shochu and whiskey. Such a distillation waste liquid usually has a temperature of about 70 to 80 ° C., and contains phosphorus, magnesium. The content of the inorganic components such as nitrogen and nitrogen is high, and magnesium ammonium phosphate (hereinafter abbreviated as MAP) is easily generated during the methane fermentation treatment step. In particular, in the membrane permeate outlet piping 56, the membrane permeate is cooled by outside air, so that an environment in which inorganic crystals of MAP are easily generated on the inner peripheral surface of the membrane permeate outlet piping 56 is formed, and this inorganic crystal grows gradually. Therefore, there is a problem that the membrane permeate outlet piping 56 is blocked.

このような問題の対策として、ＭＡＰの無機結晶の生成を抑制するために、塩鉄等の薬剤を多量にメタン発酵槽５１内に添加している。
また、下記特許文献１には、メタン発酵槽内の消化汚泥の一部を引き抜き、濃縮機で濃縮し、濃縮機の濃縮分離液を処理水として下水道等へ放流することが記載されており、さらには、濃縮分離液の移送配管中にＭＡＰの結晶が析出する場合、濃縮分離液に水道水、工業用水、下水二次処理水等を導入して濃度を下げ、ＭＡＰの析出を抑制する点が記載されている。 As a countermeasure for such a problem, a large amount of a chemical such as iron salt is added to the methane fermenter 51 in order to suppress the formation of inorganic crystals of MAP.
Patent Document 1 below describes that a part of the digested sludge in the methane fermentation tank is drawn out, concentrated with a concentrator, and the concentrated separation liquid of the concentrator is discharged into sewers as treated water. Furthermore, when MAP crystals are precipitated in the concentrated separation liquid transfer pipe, tap water, industrial water, secondary treated water, etc. are introduced into the concentrated separation liquid to lower the concentration and suppress MAP precipitation. Is described.

特開２００５−１９９２５８JP-A-2005-199258

しかしながら上記図５に示した従来形式では、薬剤の添加に要するコストが高いといった問題や、或いは、薬剤の添加によってメタン発酵槽５１内のｐＨが変動し、メタン発酵槽５１内をメタン発酵に最適なｐＨに維持することが困難になるといった問題がある。   However, in the conventional format shown in FIG. 5 above, there is a problem that the cost required for the addition of the chemical is high, or the pH in the methane fermentation tank 51 fluctuates due to the addition of the chemical, and the inside of the methane fermentation tank 51 is optimal for methane fermentation. There is a problem that it is difficult to maintain a stable pH.

また、上記特許文献１に示したものでは、濃縮分離液に水道水、工業用水、下水二次処理水等を導入することにより、濃縮分離液を薄めて濃縮分離液に含まれるアンモニアやリン等の濃度を下げているため、濃縮分離液の量が大幅に変動してしまうという問題がある。   Moreover, in what was shown in the said patent document 1, by introduce | transducing tap water, industrial water, a sewage secondary-treatment water, etc. into a concentrated separation liquid, the concentrated separation liquid is diluted and ammonia, phosphorus, etc. which are contained in a concentrated separation liquid Therefore, there is a problem that the amount of the concentrated separation liquid greatly fluctuates.

本発明は、メタン発酵槽内をメタン発酵に適したｐＨに維持しつつ、膜透過液導出配管内におけるＭＡＰの析出を抑制することが可能な低コストのメタン発酵処理装置およびメタン発酵処理方法を提供することを目的とする。   The present invention provides a low-cost methane fermentation treatment apparatus and a methane fermentation treatment method capable of suppressing the precipitation of MAP in the membrane permeate outlet piping while maintaining the inside of the methane fermentation tank at a pH suitable for methane fermentation. The purpose is to provide.

上記目的を達成するために本第１発明は、消化汚泥中において有機性物質のメタン発酵処理を行なうメタン発酵槽と、流動性を有し且つメタン発酵槽内の消化汚泥よりも高温である有機性物質をメタン発酵槽に供給する原料供給手段と、膜分離手段を有し、
メタン発酵槽内の消化汚泥中の固形分を膜分離手段によって濃縮しながらメタン発酵処理を行なうメタン発酵処理装置であって、
膜分離手段の分離膜を透過した膜透過液を外部へ取り出す膜透過液導出配管と、膜透過液導出配管内を流れる膜透過液と原料供給手段によってメタン発酵槽に供給される有機性物質との間で熱交換を行なって膜透過液を加温する熱交換手段が備えられているものである。 In order to achieve the above object, the first invention is a methane fermentation tank for performing a methane fermentation treatment of an organic substance in digested sludge, and an organic solvent having fluidity and higher temperature than the digested sludge in the methane fermentation tank. A raw material supply means for supplying a sexual substance to a methane fermentation tank, and a membrane separation means,
A methane fermentation treatment apparatus for performing a methane fermentation treatment while concentrating solids in digested sludge in a methane fermentation tank by a membrane separation means,
A membrane permeate outlet pipe for taking out the membrane permeate permeated through the separation membrane of the membrane separator means, a membrane permeate flowing in the membrane permeate outlet pipe and an organic substance supplied to the methane fermentation tank by the raw material supply means; Heat exchange means for warming the membrane permeate by performing heat exchange between the two.

