JP2010179216A - Anaerobic digestion treatment method of organic sludge - Google Patents
Anaerobic digestion treatment method of organic sludge Download PDFInfo
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- 239000010802 sludge Substances 0.000 title claims abstract description 246
- 230000029087 digestion Effects 0.000 title claims abstract description 125
- 238000000034 method Methods 0.000 title claims abstract description 52
- 230000007928 solubilization Effects 0.000 claims abstract description 60
- 238000005063 solubilization Methods 0.000 claims abstract description 60
- 239000007787 solid Substances 0.000 claims abstract description 38
- 238000010438 heat treatment Methods 0.000 claims abstract description 12
- 238000001035 drying Methods 0.000 claims description 17
- 230000018044 dehydration Effects 0.000 claims description 6
- 238000006297 dehydration reaction Methods 0.000 claims description 6
- 230000006835 compression Effects 0.000 claims description 4
- 238000007906 compression Methods 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 2
- 238000001816 cooling Methods 0.000 abstract description 9
- 230000003381 solubilizing effect Effects 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 12
- 241000894006 Bacteria Species 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 244000005700 microbiome Species 0.000 description 4
- 238000003672 processing method Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 238000010335 hydrothermal treatment Methods 0.000 description 2
- 239000010801 sewage sludge Substances 0.000 description 2
- 230000009897 systematic effect Effects 0.000 description 2
- NAWXUBYGYWOOIX-SFHVURJKSA-N (2s)-2-[[4-[2-(2,4-diaminoquinazolin-6-yl)ethyl]benzoyl]amino]-4-methylidenepentanedioic acid Chemical compound C1=CC2=NC(N)=NC(N)=C2C=C1CCC1=CC=C(C(=O)N[C@@H](CC(=C)C(O)=O)C(O)=O)C=C1 NAWXUBYGYWOOIX-SFHVURJKSA-N 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000012809 cooling fluid Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 230000001568 sexual effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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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
- 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
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/20—Sludge processing
Abstract
Description
本発明は、有機性汚泥を嫌気性消化処理する方法に関し、特に、嫌気性消化処理するために循環される可溶化汚泥の熱量と固形分量を制御する方法に関する。 The present invention relates to a method for anaerobic digestion treatment of organic sludge, and more particularly to a method for controlling the amount of heat and solid content of solubilized sludge circulated for anaerobic digestion treatment.
下水汚泥、産業排水等の有機性汚泥を処理する方法として、メタン菌等の嫌気性微生物に消化させる嫌気性消化処理が挙げられる。そして、その嫌気性消化処理においては、嫌気性微生物が消化活動しやすくするため、有機性汚泥とメタン菌が投入された消化タンク内の温度を３０〜６０℃とすることが必要とされている。 As a method for treating organic sludge such as sewage sludge and industrial wastewater, anaerobic digestion treatment in which anaerobic microorganisms such as methane bacteria are digested is exemplified. And in the anaerobic digestion process, in order to make it easy for anaerobic microorganisms to digest, it is necessary to set the temperature in the digestion tank into which organic sludge and methane bacteria are thrown into 30-60 degreeC. .
ここで、従来、消化タンク内の温度を３０〜６０℃とするため、熱交換器を介して温水ボイラによって消化タンク内を加温しており、また、その温水ボイラの可燃燃料として、嫌気性消化処理によって発生したバイオガスが利用されていた。 Here, conventionally, in order to set the temperature in the digestion tank to 30 to 60 ° C., the digestion tank is heated by a hot water boiler through a heat exchanger, and anaerobic as a combustible fuel for the hot water boiler. Biogas generated by digestion was used.
一方、引用文献１の発明によれば、有機性汚泥を嫌気性消化処理する前に、有機性汚泥を水熱処理装置によって１５０〜３５０℃となるまで加熱し、有機性汚泥中の固形分の可溶化を行う可溶化処理方法が開示されている（引用文献１の明細書段落００１７と図１の「水熱処理装置９」参照。）。 On the other hand, according to the invention of Cited Document 1, before the organic sludge is subjected to the anaerobic digestion treatment, the organic sludge is heated to 150 to 350 ° C. by a hydrothermal treatment apparatus, and the solid content in the organic sludge can be adjusted. A solubilization method for solubilization is disclosed (see paragraph 0017 of the specification of cited document 1 and “hydrothermal treatment apparatus 9” in FIG. 1).
また、引用文献２の発明によれば、バイオガスの回収率の向上等を図るため、消化タンクにおいて嫌気性消化処理された有機性汚泥である消化汚泥を可溶化処理し、その可溶化処理された可溶化汚泥を消化タンクに循環して、嫌気性消化が未処理の有機性汚泥とともに、可溶化汚泥を嫌気性消化処理する方法が開示されている。 Further, according to the invention of Cited Document 2, in order to improve the recovery rate of biogas, etc., digested sludge, which is organic sludge that has been anaerobically digested in a digestion tank, is solubilized and solubilized. A method is disclosed in which the solubilized sludge is circulated to a digestion tank and the solubilized sludge is anaerobically digested together with the organic sludge that has not been subjected to anaerobic digestion.
