JP6240800B2 - Waste treatment apparatus and waste treatment method - Google Patents
Waste treatment apparatus and waste treatment method Download PDFInfo
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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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Description
本発明は、廃棄物処理装置および廃棄物処理方法に関する。 The present invention relates to a waste treatment apparatus and a waste treatment method.
有機性廃棄物の処理方法としては、該廃棄物を、生物（メタン生成菌等）を含有する汚泥を備える生物処理槽で処理する方法が知られている（例えば、特許文献１〜４）。
また、他の方法としては、厨房排水を厨芥とともに生物処理槽で処理する方法も知られている（例えば、特許文献５）。
As a method for treating organic waste, a method is known in which the waste is treated in a biological treatment tank equipped with sludge containing organisms (methane-producing bacteria or the like) (for example, Patent Documents 1 to 4).
In addition, as another method, a method of treating kitchen wastewater in a biological treatment tank together with straw is also known (for example, Patent Document 5).
しかし、特許文献１〜４の方法では、該廃棄物における油分濃度が高いと前記汚泥に油分が付着して生物の活性が低下するという問題がある。
ここで、厨房排水は油分濃度が高い一方で、厨芥は厨房排水に比べて油分濃度が低い。よって、特許文献５の方法では、厨房排水に含まれる油分を厨芥に付着させることができ、油分が汚泥に付着するのを抑制することができる。
However, in the methods of Patent Documents 1 to 4, there is a problem that if the oil concentration in the waste is high, the oil is attached to the sludge and the activity of the organism is reduced.
Here, the kitchen drainage has a high oil concentration, while the kitchen has a lower oil concentration than the kitchen drainage. Therefore, in the method of patent document 5, the oil component contained in kitchen drainage can be made to adhere to a tub, and it can suppress that an oil component adheres to sludge.
しかしながら、特許文献５の方法でも、厨房排水の発生量が多くなった場合や、厨房排水の油分濃度が高くなった場合などには、生物の活性の低下を十分に抑制できないことがある。 However, even with the method of Patent Document 5, when the amount of kitchen wastewater generated increases or when the oil concentration of the kitchen wastewater increases, the decrease in biological activity may not be sufficiently suppressed.
そこで、上記問題点に鑑み、本発明は、油分を含む有機物を生物で分解させつつも、生物の活性の低下を抑制し得る廃棄物処理装置および廃棄物処理方法を提供することを課題とする。 Therefore, in view of the above problems, an object of the present invention is to provide a waste treatment apparatus and a waste treatment method capable of suppressing a decrease in the activity of a living organism while decomposing an organic matter containing oil by the living organism. .
本発明者らが鋭意研究したところ、生物としてメタン生成菌を用いた場合に、生物処理槽内の収容水中のノルマルヘキサン抽出物質濃度を所定以下にすることにより、汚泥に付着する油分の量を抑制することができ、その結果、油分を含めた有機物を生物で分解させつつも、生物の活性の低下を抑制し得ることを見出した。
また、本発明者らが鋭意研究したところ、油分を含む第１有機性廃棄物、及び、該第１有機性廃棄物よりも油分濃度が低い第２有機性廃棄物を処理する生物としてメタン生成菌を用いた場合に、前記生物処理槽内の収容水における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比を所定以下にすることにより、前記生物処理槽内の収容水に含まれる油分を前記第２有機性廃棄物に付着させることができ、その結果、油分を含めた有機物を生物で分解させつつも、生物の活性の低下を抑制し得ることを見出した。
そして、下記の本発明を想到するに至った。
When the present inventors diligently studied, when methanogens were used as living organisms, the amount of oil adhering to the sludge was reduced by setting the normal hexane extractable substance concentration in the contained water in the biological treatment tank to a predetermined value or less. As a result, the present inventors have found that a decrease in the activity of the organism can be suppressed while the organic matter including the oil is decomposed by the organism.