これによると、高温で且つ液状に可溶化された有機性物質は、原料供給手段によってメタン発酵槽に供給され、メタン発酵槽内でメタン発酵処理される。また、メタン発酵槽内の消化汚泥は膜分離手段により濃縮される。この際、膜分離手段の分離膜を透過した膜透過液は膜透過液導出配管内を流れて外部へ取り出される。   According to this, the organic substance solubilized at high temperature and in a liquid state is supplied to the methane fermentation tank by the raw material supply means, and is subjected to methane fermentation treatment in the methane fermentation tank. The digested sludge in the methane fermentation tank is concentrated by membrane separation means. At this time, the membrane permeate that has passed through the separation membrane of the membrane separation means flows through the membrane permeate outlet pipe and is taken out to the outside.

このとき、熱交換手段が膜透過液導出配管内を流れる膜透過液とメタン発酵槽に供給される高温の有機性物質との間で熱交換を行なって膜透過液を加温することにより、膜透過液導出配管内の膜透過液の温度低下に伴うＭＡＰの溶解度積の減少が抑制されるため、ＭＡＰの無機結晶が析出し難い環境となり、膜透過液導出配管の内周面にＭＡＰが析出するのを抑制することができる。   At this time, the heat exchange means performs heat exchange between the membrane permeate flowing in the membrane permeate outlet piping and the high-temperature organic substance supplied to the methane fermentation tank to heat the membrane permeate, Since the decrease in the solubility product of MAP accompanying the decrease in the temperature of the membrane permeate in the membrane permeate outlet pipe is suppressed, it becomes an environment in which inorganic crystals of MAP hardly precipitate, and MAP is formed on the inner peripheral surface of the membrane permeate outlet pipe. Precipitation can be suppressed.

これにより、塩鉄等の薬剤の添加量（使用量）を大幅に削減することができるため、コストを低減することが可能であり、さらに、容易にメタン発酵槽内をメタン発酵に最適なｐＨに維持することができる。   As a result, the amount of chemicals such as iron salt (the amount used) can be significantly reduced, which can reduce the cost, and the pH within the methane fermentation tank can be easily optimized for methane fermentation. Can be maintained.

また、メタン発酵槽に供給される高温の有機性物質の温度を利用して膜透過液を加温するため、有機性物質の温度を有効に利用でき、さらにコストを低減することができる。
本第２発明は、原料供給手段は有機性物質を液状又はスラリー状に可溶化させる可溶化槽を有し、
熱交換手段は膜透過液導出配管が可溶化槽内を通過する構成を有するものである。 Moreover, since the membrane permeate is heated using the temperature of the high-temperature organic substance supplied to the methane fermentation tank, the temperature of the organic substance can be used effectively, and the cost can be further reduced.
In the second invention, the raw material supply means has a solubilization tank for solubilizing the organic substance in a liquid or slurry state,
The heat exchange means has a configuration in which the membrane permeate outlet piping passes through the solubilization tank.

これによると、膜透過液が膜透過液導出配管内を流れて外部へ取り出される際、膜透過液導出配管内の膜透過液と可溶化槽内に貯留された高温の有機性物質との間で熱交換が行なわれて膜透過液が加温される。これにより、膜透過液導出配管内の膜透過液の温度低下が抑制される。   According to this, when the membrane permeate flows through the membrane permeate outlet piping and is taken out to the outside, it is between the membrane permeate in the membrane permeate outlet and the high temperature organic substance stored in the solubilization tank. Then, heat exchange is performed and the membrane permeate is heated. Thereby, the temperature fall of the membrane permeate in the membrane permeate outlet pipe is suppressed.

本第３発明は、原料供給手段は流動性を有する有機性物質を貯留する貯留槽を有し、
熱交換手段は膜透過液導出配管が貯留槽内を通過する構成を有するものである。
これによると、膜透過液が膜透過液導出配管内を流れて外部へ取り出される際、膜透過液導出配管内の膜透過液と貯留槽内に貯留された高温の有機性物質との間で熱交換が行なわれて膜透過液が加温される。 In the third aspect of the present invention, the raw material supply means has a storage tank for storing an organic substance having fluidity,
The heat exchange means has a configuration in which the membrane permeate outlet piping passes through the storage tank.
According to this, when the membrane permeate flows through the membrane permeate outlet piping and is taken out to the outside, between the membrane permeate in the membrane permeate outlet and the high temperature organic substance stored in the storage tank. Heat exchange is performed to warm the membrane permeate.

本第４発明は、原料供給手段は流動性を有する有機性物質をメタン発酵槽に供給する原料供給配管を有し、
熱交換手段は膜透過液導出配管と原料供給配管とが当接する構成を有するものである。 In the fourth invention, the raw material supply means has a raw material supply pipe for supplying a fluid organic substance to the methane fermentation tank,
The heat exchange means has a configuration in which the membrane permeate outlet piping and the raw material supply piping abut.

これによると、膜透過液が膜透過液導出配管内を流れて外部へ取り出される際、膜透過液導出配管内の膜透過液と原料供給配管内の高温の有機性物質との間で熱交換が行なわれて膜透過液が加温される。これにより、膜透過液導出配管内の膜透過液の温度低下が抑制される。   According to this, when the membrane permeate flows through the membrane permeate outlet pipe and is taken out to the outside, heat exchange is performed between the membrane permeate in the membrane permeate outlet pipe and the high-temperature organic substance in the raw material supply pipe. Is performed to warm the membrane permeate. Thereby, the temperature fall of the membrane permeate in the membrane permeate outlet pipe is suppressed.