しかしながら、引用文献１の発明によれば、可溶化処理された可溶化汚泥の温度は１５０〜３５０℃であり、嫌気性消化処理するためには、その可溶化汚泥の温度を下げる必要があった。つまり、引用文献１の発明によれば、可溶化した汚泥の温度を下げるための熱交換器等の冷却装置を設ける必要があり、設備の増加という問題を招いていた（引用文献１の「クーラ２０」と「冷却用熱媒流体２１」を参照。）。 However, according to the invention of Cited Document 1, the temperature of the solubilized sludge solubilized is 150 to 350 ° C., and in order to perform the anaerobic digestion treatment, the temperature of the solubilized sludge had to be lowered. . That is, according to the invention of Cited Document 1, it is necessary to provide a cooling device such as a heat exchanger for lowering the temperature of the solubilized sludge, which causes a problem of an increase in equipment (“Cooler of Cited Document 1”). 20 ”and“ Cooling fluid 21 for cooling ”).
また、引用文献２の発明によれば、嫌気性消化が未処理の有機性汚泥と可溶化汚泥とを混合した汚泥全体の温度が、嫌気性消化処理に必要とされる３０〜６０℃でない場合があった。
つまり、可溶化汚泥の熱量が大きいため、嫌気性消化される汚泥全体の温度が前記する嫌気性消化に必要な温度を超える場合は、可溶化汚泥を冷却するための熱交換器を設ける必要があった。一方、可溶化汚泥の熱量が小さいため、嫌気性消化される汚泥全体の温度が嫌気性消化に必要な温度に達していない場合には、熱交換器によって消化タンク内の温度を上昇させることが必要となり、加熱するための余分なエネルギーが必要となるという問題が生じていた。
Moreover, according to invention of the cited reference 2, when the temperature of the whole sludge which mixed the anaerobic digestion untreated organic sludge and the solubilized sludge is not 30-60 degreeC required for anaerobic digestion processing was there.
That is, since the amount of heat of the solubilized sludge is large, when the temperature of the entire sludge to be anaerobically digested exceeds the temperature required for the anaerobic digestion, it is necessary to provide a heat exchanger for cooling the solubilized sludge. there were. On the other hand, since the amount of heat of solubilized sludge is small, if the temperature of the whole sludge to be anaerobically digested does not reach the temperature required for anaerobic digestion, the temperature in the digestion tank may be increased by a heat exchanger. There is a problem that it is necessary and extra energy for heating is required.
他方、前記する問題に対し、嫌気性消化工程に必要な熱量となるように、消化タンク内に循環する可溶化汚泥の量を調整する方法が考えられるが、可溶化汚泥の量を調整すると、可溶化・嫌気性消化処理に必要とする可溶化汚泥中の固形分量の過不足が生じる場合がある。 On the other hand, for the above-mentioned problem, a method of adjusting the amount of solubilized sludge circulating in the digestion tank so that the amount of heat necessary for the anaerobic digestion step can be considered, but when adjusting the amount of solubilized sludge, The amount of solid content in the solubilized sludge required for the solubilization / anaerobic digestion treatment may occur.
前記問題に鑑みて、本発明は、可溶化汚泥を嫌気性消化処理する場合に熱交換器等の冷却設備が不要であって、かつ、可溶化汚泥を嫌気性消化処理する際に加熱するための余分なエネルギーを消費することなく、かつ、可溶化汚泥が可溶化・嫌気性消化処理に必要な固形分量を有することができる有機性汚泥の嫌気性消化処理方法を提供することを課題とする。 In view of the above problems, the present invention does not require a cooling facility such as a heat exchanger when anaerobic digestion of solubilized sludge, and heats the solubilized sludge when anaerobically digested. It is an object of the present invention to provide an anaerobic digestion method for organic sludge that does not consume excess energy of the solubilized sludge and has a solid content necessary for solubilization and anaerobic digestion. .
前記課題を解決するため、請求項１に記載の有機性汚泥の嫌気性処理方法は、消化タンクに投入される有機性汚泥を嫌気性消化処理して消化汚泥を生成する嫌気性消化工程と、前記消化汚泥を脱水処理して脱水汚泥を生成する脱水工程と、前記消化汚泥の一部と前記脱水汚泥の一部を可溶化タンクに供給する消化・脱水汚泥供給工程と、前記可溶化タンクで前記消化汚泥の一部と前記脱水汚泥の一部を加熱処理し可溶化させることで可溶化汚泥を生成する可溶化工程と、前記可溶化汚泥を前記消化タンクに循環させ、前記消化タンクに投入された前記有機性汚泥と混合させる可溶化汚泥循環工程と、を含む有機性汚泥の嫌気性消化処理方法であって、前記可溶化汚泥循環工程は、前記可溶化汚泥の処理温度に基づいて、消化タンクにおける嫌気性消化処理に必要とする熱量となるように、前記可溶化汚泥の循環量を設定し、前記消化・脱水汚泥供給工程は、前記可溶化汚泥循環工程において設定された前記可溶化汚泥の循環量に基づいて、前記可溶化汚泥が可溶化・嫌気性消化処理において必要とされる固形分量を有するように、可溶化タンクに供給する前記消化汚泥量と前記脱水汚泥量とを調整することを特徴とする In order to solve the above-mentioned problem, the anaerobic treatment method of organic sludge according to claim 1 comprises an anaerobic digestion step of producing an digested sludge by anaerobically digesting the organic sludge charged into the digestion tank; A dehydration step of dehydrating the digested sludge to produce a dehydrated sludge, a digestion / dehydrated sludge supply step of supplying a part of the digested sludge and a part of the dehydrated sludge to the solubilization tank, and the solubilization tank A solubilization step of generating a solubilized sludge by heat-treating and solubilizing a part of the digested sludge and a part of the dewatered sludge, circulating the solubilized sludge to the digestion tank, and charging the digestion tank A solubilized sludge circulation step for mixing with the organic sludge, and an anaerobic digestion treatment method for organic sludge, wherein the solubilized sludge circulation step is based on the treatment temperature of the solubilized sludge, Disgust in digestion tank The amount of circulation of the solubilized sludge is set so that the amount of heat required for the sexual digestion treatment is obtained, and the digestion / dehydrated sludge supply step is a circulation amount of the solubilized sludge set in the solubilized sludge circulation step. The amount of the digested sludge supplied to the solubilization tank and the amount of the dewatered sludge are adjusted so that the solubilized sludge has a solid content required in the solubilization / anaerobic digestion process. To
本発明によれば、可溶化汚泥循環工程において、消化タンクに循環される可溶化汚泥の熱量は、消化タンク内の有機性汚泥と可溶化汚泥とを併せた汚泥全体を嫌気性処理するのに必要な熱量と設定されているため、その可溶化汚泥を消化タンク内に循環させると、消化タンク内の汚泥全体の温度は、嫌気性消化処理を行う温度となる。従って、可溶化汚泥を冷却する必要や、消化タンク内の温度を上昇させる必要がないため、可溶化汚泥を冷却するための熱交換器が不要となり、消化タンク内の汚泥全体を加熱するための余分なエネルギーを消費することもない。 According to the present invention, in the solubilized sludge circulation process, the calorific value of the solubilized sludge circulated in the digestion tank is used to anaerobically treat the entire sludge combining the organic sludge and the solubilized sludge in the digestion tank. Since the required amount of heat is set, when the solubilized sludge is circulated in the digestion tank, the temperature of the entire sludge in the digestion tank becomes the temperature at which the anaerobic digestion treatment is performed. Therefore, since it is not necessary to cool the solubilized sludge or to increase the temperature in the digestion tank, there is no need for a heat exchanger for cooling the solubilized sludge, and for heating the entire sludge in the digestion tank. No extra energy is consumed.
また、消化・脱水汚泥供給工程において、可溶化汚泥が循環する量に基づいて、可溶化タンク内に供給する消化汚泥と脱水汚泥の量を調整することによって、その循環される可溶化汚泥中の可溶化に必要な固形分量を調整することが可能となるため、可溶化汚泥が可溶化・嫌気性消化処理に必要とする固形分量を含有することとなる。 Also, in the digestion / dewatered sludge supply process, by adjusting the amount of digested sludge and dewatered sludge supplied to the solubilization tank based on the amount of the solubilized sludge circulated, Since it is possible to adjust the amount of solids necessary for solubilization, the solubilized sludge contains the amount of solids necessary for solubilization and anaerobic digestion.
また、請求項２に記載の構成は、前記嫌気性消化工程において、前記有機性汚泥を嫌気性消化処理するときに、前記有機性汚泥の温度を３０〜６０℃に維持し、前記可溶化工程において、前記消化・脱水汚泥を加熱して可溶化処理するときの前記消化・脱水汚泥の温度を１２０〜２３０℃に維持することを特徴とする。 Moreover, the structure of Claim 2 maintains the temperature of the said organic sludge at 30-60 degreeC, when carrying out the anaerobic digestion process of the said organic sludge in the said anaerobic digestion process, The said solubilization process The temperature of the digested / dehydrated sludge during the solubilization treatment by heating the digested / dehydrated sludge is maintained at 120 to 230 ° C.
また、請求項３に記載の構成は、前記可溶化汚泥が可溶化・嫌気性消化処理において必要とされる固形分量は、消化タンクに投入される前記有機性汚泥の固形分量の３０〜８０％であることを特徴とする。
Further, in the configuration according to
また、請求項４に記載の構成は、脱水汚泥の残部を乾燥炉に流入させて、前記乾燥炉を間接加熱することにより乾燥処理する汚泥乾燥工程と、前記汚泥乾燥工程において前記乾燥炉内に生じた蒸気を圧縮し、前記可溶化タンクに圧縮された蒸気を供給する蒸気圧縮工程とを含み、前記蒸気圧縮工程により圧縮された蒸気を可溶化処理の加熱源とすることを特徴とする。 According to a fourth aspect of the present invention, there is provided a sludge drying process in which the remainder of the dewatered sludge is allowed to flow into a drying furnace and the drying furnace is indirectly heated to perform a drying process in the sludge drying process. A vapor compression step of compressing the generated vapor and supplying the vapor compressed to the solubilization tank, wherein the vapor compressed by the vapor compression step is used as a heat source for the solubilization process.
本発明によれば、可溶化汚泥を嫌気性消化処理させる場合に熱交換器等の冷却設備が不要であって、かつ、可溶化汚泥を嫌気性消化処理するとしても加熱するための余分なエネルギーを消費することなく、かつ、可溶化汚泥が可溶化・嫌気性消化処理に必要な固形分量を有することができる有機性汚泥の嫌気性消化処理方法を提供することができる。
また、本発明によれば、嫌気性消化工程に供給する可溶化汚泥を冷却するための熱交換器等の設備が不要となるため、スケールによる閉鎖等に対するメンテナンスが不要となり、労力削減が図れる。
According to the present invention, when the solubilized sludge is subjected to the anaerobic digestion treatment, a cooling facility such as a heat exchanger is unnecessary, and extra energy for heating even if the solubilized sludge is subjected to the anaerobic digestion treatment. It is possible to provide a method for anaerobic digestion treatment of organic sludge, which can consume the amount of solids necessary for solubilization and anaerobic digestion treatment without consuming soy.