本第５発明は、熱交換手段は、熱媒を介して、膜透過液と原料供給手段によってメタン発酵槽に供給される有機性物質との間で熱交換を行なうものである。
これによると、膜透過液が膜透過液導出配管内を流れて外部へ取り出される際、膜透過液導出配管内の膜透過液とメタン発酵槽に供給される高温の有機性物質との間で、熱媒を介して、熱交換が行なわれ、膜透過液が加温される。これにより、膜透過液導出配管内の膜透過液の温度低下が抑制される。 In the fifth aspect of the invention, the heat exchange means exchanges heat between the membrane permeate and the organic material supplied to the methane fermentation tank by the raw material supply means via a heat medium.
According to this, when the membrane permeate flows through the membrane permeate outlet piping and is taken out to the outside, between the membrane permeate in the membrane permeate outlet and the high temperature organic substance supplied to the methane fermentation tank Then, heat exchange is performed via the heat medium, and the membrane permeate is heated. Thereby, the temperature fall of the membrane permeate in the membrane permeate outlet pipe is suppressed.

本第６発明は、メタン発酵槽に、メタン発酵槽内の消化汚泥よりも高温で且つ液状に可溶化された有機性物質を供給し、メタン発酵槽内の消化汚泥を膜分離手段によって濃縮しながらメタン発酵処理を行なうメタン発酵処理方法であって、
膜分離手段の分離膜を透過して膜透過液導出配管内を流れる膜透過液とメタン発酵槽に供給される有機性物質との間で熱交換を行なって膜透過液を加温するものである。 In the sixth aspect of the present invention, an organic substance that is solubilized in liquid form at a higher temperature than the digested sludge in the methane fermenter is supplied to the methane fermenter, and the digested sludge in the methane fermenter is concentrated by membrane separation means. A methane fermentation treatment method for performing methane fermentation treatment while
The membrane permeate is heated by exchanging heat between the membrane permeate passing through the separation membrane of the membrane separation means and flowing in the membrane permeate outlet piping and the organic substance supplied to the methane fermentation tank. is there.

以上のように本発明によれば、メタン発酵槽内をメタン発酵に適したｐＨに維持しつつ、低コストで、膜透過液導出配管内におけるＭＡＰの析出を抑制することが可能である。   As described above, according to the present invention, it is possible to suppress the precipitation of MAP in the membrane permeate outlet piping at low cost while maintaining the inside of the methane fermentation tank at a pH suitable for methane fermentation.

本発明の第１の実施の形態におけるメタン発酵処理装置の図である。It is a figure of the methane fermentation processing apparatus in the 1st Embodiment of this invention. 本発明の第２の実施の形態におけるメタン発酵処理装置の図である。It is a figure of the methane fermentation processing apparatus in the 2nd Embodiment of this invention. 本発明の第３の実施の形態におけるメタン発酵処理装置の図である。It is a figure of the methane fermentation processing apparatus in the 3rd Embodiment of this invention. 本発明の第４の実施の形態におけるメタン発酵処理装置の図である。It is a figure of the methane fermentation processing apparatus in the 4th Embodiment of this invention. 従来のメタン発酵処理装置の図である。It is a figure of the conventional methane fermentation processing apparatus.

以下、本発明における第１の実施の形態を、図１を参照しながら説明する。
１１は、メタン発酵槽１２内の消化汚泥を浸漬型の膜分離手段１３で固液分離して濃縮しながらメタン発酵処理を行なうメタン発酵処理装置である。メタン発酵処理装置１１は、メタン発酵槽１２内の消化汚泥よりも高温で且つ流動性を有する有機性物質をメタン発酵槽１２に供給する原料供給手段１４を有している。 Hereinafter, a first embodiment of the present invention will be described with reference to FIG.
11 is a methane fermentation treatment apparatus that performs methane fermentation treatment while concentrating the digested sludge in the methane fermentation tank 12 by solid-liquid separation by the submerged membrane separation means 13. The methane fermentation treatment apparatus 11 has raw material supply means 14 for supplying an organic substance having a higher temperature and fluidity than the digested sludge in the methane fermentation tank 12 to the methane fermentation tank 12.

原料供給手段１４は、メタン発酵槽１２の前段に設置され且つ上記高温の有機性物質を液状又はスラリー状に可溶化させる可溶化槽１５と、メタン発酵槽１２と可溶化槽１５とに連通する原料供給配管１６と、原料供給配管１６に設けられた供給ポンプ１７とを有している。   The raw material supply means 14 is installed in the front | former stage of the methane fermentation tank 12, and is connected to the solubilization tank 15 which solubilizes the said high temperature organic substance in a liquid form or a slurry form, and the methane fermentation tank 12 and the solubilization tank 15. A raw material supply pipe 16 and a supply pump 17 provided in the raw material supply pipe 16 are provided.

また、メタン発酵槽１２の後段には、膜分離手段１３の分離膜１９を透過した膜透過液を生物処理する生物処理槽２０が設置されている。生物処理槽２０は脱窒素槽２１と硝化槽２２とを有している。硝化槽２２には曝気手段２３が設けられている。   Further, a biological treatment tank 20 for biologically treating the membrane permeate that has permeated through the separation membrane 19 of the membrane separation means 13 is installed at the subsequent stage of the methane fermentation tank 12. The biological treatment tank 20 has a denitrification tank 21 and a nitrification tank 22. The nitrification tank 22 is provided with aeration means 23.