Further, according to the present invention, since a facility such as a heat exchanger for cooling the solubilized sludge supplied to the anaerobic digestion step is not required, maintenance for closing by a scale is unnecessary, and labor can be reduced.
（有機性汚泥の嫌気性消化処理方法）
次に、本発明の実施形態に係る有機性汚泥の嫌気性消化処理方法の一例について、図１を用いて説明する。ここで、図1は有機性汚泥の嫌気性消化処理システムを示し、当該システムによって実施形態に係る有機性汚泥の嫌気性消化処理方法を実施する。
(Anaerobic digestion treatment method of organic sludge)
Next, an example of the anaerobic digestion method of organic sludge according to the embodiment of the present invention will be described with reference to FIG. Here, FIG. 1 shows an anaerobic digestion treatment system for organic sludge, and the organic sludge anaerobic digestion treatment method according to the embodiment is performed by the system.
実施形態に係る有機性汚泥の嫌気性消化処理方法は、下水汚泥等の有機性汚泥１００ａを嫌気性消化処理し、消化汚泥１００ｂを生成する嫌気性消化工程と、その生成された消化汚泥１００ｂを脱水処理し、脱水汚泥１００ｃを生成する脱水工程と、消化汚泥１００ｂの一部と脱水汚泥１００ｃの一部とを可溶化タンク４０に供給する消化・脱水汚泥供給工程と、可溶化タンク４０内に供給された消化汚泥１００ｂと脱水汚泥１００ｃとを可溶化処理する可溶化工程と、その可溶化汚泥１００ｄを、消化タンク１０に循環させる可溶化汚泥循環工程とからなる。
The method of anaerobic digestion treatment of organic sludge according to the embodiment comprises an anaerobic digestion process in which organic sludge 100a such as sewage sludge is anaerobically digested to produce digested sludge 100b, and the generated digested sludge 100b. In the solubilization tank 40, a dehydration process for dehydrating and generating the
（嫌気性消化工程）
嫌気性消化工程は、消化タンク１０内に投入される有機性汚泥１００ａを嫌気性消化処理する工程である。ここで、嫌気性消化処理は、有機性汚泥１００ａとメタン菌等の嫌気性微生物を消化タンク１０内に投入し、その消化タンク１０内の温度を３０〜６０℃として、７〜２０日間維持して行われる。これにより有機性汚泥１００ａ中の有機物が消化されて消化汚泥１００ｂが生成される。また、温度が３０〜６０℃であるのは、嫌気性微生物の活動が活発化されるためであって、好ましくは、３５〜５５℃とすることが望ましい。また、消化タンク１０内には、メタン菌等の消化によってメタンガス等のバイオガスを発生するが、このバイオガスは後述する可溶化タンク４０の加熱燃料とする。
尚、本発明によれば、有機性汚泥１００ａの他に、後述する可溶化汚泥１００ｄも消化タンク１０に循環されて嫌気性消化処理される。
(Anaerobic digestion process)
The anaerobic digestion step is an anaerobic digestion process of the organic sludge 100a put into the digestion tank 10. Here, the anaerobic digestion treatment is performed by introducing organic sludge 100a and anaerobic microorganisms such as methane bacteria into the digestion tank 10 and maintaining the temperature in the digestion tank 10 at 30 to 60 ° C. for 7 to 20 days. Done. Thereby, the organic substance in the organic sludge 100a is digested and the digested sludge 100b is produced | generated. The temperature is 30 to 60 ° C. because the activity of anaerobic microorganisms is activated, and preferably 35 to 55 ° C. Further, in the digestion tank 10, biogas such as methane gas is generated by digestion of methane bacteria and the like, and this biogas is used as a heating fuel for the solubilization tank 40 described later.
In addition, according to this invention, the solubilized sludge 100d mentioned later other than the organic sludge 100a is also circulated to the digestion tank 10, and is anaerobically digested.
（脱水工程）
脱水工程は、消化汚泥１００ｂを消化汚泥脱水機２０によって脱水する工程である。これによって、脱水汚泥１００ｃと脱水ろ液が生成されるが、脱水ろ液は図示しない晶析脱隣装置等によって脱隣され、あるいは直接下水処理の水処理工程に返送される。また、脱水汚泥１００ｃの一部は、後述する消化・脱水汚泥供給工程によって、可溶化タンク４０内に供給されるが、可溶化タンク４０に供給されない脱水汚泥１００ｃの残部は、例えば乾燥炉５０によって乾燥処理されるなどして処分される。
(Dehydration process)
The dewatering step is a step of dewatering the digested sludge 100b with the
（消化・脱水汚泥供給工程）
消化・脱水汚泥供給工程は、消化汚泥１００ｂの一部である消化汚泥１００ｂ１と脱水汚泥１００ｃの一部である脱水汚泥１００ｃ１を可溶化タンク４０内に供給する工程である。
ここで、可溶化汚泥１００ｄが可溶化タンク４０内で可溶化される際に必要とする固形分量を確保させるために、下記式（１）と式（２）の連立方程式によって、消化汚泥１００ｂ１の供給量と脱水汚泥１００ｃ１の供給量を設定する。
尚、式（１）と式（２）の単位が相違するが、通常、汚泥と排水の比重は１と考えるため、１Ｔ＝１ｍ３として、上記式（１）と式（２）から、消化汚泥１００ｂ１の供給量と脱水汚泥１００ｃ１の供給量を求める。
(Digestion / dehydrated sludge supply process)
The digested / dehydrated sludge supply step is a step of supplying the digested sludge 100b1 which is a part of the digested sludge 100b and the dehydrated sludge 100c1 which is a part of the
Here, in order to ensure the amount of solid content required when the solubilized sludge 100d is solubilized in the solubilization tank 40, the digested sludge 100b1 is expressed by the following simultaneous equations (1) and (2). The supply amount and the supply amount of the dewatered sludge 100c1 are set.