膜分離手段１３は、メタン発酵槽１２に連通する膜分離槽２５内に設けられており、所定間隔をあけて平行に配列された複数枚の平板状の膜カートリッジを鉛直方向に配置し、各膜カートリッジの相互間に流路を形成したものである。各膜カートリッジは、濾板の両面に分離膜１９（濾過膜）を配置している。   The membrane separation means 13 is provided in a membrane separation tank 25 communicating with the methane fermentation tank 12, and a plurality of flat plate membrane cartridges arranged in parallel with a predetermined interval are arranged in the vertical direction. A flow path is formed between the membrane cartridges. Each membrane cartridge has a separation membrane 19 (filtration membrane) disposed on both sides of the filter plate.

また、膜分離槽２５内には、メタン発酵槽１２内のバイオガスを膜分離手段１３の下方から散気する散気手段２６が設けられている。尚、メタン発酵槽１２内のバイオガスを散気手段２６へ供給するガス供給流路２７には、ブロワ装置２８が設けられている。   Further, in the membrane separation tank 25, an aeration means 26 for diffusing the biogas in the methane fermentation tank 12 from below the membrane separation means 13 is provided. A blower device 28 is provided in the gas supply passage 27 for supplying the biogas in the methane fermentation tank 12 to the aeration means 26.

膜分離手段１３と生物処理槽２０との間には、膜分離手段１３の分離膜１９を透過した膜透過液を膜分離手段１３から外部の脱窒素槽２１へ取り出す膜透過液導出配管３０が設けられている。膜透過液導出配管３０の一端は膜カートリッジに形成された透過液流路に連通し、他端は脱窒素槽２１に連通している。   Between the membrane separation means 13 and the biological treatment tank 20, there is a membrane permeate outlet pipe 30 for taking out the membrane permeate that has permeated the separation membrane 19 of the membrane separation means 13 from the membrane separation means 13 to the external denitrification tank 21. Is provided. One end of the membrane permeate outlet pipe 30 communicates with a permeate channel formed in the membrane cartridge, and the other end communicates with the denitrification tank 21.

膜透過液導出配管３０は、可溶化槽１５内の底部に設けられたコイル状の第１の管部３０ａと、膜カートリッジの透過液流路と第１の管部３０ａの一端とに連通する第２の管部３０ｂと、第１の管部３０ａの他端と脱窒素槽２１とに連通する第３の管部３０ｃとを有している。尚、第１の管部３０ａは、膜透過液導出配管３０内を流れる膜透過液と原料供給手段１４によってメタン発酵槽１２に供給される高温の有機性物質との間で熱交換を行なって膜透過液を加温する熱交換手段の一例であり、膜透過液導出配管３０の一部を可溶化槽１５内に通した構成に該当する。   The membrane permeate outlet pipe 30 communicates with the coiled first tube portion 30a provided at the bottom of the solubilization tank 15, the permeate flow path of the membrane cartridge, and one end of the first tube portion 30a. It has the 2nd pipe part 30b, and the 3rd pipe part 30c connected to the other end of the 1st pipe part 30a, and the denitrification tank 21. The first pipe portion 30a exchanges heat between the membrane permeate flowing in the membrane permeate outlet piping 30 and the high-temperature organic substance supplied to the methane fermentation tank 12 by the raw material supply means 14. This is an example of heat exchange means for heating the membrane permeate, and corresponds to a configuration in which a part of the membrane permeate outlet pipe 30 is passed through the solubilization tank 15.

また、膜透過液導出配管３０の第２の管部３０ｂには吸引ポンプ３２が介装され、膜分離手段１３は、吸引ポンプ３２によって、メタン発酵槽１２内の消化汚泥を吸引濾過するものである。   Further, a suction pump 32 is interposed in the second pipe portion 30b of the membrane permeate discharge pipe 30, and the membrane separation means 13 suctions and filters the digested sludge in the methane fermentation tank 12 by the suction pump 32. is there.

以下、上記構成における作用を説明する。
有機性物質は、可溶化槽１５に投入され、可溶化槽１５内で液状（又はスラリー状）に可溶化された後、可溶化槽１５から原料供給配管１６を流れてメタン発酵槽１２内へ供給され、メタン発酵槽１２内でメタン発酵処理される。また、メタン発酵槽１２内の消化汚泥は膜分離手段１３で固液分離されて固形分が濃縮される。この際、膜分離手段１３の分離膜１９を透過した膜透過液は、吸引ポンプ３２によって吸引され、膜透過液導出配管３０内を流れて脱窒素槽２１と硝化槽２２で生物処理された後、処理液として河川等に放流される。 Hereinafter, the operation of the above configuration will be described.
The organic substance is charged into the solubilization tank 15 and solubilized in a liquid (or slurry) form in the solubilization tank 15, and then flows from the solubilization tank 15 through the raw material supply pipe 16 into the methane fermentation tank 12. The methane fermentation process is performed in the methane fermentation tank 12. Further, the digested sludge in the methane fermentation tank 12 is solid-liquid separated by the membrane separation means 13 and the solid content is concentrated. At this time, the membrane permeate that has permeated through the separation membrane 19 of the membrane separation means 13 is sucked by the suction pump 32, flows through the membrane permeate discharge pipe 30, and is biologically treated in the denitrification tank 21 and the nitrification tank 22. Then, it is discharged into a river as a treatment liquid.

尚、有機性物質としては例えば焼酎やウイスキー等の蒸留酒を造る際に発生する蒸留廃液等があり、このような蒸留廃液は、通常約７０〜８０℃の温度を有した状態で可溶化槽１５に投入される。また、メタン発酵槽１２内の消化汚泥の温度は約３５〜６０℃の範囲内で保持され、メタン発酵槽１２に供給される有機性物質の温度はメタン発酵槽１２内の消化汚泥の温度よりも高温である。尚、メタン発酵槽１２と可溶化槽１５とは、保温材で保温或いはヒーター等で加温されている。   In addition, as an organic substance, there exist distillation waste liquid etc. which generate | occur | produce, for example, when making distilled spirits, such as shochu and whiskey, and such a distillation waste liquid is a solubilization tank in the state which usually has a temperature of about 70-80 degreeC. 15 is input. Moreover, the temperature of the digested sludge in the methane fermentation tank 12 is maintained within a range of about 35 to 60 ° C., and the temperature of the organic substance supplied to the methane fermentation tank 12 is higher than the temperature of the digested sludge in the methane fermentation tank 12. Is also hot. In addition, the methane fermentation tank 12 and the solubilization tank 15 are heated with a heat insulating material or heated with a heater or the like.

上記のような高温の有機性物質をメタン発酵処理する際、上記膜透過液は、膜透過液導出配管３０の第２の管部３０ｂから第１の管部３０ａを経て第３の管部３０ｃへ流れるのであるが、このとき、可溶化槽１５内の有機性物質の温度が第１の管部３０ａ内を流れる膜透過液の温度よりも高温であるため、第１の管部３０ａ内を流れる膜透過液と可溶化槽１５内の高温の有機性物質との間で熱交換が行なわれて、第１の管部３０ａ内の膜透過液が加温される。   When the high-temperature organic substance as described above is subjected to methane fermentation, the membrane permeate passes from the second pipe part 30b of the membrane permeate outlet pipe 30 through the first pipe part 30a to the third pipe part 30c. At this time, since the temperature of the organic substance in the solubilization tank 15 is higher than the temperature of the membrane permeate flowing in the first pipe part 30a, the inside of the first pipe part 30a is Heat exchange is performed between the flowing membrane permeate and the high-temperature organic substance in the solubilization tank 15 to heat the membrane permeate in the first pipe portion 30a.

これにより、膜透過液導出配管３０内の膜透過液の温度低下が抑制されて、それに伴いＭＡＰの溶解度積の減少が抑制されるため（尚、ＭＡＰの溶解度積は温度が低いほど小さくなる）、ＭＡＰの無機結晶が析出し難い環境となり、膜透過液導出配管３０の内周面にＭＡＰが析出するのを抑制することができる。   As a result, a decrease in the temperature of the membrane permeate in the membrane permeate outlet pipe 30 is suppressed, and accordingly, a decrease in the solubility product of MAP is suppressed (note that the solubility product of MAP decreases as the temperature decreases). , It becomes an environment in which inorganic crystals of MAP are difficult to precipitate, and it is possible to suppress the precipitation of MAP on the inner peripheral surface of the membrane permeate outlet pipe 30.

これにより、塩鉄等の薬剤の添加量（使用量）を大幅に削減することができるため、コストを低減することが可能であり、さらに、容易にメタン発酵槽１２内をメタン発酵に最適なｐＨに維持することができる。   Thereby, since the addition amount (use amount) of chemical | medical agents, such as salt iron, can be reduced significantly, it is possible to reduce cost, and also the inside of the methane fermentation tank 12 is easily optimal for methane fermentation. The pH can be maintained.

また、メタン発酵槽１２に供給される高温の有機性物質の温度を利用して膜透過液を加温するため、有機性物質の本来の温度を有効に利用でき、さらにコストを低減することができる。   Moreover, since the membrane permeate is heated using the temperature of the high-temperature organic substance supplied to the methane fermentation tank 12, the original temperature of the organic substance can be used effectively, and the cost can be further reduced. it can.

上記第１の実施の形態では、図１に示すように、原料供給手段１４は、可溶化槽１５を有しているが、原料の有機性物質が流動性を有している場合には、可溶化槽１５に替えて、有機性物質を貯留する貯留槽３３を有するものであってもよい。この場合も同様に、膜透過液導出配管３０の第１の管部３０ａが貯留槽３３内の底部に設けられており、膜透過液と貯留槽３３内の有機性物質との間で熱交換を行なってもよい。或いは、貯留槽３３を可溶化槽１５の前段又は後段に配置してもよい。   In the first embodiment, as shown in FIG. 1, the raw material supply means 14 has a solubilization tank 15, but when the organic substance of the raw material has fluidity, It may replace with the solubilization tank 15 and may have the storage tank 33 which stores an organic substance. In this case as well, the first pipe portion 30 a of the membrane permeate discharge pipe 30 is provided at the bottom of the storage tank 33, and heat exchange is performed between the membrane permeate and the organic substance in the storage tank 33. May be performed. Or you may arrange | position the storage tank 33 in the front | former stage or back | latter stage of the solubilization tank 15. FIG.