In addition, although the unit of Formula (1) and Formula (2) is different, since the specific gravity of sludge and waste water is normally considered to be 1, 1T = 1m 3 , the above formula (1) and formula (2) The supply amount of the sludge 100b1 and the supply amount of the dewatered sludge 100c1 are obtained.
尚、式（１）中におけるＱ１００ｂ１は消化汚泥１００ｂ１の供給量［ｍ３／日］を、Ｃ１００ｂ１は消化汚泥１００ｂ１中に含まれる固形分量の濃度［ｗｔ％］を示す。Ｑ１００ｃ１は脱水汚泥１００ｃ１の供給量［ｍ３／日］を示し、Ｃ１００ｃ１は脱水汚泥１００ｃ１中に含まれる固形分量の濃度［ｗｔ％］を示す。Ｑ１００ａは有機性汚泥１００ａの供給量［ｍ３／日］を示し、Ｃ１００ａは有機性汚泥中に含まれる固形分量の濃度［ｗｔ％］を示す。尚、［ｗｔ％］は、重量パーセントを示す。
Ｙは、可溶化タンク４０へ供給する可溶化汚泥１００ｄの固形分量を有機性汚泥１００a中に含まれる固形分量に対する割合で表したものである。
尚、可溶化タンク４０内に供給する固形分量を調整する理由は、可溶化する固形分量が多いと嫌気性消化処理においてガス発生量が多くなる、汚泥減量が多くなるというメリットがある一方で、可溶化する固形分量が多すぎると脱水汚泥１００ｃの割合が高くなり流動性が悪くなる、消化タンク１０内において不活性な汚泥の割合が高くなり、また、汚泥濃度も高くなってしまうというデメリットがあるためである。
したがって、可溶化タンク４０へ供給する可溶化汚泥１００ｄの固形分量を有機性汚泥１００a中に含まれる固形分量に対する割合Ｙは３０〜８０％の範囲が適当であり、より好ましくは４０〜６０％が望ましい。
In the formula (1), Q 100b1 represents the supply amount [m 3 / day] of the digested sludge 100b1, and C 100b1 represents the concentration [wt%] of the solid content contained in the digested sludge 100b1. Q 100c1 supply amount of dehydrated sludge 100c1 indicates [m 3 / day], C 100c1 indicates the concentration [wt%] of the solid content contained in the dehydrated sludge 100c1. Q 100a indicates the supply amount [m 3 / day] of the organic sludge 100a , and C 100a indicates the concentration [wt%] of the solid content contained in the organic sludge. In addition, [wt%] shows weight percent.
Y represents the solid content of the solubilized sludge 100d supplied to the solubilization tank 40 as a percentage of the solid content contained in the organic sludge 100a.
The reason for adjusting the amount of solid content to be supplied into the solubilization tank 40 is that there is a merit that if the amount of solid content to be solubilized is large, the amount of gas generation increases in anaerobic digestion treatment, and sludge reduction increases. If the amount of solid content to be solubilized is too large, the ratio of
Therefore, the ratio Y of the solid content of the solubilized sludge 100d supplied to the solubilization tank 40 to the solid content contained in the organic sludge 100a is suitably in the range of 30 to 80%, more preferably 40 to 60%. desirable.
また、式（２）中におけるＴ１００ａは有機性汚泥１００ａの温度［℃］を示し、Ｔ１００ｄは可溶化汚泥１００ｄの温度［℃］を示し、Ｔ１０は消化タンク１０内における嫌気性消化処理を行う温度［℃］を示し、Ｈは比熱で４．１８６ＭＪ／ｍ３・℃を示し、Ｆは、消化タンク１０内における放熱量［ＭＪ／日］を示す。 T 100a in the formula (2) indicates the temperature [° C.] of the organic sludge 100a, T 100d indicates the temperature [° C.] of the solubilized sludge 100d, and T 10 is an anaerobic digestion treatment in the digestion tank 10. , H indicates a specific heat of 4.186 MJ / m 3 · ° C., and F indicates a heat release amount [MJ / day] in the digestion tank 10.
次に、上記式（１）の算出方法について説明する。尚、上記式（２）は、後述する可溶化汚泥循環工程によって、消化タンク１０内に循環させる可溶化汚泥量Ｑ１００ｄを求める式（６）と式（８）によって導出されるため、具体的な説明は可溶化汚泥循環工程で後述する。 Next, the calculation method of the above formula (1) will be described. The above formula (2) is derived from the formulas (6) and (8) for obtaining the solubilized sludge amount Q 100d to be circulated in the digestion tank 10 in the solubilized sludge circulation step described later. This will be described later in the solubilized sludge circulation process.