次に、本発明における第２の実施の形態を、図２を参照しながら説明する。
膜透過液導出配管３０は、原料供給配管１６内に挿入された管状の第１の管部３０ａと、膜カートリッジの透過液流路と第１の管部３０ａの一端とに連通する第２の管部３０ｂと、第１の管部３０ａの他端と脱窒素槽２１とに連通する第３の管部３０ｃとを有している。熱交換手段３４は、上記内管側の第１の管部３０ａと外管側の原料供給配管１６とによって、膜透過液導出配管３０の一部を原料供給配管１６内に通した二重管構造を有して構成される。この熱交換手段３４によって、膜透過液導出配管３０内を流れる膜透過液と原料供給手段１４によってメタン発酵槽１２に供給される高温の有機性物質との間で熱交換が行なわれて膜透過液が加温される。 Next, a second embodiment of the present invention will be described with reference to FIG.
The membrane permeate outlet pipe 30 is a second pipe portion 30a inserted into the raw material supply pipe 16, and a second permeate passage of the membrane cartridge and one end of the first pipe portion 30a. It has a pipe part 30b and a third pipe part 30c communicating with the other end of the first pipe part 30a and the denitrification tank 21. The heat exchanging means 34 is a double pipe in which a part of the membrane permeate outlet pipe 30 is passed through the raw material supply pipe 16 by the first pipe portion 30a on the inner pipe side and the raw material supply pipe 16 on the outer pipe side. It has a structure. The heat exchange means 34 exchanges heat between the membrane permeate flowing in the membrane permeate outlet piping 30 and the high-temperature organic substance supplied to the methane fermentation tank 12 by the raw material supply means 14 to allow the membrane permeation. The liquid is warmed.

以下、上記構成における作用を説明する。
膜透過液は、膜透過液導出配管３０の第２の管部３０ｂから第１の管部３０ａを経て第３の管部３０ｃへ流れるのであるが、このとき、原料供給配管１６内を流れる流動性を有する有機性物質の温度が第１の管部３０ａ内を流れる膜透過液の温度よりも高温であるため、第１の管部３０ａ内を流れる膜透過液と原料供給配管１６内の高温の有機性物質との間で熱交換が行なわれて、第１の管部３０ａ内の膜透過液が加温される。 Hereinafter, the operation of the above configuration will be described.
The membrane permeate flows from the second pipe part 30b of the membrane permeate outlet pipe 30 to the third pipe part 30c through the first pipe part 30a. At this time, the flow that flows in the raw material supply pipe 16 Since the temperature of the organic substance having the property is higher than the temperature of the membrane permeate flowing in the first pipe 30a, the temperature of the membrane permeate flowing in the first pipe 30a and the raw material supply pipe 16 is high. Heat exchange is performed with the organic substance, and the membrane permeate in the first tube portion 30a is heated.

これにより、膜透過液導出配管３０内の膜透過液の温度低下が抑制されて、ＭＡＰの溶解度積の減少が抑制されるため、ＭＡＰの無機結晶が析出し難い環境となり、膜透過液導出配管３０の内周面にＭＡＰが析出するのを抑制することができる。   As a result, a decrease in the temperature of the membrane permeate in the membrane permeate outlet piping 30 is suppressed, and a decrease in the solubility product of MAP is suppressed, resulting in an environment in which inorganic crystals of MAP are difficult to precipitate. It is possible to suppress MAP from being deposited on the inner peripheral surface of 30.

上記第２の実施の形態では、メタン発酵槽１２と可溶化槽１５との間が原料供給配管１６を介して連通しているが、可溶化槽１５を設けず、可溶化行程が不要である液状（又はスラリー状）の有機性物質を原料供給配管１６からメタン発酵槽１２へ供給するメタン発酵処理装置に適用してもよい。   In the second embodiment, the methane fermentation tank 12 and the solubilization tank 15 communicate with each other via the raw material supply pipe 16, but the solubilization tank 15 is not provided and the solubilization process is unnecessary. You may apply to the methane fermentation processing apparatus which supplies a liquid (or slurry-like) organic substance to the methane fermentation tank 12 from the raw material supply piping 16. FIG.

上記第２の実施の形態では、膜透過液導出配管３０の一部３０ａを原料供給配管１６の内部に挿入したが、原料供給配管１６の一部を膜透過液導出配管３０の内部に挿入してもよい。   In the second embodiment, a part 30 a of the membrane permeate outlet pipe 30 is inserted into the raw material supply pipe 16, but a part of the raw material supply pipe 16 is inserted into the membrane permeate outlet pipe 30. May be.

次に、本発明における第３の実施の形態を、図３を参照しながら説明する。
熱交換手段３５は、膜透過液導出配管３０の一部３０ａの外周面と原料供給配管１６の一部１６ａの外周面とを当接させた状態で、原料供給配管１６の一部１６ａを膜透過液導出配管３０の一部３０ａの外周面に巻き付けた構成を有している。 Next, a third embodiment of the present invention will be described with reference to FIG.
The heat exchanging means 35 forms a part 16a of the raw material supply pipe 16 in a state where the outer peripheral surface of the part 30a of the membrane permeate discharge pipe 30 and the outer peripheral surface of the part 16a of the raw material supply pipe 16 are in contact with each other. The permeated liquid outlet pipe 30 has a configuration wound around the outer peripheral surface of a part 30a.

これによると、膜透過液導出配管３０内を流れる膜透過液と原料供給配管１６内の高温の有機性物質との間で熱交換が行なわれて、膜透過液導出配管３０内の膜透過液が加温される。   According to this, heat exchange is performed between the membrane permeate flowing in the membrane permeate outlet piping 30 and the high-temperature organic substance in the raw material supply pipe 16, and the membrane permeate in the membrane permeate outlet piping 30. Is warmed.

尚、上記第３の実施の形態では、原料供給配管１６の一部１６ａを膜透過液導出配管３０の一部３０ａの外周面に巻き付けたが、膜透過液導出配管３０の一部３０ａを原料供給配管１６の一部１６ａの外周面に巻き付けてもよい。   In the third embodiment, the part 16a of the raw material supply pipe 16 is wound around the outer peripheral surface of the part 30a of the membrane permeate outlet pipe 30, but the part 30a of the membrane permeate outlet pipe 30 is used as the raw material. You may wind around the outer peripheral surface of the part 16a of the supply piping 16. FIG.