まず、上記式（１）を求めるにあたって、可溶化に必要な可溶化汚泥中の固形分量を有機性汚泥１００a中の固形分量に対する割合を表わすものをＹとすると、下記式（３）となる。 First, in obtaining the above formula (1), if the solid content in the solubilized sludge necessary for solubilization is Y, which represents the ratio of the solid content in the organic sludge 100a, the following formula (3) is obtained.
そして、上記式（３）から、必要とされる可溶化処理の固形分量は以下の式（４）となる。 And from the said Formula (3), the solid content amount of the solubilization process required becomes the following formula | equation (4).
また、可溶化処理に必要な固形分量は、可溶化タンク４０内に供給する消化汚泥１００ｂ１と脱水汚泥１００ｃ１の供給する量の割合によって決まるため、下記式（５）が導出される。そして、上記式（４）と下記式（５）とから、上記式（１）が導出することができる。 Further, since the solid content amount necessary for the solubilization process is determined by the ratio of the amount of digested sludge 100b1 and dehydrated sludge 100c1 supplied into the solubilization tank 40, the following equation (5) is derived. And the said Formula (1) can be derived | led-out from the said Formula (4) and following formula (5).
（可溶化工程）
可溶化工程は、可溶化タンク４０に供給された消化汚泥１００ｂ１と脱水汚泥１００ｃ１を加熱処理することによって、可溶化汚泥１００ｄを生成する工程である。加熱する温度は、１２０〜２３０℃であって、好ましくは１５０〜１８０℃である。加熱する方法は、消化タンク１０内に発生したメタンガスを可燃燃料とし、図示しない蒸気ボイラにより発生した蒸気を可溶化タンク４０に直接吹き込んで加熱する。
(Solubilization process)
The solubilization step is a step of generating the solubilized sludge 100d by heating the digested sludge 100b1 and the dehydrated sludge 100c1 supplied to the solubilization tank 40. The temperature to heat is 120-230 degreeC, Preferably it is 150-180 degreeC. In the heating method, methane gas generated in the digestion tank 10 is used as combustible fuel, and steam generated by a steam boiler (not shown) is directly blown into the solubilization tank 40 and heated.
（可溶化汚泥循環工程）
可溶化汚泥循環工程は、可溶化汚泥１００ｄを再度嫌気性消化処理させるために、可溶化タンク４０内で可溶化された可溶化汚泥１００ｄを消化タンク１０内に循環させる工程である。
ここで、循環させる可溶化汚泥１００ｄの量Ｑ１００ｄは、有機性汚泥１００ａと可溶化汚泥１００ｄとを嫌気性消化するために必要な熱量となるように下記式（６）により決定する。
(Solubilized sludge circulation process)
The solubilized sludge circulation step is a step of circulating the solubilized sludge 100d solubilized in the solubilization tank 40 in the digestion tank 10 in order to subject the solubilized sludge 100d to anaerobic digestion again.
Here, the amount Q 100d of the solubilized sludge 100d to be circulated is determined by the following formula (6) so as to be the amount of heat necessary for anaerobically digesting the organic sludge 100a and the solubilized sludge 100d.
ここで、有機性汚泥１００ａと可溶化汚泥１００ｄを嫌気性消化処理する温度をＴ１０℃とする。
そして、有機性汚泥１００ａの量と温度をＱ１００ａ［ｍ３／日］とＴ１００ａ［℃］、可溶化汚泥１００ｄの量と温度をＱ１００ｄ［ｍ３／日］とＴ１００ｄとすると、消化タンク１０内の熱収支は、下記式（７）となる。そして、この下記式（７）を整理すると上記式（６）となる。
Here, the temperature at which the organic sludge 100a and the solubilized sludge 100d are subjected to the anaerobic digestion treatment is defined as T 10 ° C.
When the amount and temperature of the organic sludge 100a are Q 100a [m 3 / day] and T 100a [° C.], and the amount and temperature of the solubilized sludge 100d are Q 100d [m 3 / day] and T 100d , digestion is performed. The heat balance in the tank 10 is expressed by the following formula (7). Then, when the following formula (7) is arranged, the above formula (6) is obtained.
尚、上記式（６）によって、循環させる可溶化汚泥１００ｄの量Ｑ１００ｄを求めるが、この可溶化汚泥１００ｄの量Ｑ１００ｄは、可溶化タンク４０内に供給された消化汚泥１００ｂ１と脱水汚泥１００ｃ１の合計と等しい。よって、下記式（８）が成立する。そして、下記式（８）と上記式（６）とから、上記式（２）が導出される。 Incidentally, by the above formula (6), but it obtains the quantity Q 100d solubilizing sludge 100d circulating amount Q 100d of the solubilized sludge 100d is digested sludge 100b1 supplied to the solubilization tank 40 and dewatered sludge 100c1 Equal to the sum of Therefore, the following formula (8) is established. Then, the above equation (2) is derived from the following equation (8) and the above equation (6).