次に、本発明における第４の実施の形態を、図４を参照しながら説明する。
原料供給手段１４は、可溶化槽１５と、原料供給配管１６と、供給ポンプ１７と、可溶化槽１５内に貯留された液状の有機性物質を底部から取り出して上部へ戻す外部循環配管３７と、外部循環配管３７に設けられた循環ポンプ３８とを有している。 Next, a fourth embodiment of the present invention will be described with reference to FIG.
The raw material supply means 14 includes a solubilization tank 15, a raw material supply pipe 16, a supply pump 17, and an external circulation pipe 37 that takes out a liquid organic substance stored in the solubilization tank 15 from the bottom and returns it to the top. And a circulation pump 38 provided in the external circulation pipe 37.

メタン発酵処理装置１１には熱交換器４１（熱交換手段の一例）が設けられており、熱交換器４１は、水（熱媒の一例）を介して、外部循環配管３７内の有機性物質と膜透過液導出配管３０内の膜透過液との間で熱交換を行なうものである。   The methane fermentation treatment apparatus 11 is provided with a heat exchanger 41 (an example of a heat exchange means), and the heat exchanger 41 is an organic substance in the external circulation pipe 37 via water (an example of a heat medium). Is exchanged with the membrane permeate in the membrane permeate outlet pipe 30.

すなわち、上記熱交換器４１は、内部に、水４１ａと、水４１ａが循環する循環流路４１ｂと、水４１ａを循環させるポンプ４１ｃとを有しており、水４１ａが外部循環配管３７の一部の外周と膜透過液導出配管３０の一部の外周との間で接触しながら循環流路４１ｂを循環することにより、熱交換を行なうものである。   That is, the heat exchanger 41 includes therein water 41 a, a circulation passage 41 b through which the water 41 a circulates, and a pump 41 c through which the water 41 a is circulated. Heat exchange is performed by circulating through the circulation passage 41b while contacting between the outer periphery of the part and the outer periphery of a part of the membrane permeate outlet pipe 30.

以下、上記構成における作用を説明する。
循環ポンプ３８を駆動することにより、可溶化槽１５内で液状（又はスラリー状）に可溶化された有機性物質が外部循環配管３７内を流れ、可溶化槽１５内が攪拌される。このとき、外部循環配管３７内を流れる液状の有機性物質の温度が膜透過液導出配管３０内を流れる膜透過液の温度よりも高温であるため、膜透過液導出配管３０内の膜透過液と外部循環配管３７内の高温の有機性物質との間で、熱交換器４１の水４１ａ（熱媒）を介して、熱交換が行なわれ、膜透過液導出配管３０内の膜透過液が加温される。これにより、膜透過液導出配管３０内の膜透過液の温度低下が抑制されて、ＭＡＰの溶解度積の減少が抑制される。 Hereinafter, the operation of the above configuration will be described.
By driving the circulation pump 38, the organic substance solubilized in the liquid (or slurry) form in the solubilization tank 15 flows in the external circulation pipe 37 and the inside of the solubilization tank 15 is agitated. At this time, the temperature of the liquid organic substance flowing in the external circulation pipe 37 is higher than the temperature of the membrane permeate flowing in the membrane permeate outlet pipe 30, so the membrane permeate in the membrane permeate outlet pipe 30. And the high-temperature organic substance in the external circulation pipe 37 are subjected to heat exchange via the water 41a (heat medium) of the heat exchanger 41, and the membrane permeate in the membrane permeate lead-out pipe 30 is exchanged. It is warmed. Thereby, the temperature fall of the membrane permeate in the membrane permeate lead-out piping 30 is suppressed, and the decrease in the solubility product of MAP is suppressed.

上記第４の実施の形態では、熱交換器４１の熱媒の一例として水を用いたが、水に限定されるものではなく、例えば油やエチレングリコール等の液体を用いてもよい。
上記各実施の形態では、有機性物質と膜透過液との間で熱交換を行なって、温度が低下した高温の有機性物質を直接メタン発酵槽１２内に供給しているが、供給された高温の有機性物質がメタン発酵槽１２内の温度保持に悪影響を及ぼす場合には、熱交換手段の前段又は後段で放熱等により高温の有機性物質を適温まで冷却した後、メタン発酵槽１２に供給してもよい。 In the fourth embodiment, water is used as an example of the heat medium of the heat exchanger 41, but is not limited to water, and liquids such as oil and ethylene glycol may be used.
In each of the above embodiments, heat exchange is performed between the organic substance and the membrane permeate, and the high-temperature organic substance having a reduced temperature is directly supplied into the methane fermenter 12. When the high-temperature organic substance adversely affects the temperature maintenance in the methane fermentation tank 12, the high-temperature organic substance is cooled to an appropriate temperature by heat radiation or the like before or after the heat exchange means, and then the methane fermentation tank 12 You may supply.