（処理方法について）
次に、実施形態に係る有機性汚泥の嫌気性消化処理方法の使用方法について図２を用いて説明する。
尚、本実施形態における消化タンク１０内の消化温度Ｔ１０を３５℃、可溶化タンク４０内において可溶化された可溶化汚泥１００ｄの温度は１７０℃と設定する。
また、消化タンク１０に投入される有機性汚泥１００ａの量Ｑ１００ａは５０ｍ３／日、温度Ｔ１００ａは１５℃、固形分濃度Ｃ１００ａは４ｗｔ％とする。
また、可溶化に必要な固形分量と、有機性汚泥１００ａの固形分量との比率を１：２、すなわち、Ｙ＝１／２と設定する。
また、消化汚泥１００ｂ１の固形分濃度Ｃ１００ｂ１は３ｗｔ％、脱水汚泥１００ｃ１の固形分濃度Ｃ１００ｃ１は２５ｗｔ％とする。
また、放熱量Ｆは、０．３×（Ｔ１０−Ｔ１００ａ）×Ｈ［ＭＪ／日］とする。
(About processing method)
Next, the usage method of the anaerobic digestion processing method of the organic sludge which concerns on embodiment is demonstrated using FIG.
Incidentally, digestion temperature T 10 to 35 ° C. in the digesting tank 10 in the present embodiment, the temperature of the solubilized sludge 100d solubilized in solubilization tank 40 is set to 170 ° C..
The amount Q 100a of the organic sludge 100a charged into the digestion tank 10 is 50 m 3 / day, the temperature T 100a is 15 ° C., and the solid content concentration C 100a is 4 wt%.
In addition, the ratio of the solid content necessary for solubilization and the solid content of the organic sludge 100a is set to 1: 2, that is, Y = 1/2.
Further, the solid content concentration C 100b1 of the digested sludge 100b1 is 3 wt%, and the solid content concentration C 100c1 of the dehydrated sludge 100c1 is 25 wt%.
The heat release amount F is 0.3 × (T 10 −T 100a ) × H [MJ / day].
まず、上記式（６）より、消化タンク１０内に循環させる可溶化汚泥１００ｄの量Ｑ１００ｄを求める。 First, the amount Q 100d of the solubilized sludge 100d to be circulated in the digestion tank 10 is obtained from the above equation (6).
また、上記式（１）より可溶化処理に必要な固形分量を求める。 Further, the solid content amount required for the solubilization treatment is obtained from the above formula (1).
また、上記式（８）と式（９）より下記式（１１）が導出される。 Further, the following equation (11) is derived from the above equations (8) and (9).
上記式（１０）と式（１１）より、Ｑ１００ｂ１＝６．４［ｍ３／日］、Ｑ１００ｃ１＝３．２［ｍ３／日］となる。 From the above formula (10) and formula (11), Q 100b1 = 6.4 [m 3 / day] and Q 100c1 = 3.2 [m 3 / day].
そして、消化タンク１０内に循環させる可溶化汚泥１００ｄの量Ｑ１００ｄは９．６ｍ３／日と設定することで、消化タンク１０内の汚泥全体を嫌気性消化処理するのに必要な熱量を有する可溶化汚泥１００ｄを循環させることが可能となり、消化タンク１０内の汚泥全体の温度が嫌気性消化処理するために必要な温度となる。
また、消化汚泥１００ｂの量Ｑ１００ｂ１を６．４［ｍ３／日］と、また、脱水汚泥１００ｃの量Ｑ１００ｃ１を３．２［ｍ３／日]と調整することによって、可溶化処理に必要とする固形分量とすることが可能となる。
And the amount Q 100d of the solubilized sludge 100d to be circulated in the digestion tank 10 is set to 9.6 m 3 / day, so that the amount of heat necessary for anaerobically digesting the entire sludge in the digestion tank 10 is obtained. The solubilized sludge 100d can be circulated, and the temperature of the entire sludge in the digestion tank 10 becomes a temperature necessary for anaerobic digestion treatment.
Further, by adjusting the amount Q 100b1 of the digested sludge 100b to 6.4 [m 3 / day] and the amount Q 100c1 of the
以上、本発明によれば、可溶化汚泥を冷却する必要がなく、かつ、消化タンク１０内の温度を上昇させる必要がないため、可溶化汚泥を冷却するための熱交換器が不要となり、消化タンク１０内の汚泥全体を加熱するための余分なエネルギーを消費することがない。
また、可溶化タンク４０内に循環される可溶化すべき汚泥中の固形分量が、過不足無く確保される。
As described above, according to the present invention, it is not necessary to cool the solubilized sludge, and it is not necessary to raise the temperature in the digestion tank 10, so that a heat exchanger for cooling the solubilized sludge is not required. No extra energy is consumed to heat the entire sludge in the tank 10.
Moreover, the solid content in the sludge to be solubilized circulated in the solubilization tank 40 is ensured without excess or deficiency.
また、本実施形態によれば、消化タンク１０内に発生したバイオガスを燃焼燃料として、図示しない蒸気ボイラにより蒸気を発生させて可溶化タンク４０を加熱していたが、脱水汚泥１００ｃの可溶化汚泥循環工程に供しない残部を乾燥処理する際に、脱水汚泥から発生した蒸気を利用してもよい。
具体的には、図３に示すように、脱水汚泥１００ｃの可溶化汚泥循環工程に供しない残部が流入した乾燥炉５０を間接加熱した場合、その乾燥炉５０内に脱水汚泥から発生した蒸気をコンプレッサ６０によって圧縮することによって、さらに高温の蒸気を得ることができる。そして、その高温の蒸気を加熱源として可溶化タンク４０に流入させることによって、可溶化タンク４０内に供給された消化汚泥１００ｂ１と脱水汚泥１００ｃ１を可溶化処理することが可能となる。
Further, according to the present embodiment, the biogas generated in the digestion tank 10 is used as combustion fuel to generate steam with a steam boiler (not shown) to heat the solubilization tank 40. However, the solubilization of the dewatered
Specifically, as shown in FIG. 3, when the drying
これによれば、可溶化タンク４０内を加熱するための蒸気ボイラが不要となり、設備の縮小を図ることができる。また、蒸気ボイラの不要化に伴い、バイオガスの使用量の削減も図ることが可能となる。
尚、乾燥炉５０における乾燥処理は、乾燥炉５０の外壁等を消化タンク１０から発生するバイオガスなどを燃焼し脱水汚泥を間接的に加熱する方法により行う。
According to this, the steam boiler for heating the inside of the solubilization tank 40 becomes unnecessary, and it can aim at reduction of an installation. In addition, with the need for a steam boiler, the amount of biogas used can be reduced.
In addition, the drying process in the drying
１０ 消化タンク
２０ 消化汚泥脱水機
４０ 可溶化タンク
５０ 乾燥炉
６０ コンプレッサ
１００ａ 有機性汚泥
１００ｂ 消化汚泥
１００ｃ 脱水汚泥
１００ｄ 可溶化汚泥
DESCRIPTION OF SYMBOLS 10
Claims (4)
前記消化汚泥を脱水処理して脱水汚泥を生成する脱水工程と、
前記消化汚泥の一部と前記脱水汚泥の一部を可溶化タンクに供給する消化・脱水汚泥供給工程と、
前記可溶化タンクで前記消化汚泥の一部と前記脱水汚泥の一部を加熱処理し可溶化させることで可溶化汚泥を生成する可溶化工程と、
前記可溶化汚泥を前記消化タンクに循環させ、前記消化タンクに投入された前記有機性汚泥と混合させる可溶化汚泥循環工程と、を含む有機性汚泥の嫌気性消化処理方法であって、
前記可溶化汚泥循環工程は、
前記可溶化汚泥の処理温度に基づいて、消化タンクにおける嫌気性消化処理に必要とする熱量となるように、前記可溶化汚泥の循環量を設定し、
前記消化・脱水汚泥供給工程は、
前記可溶化汚泥循環工程において設定された前記可溶化汚泥の循環量に基づいて、前記可溶化汚泥が可溶化・嫌気性消化処理において必要とされる固形分量を有するように、可溶化タンクに供給する前記消化汚泥量と前記脱水汚泥量とを調整することを特徴とする有機性汚泥の嫌気性消化処理方法。 Anaerobic digestion process to produce digested sludge by anaerobic digestion treatment of organic sludge put into the digestion tank;
A dehydration step of dehydrating the digested sludge to produce dehydrated sludge;
Digestion / dehydration sludge supply step of supplying a part of the digested sludge and a part of the dewatered sludge to the solubilization tank,
A solubilization step of generating a solubilized sludge by heat-treating a part of the digested sludge and a part of the dehydrated sludge in the solubilization tank;
Circulating the solubilized sludge to the digestion tank and mixing the solubilized sludge with the organic sludge charged into the digestion tank, and anaerobic digestion treatment method of organic sludge,
The solubilized sludge circulation step includes:
Based on the treatment temperature of the solubilized sludge, set the circulation amount of the solubilized sludge so as to be the amount of heat required for the anaerobic digestion treatment in the digestion tank,
The digestion / dehydrated sludge supply process includes:
Based on the circulation amount of the solubilized sludge set in the solubilized sludge circulation step, the solubilized sludge is supplied to the solubilization tank so that it has the solid content required in the solubilization / anaerobic digestion process. The method of anaerobic digestion treatment of organic sludge characterized by adjusting the amount of digested sludge and the amount of dehydrated sludge.
前記可溶化工程において、前記消化・脱水汚泥を加熱して可溶化処理するときの前記消化・脱水汚泥の温度を１２０〜２３０℃に維持することを特徴とする請求項１又は請求項２に記載の有機性汚泥の嫌気性消化処理方法。 In the anaerobic digestion step, when the organic sludge is subjected to anaerobic digestion, the temperature of the organic sludge is maintained at 30 to 60 ° C.
3. The temperature of the digested / dehydrated sludge is maintained at 120 to 230 ° C. when the digested / dehydrated sludge is heated and solubilized in the solubilization step. Of anaerobic digestion of organic sludge.
前記汚泥乾燥工程において前記乾燥炉内に生じた蒸気を圧縮し、前記可溶化タンクに圧縮された蒸気を供給する蒸気圧縮工程とを含み、
前記蒸気圧縮工程により圧縮された蒸気を可溶化処理の加熱源とすることを特徴とする請求項１乃至３に記載の有機性汚泥の嫌気性消化処理方法。
A sludge drying step in which the remainder of the dewatered sludge is allowed to flow into a drying furnace and is dried by indirectly heating the drying furnace;
A vapor compression step of compressing the steam generated in the drying furnace in the sludge drying step and supplying the compressed steam to the solubilization tank,
The method of anaerobic digestion treatment of organic sludge according to any one of claims 1 to 3, wherein the steam compressed in the vapor compression step is used as a heat source for solubilization treatment.
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