１１ メタン発酵処理装置
１２ メタン発酵槽
１３ 膜分離手段
１４ 原料供給手段
１５ 可溶化槽
１６ 原料供給配管
１９ 分離膜
３０ 膜透過液導出配管
３０ａ 第１の管部（熱交換手段）
３３ 貯留槽
３４，３５ 熱交換手段
４１ 熱交換器（熱交換手段）
４１ａ 水（熱媒） DESCRIPTION OF SYMBOLS 11 Methane fermentation processing apparatus 12 Methane fermentation tank 13 Membrane separation means 14 Raw material supply means 15 Solubilization tank 16 Raw material supply piping 19 Separation membrane 30 Membrane permeate outlet piping 30a First pipe part (heat exchange means)
33 Storage tanks 34, 35 Heat exchange means 41 Heat exchanger (heat exchange means)
41a Water (heat medium)

Claims (6)

消化汚泥中において有機性物質のメタン発酵処理を行なうメタン発酵槽と、流動性を有し且つメタン発酵槽内の消化汚泥よりも高温である有機性物質をメタン発酵槽に供給する原料供給手段と、膜分離手段を有し、
メタン発酵槽内の消化汚泥中の固形分を膜分離手段によって濃縮しながらメタン発酵処理を行なうメタン発酵処理装置であって、
膜分離手段の分離膜を透過した膜透過液を外部へ取り出す膜透過液導出配管と、膜透過液導出配管内を流れる膜透過液と原料供給手段によってメタン発酵槽に供給される有機性物質との間で熱交換を行なって膜透過液を加温する熱交換手段が備えられていることを特徴とするメタン発酵処理装置。 A methane fermentation tank for performing methane fermentation of organic substances in the digested sludge, and a raw material supply means for supplying the methane fermentation tank with an organic substance having fluidity and higher temperature than the digested sludge in the methane fermentation tank. , Having membrane separation means,
A methane fermentation treatment apparatus for performing a methane fermentation treatment while concentrating solids in digested sludge in a methane fermentation tank by a membrane separation means,
A membrane permeate outlet pipe for taking out the membrane permeate permeated through the separation membrane of the membrane separator means, a membrane permeate flowing in the membrane permeate outlet pipe and an organic substance supplied to the methane fermentation tank by the raw material supply means; A methane fermentation treatment apparatus comprising heat exchange means for heating the membrane permeate by exchanging heat between the two. 原料供給手段は有機性物質を液状又はスラリー状に可溶化させる可溶化槽を有し、
熱交換手段は膜透過液導出配管が可溶化槽内を通過する構成を有することを特徴とする請求項１記載のメタン発酵処理装置。 The raw material supply means has a solubilization tank for solubilizing organic substances in liquid or slurry form,
The methane fermentation treatment apparatus according to claim 1, wherein the heat exchange means has a configuration in which the membrane permeate outlet piping passes through the solubilization tank. 原料供給手段は流動性を有する有機性物質を貯留する貯留槽を有し、
熱交換手段は膜透過液導出配管が貯留槽内を通過する構成を有することを特徴とする請求項１記載のメタン発酵処理装置。 The raw material supply means has a storage tank for storing an organic substance having fluidity,
The methane fermentation treatment apparatus according to claim 1, wherein the heat exchange means has a configuration in which the membrane permeate outlet piping passes through the storage tank. 原料供給手段は流動性を有する有機性物質をメタン発酵槽に供給する原料供給配管を有し、
熱交換手段は膜透過液導出配管と原料供給配管とが当接する構成を有することを特徴とする請求項１記載のメタン発酵処理装置。 The raw material supply means has a raw material supply pipe for supplying a fluid organic substance to the methane fermentation tank,
The methane fermentation treatment apparatus according to claim 1, wherein the heat exchange means has a configuration in which the membrane permeate discharge pipe and the raw material supply pipe come into contact with each other. 熱交換手段は、熱媒を介して、膜透過液と原料供給手段によってメタン発酵槽に供給される有機性物質との間で熱交換を行なうことを特徴とする請求項１記載のメタン発酵処理装置。 The methane fermentation treatment according to claim 1, wherein the heat exchange means exchanges heat between the membrane permeate and the organic material supplied to the methane fermentation tank by the raw material supply means via a heat medium. apparatus. メタン発酵槽に、メタン発酵槽内の消化汚泥よりも高温で且つ液状に可溶化された有機性物質を供給し、メタン発酵槽内の消化汚泥を膜分離手段によって濃縮しながらメタン発酵処理を行なうメタン発酵処理方法であって、
膜分離手段の分離膜を透過して膜透過液導出配管内を流れる膜透過液とメタン発酵槽に供給される有機性物質との間で熱交換を行なって膜透過液を加温することを特徴とするメタン発酵処理方法。 Supply organic substances that are solubilized in liquid form at a higher temperature than the digested sludge in the methane fermenter to the methane fermenter, and perform the methane fermentation process while concentrating the digested sludge in the methane fermenter by membrane separation means A methane fermentation treatment method,
The membrane permeate is heated by exchanging heat between the membrane permeate flowing through the separation membrane of the membrane separation means and flowing in the membrane permeate outlet pipe and the organic substance supplied to the methane fermentation tank. A characteristic methane fermentation treatment method.
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DE102012021086A1 (en) 2012-10-26 2014-04-30 Bauer Water GmbH System for sewage treatment, comprises buffer tank for storing waste water to be treated, bioreactor tank in which sewage is treated by microorganisms in bioreactor tank under anaerobic conditions and filter tank with filter medium
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JP2017170367A (en) * 2016-03-24 2017-09-28 日本プライスマネジメント株式会社 Methane fermentation system
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JP2022093738A (en) * 2017-07-31 2022-06-23 三菱化工機株式会社 Organic wastewater treatment apparatus and organic wastewater treatment method
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