In addition, as a result of intensive research by the present inventors, methane is produced as an organism that processes the first organic waste containing oil and the second organic waste having a lower oil concentration than the first organic waste. When bacteria are used, the ratio of the normal hexane extractable substance concentration to the loss on ignition of the total evaporation residue in the stored water in the biological treatment tank is reduced to a predetermined value or less, so that the stored water in the biological treatment tank It has been found that the contained oil can be attached to the second organic waste, and as a result, the decrease in the activity of the organism can be suppressed while the organic matter including the oil is decomposed by the organism.
The inventors have come up with the following present invention.
すなわち、本発明の一の局面に係る廃棄物処理装置は、油分を含む第１有機性廃棄物、及び、該第１有機性廃棄物よりも油分濃度が低い第２有機性廃棄物をメタン生成菌で生物処理する生物処理槽を有する処理部と、
前記第１有機性廃棄物及び前記第２有機性廃棄物を前記生物処理槽に移送する移送部と、
下記（１）及び（２）の少なくとも何れか一方を満たすように前記生物処理槽内の収容水を調整する調整部とを備えている。
（１）前記生物処理槽内の収容水のノルマルヘキサン抽出物質濃度が２，２５０ｍｇ／Ｌ以下となる。
（２）前記生物処理槽内の収容水における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比が０．１５以下となる。
That is, the waste treatment apparatus according to one aspect of the present invention methane-generates a first organic waste containing oil and a second organic waste having a lower oil concentration than the first organic waste. A treatment unit having a biological treatment tank for biological treatment with bacteria;
A transfer unit for transferring the first organic waste and the second organic waste to the biological treatment tank;
And an adjusting unit that adjusts the water contained in the biological treatment tank so as to satisfy at least one of the following (1) and (2).
(1) The normal hexane extract substance concentration of the water contained in the biological treatment tank is 2,250 mg / L or less.
(2) The ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the stored water in the biological treatment tank is 0.15 or less.
ここで、本発明の一の局面に係る廃棄物処理装置は、前記移送部が、前記第１有機性廃棄物及び前記第２有機性廃棄物を混合することにより混合物を得る混合槽と、前記第１有機性廃棄物を前記混合槽に移送する第１移送部と、前記第２有機性廃棄物を前記混合槽に移送する第２移送部と、前記混合物を前記生物処理槽に移送する第３移送部とを有してもよい。 Here, in the waste treatment apparatus according to one aspect of the present invention, the transfer unit obtains a mixture by mixing the first organic waste and the second organic waste, and the mixing tank, A first transfer unit that transfers the first organic waste to the mixing tank; a second transfer unit that transfers the second organic waste to the mixing tank; and a first transfer unit that transfers the mixture to the biological treatment tank. You may have 3 transfer parts.
また、前記混合槽を有する廃棄物処理装置は、前記調整部が、前記混合槽内の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比が０．３２以下となるように前記混合槽内の混合物を調整する調整部であってもよい。 Further, in the waste treatment apparatus having the mixing tank, the adjustment unit is configured such that the ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the mixture in the mixing tank is 0.32 or less. The adjustment part which adjusts the mixture in the said mixing tank may be sufficient.
また、本発明者らが鋭意研究したところ、第１有機性廃棄物及び第２有機性廃棄物を混合槽で混合することにより混合物を得、該混合物を生物処理槽で生物処理し、生物としてメタン生成菌を用いる態様においては、前記混合槽内の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比を所定以下にすることにより、前記生物処理槽内の収容水に含まれる油分を前記第２有機性廃棄物に付着させることができ、その結果、油分を含めた有機物を生物で分解させつつも、生物の活性の低下を抑制し得ることを見出し、下記の本発明を想到するに至った。 Moreover, when the present inventors earnestly researched, a 1st organic waste and a 2nd organic waste were mixed with a mixing tank, a mixture was obtained, this mixture was biologically processed with a biological treatment tank, and it was used as a living thing. In the embodiment using the methanogen, the ratio of the normal hexane extractable substance to the loss on ignition of the total evaporation residue in the mixture in the mixing tank is set to a predetermined value or less so that the water contained in the biological treatment tank It was found that the contained oil component can be attached to the second organic waste, and as a result, the organic matter including the oil component can be decomposed by the organism, and the decrease in the activity of the organism can be suppressed. The inventors came up with the invention.
すなわち、本発明の他の局面に係る廃棄物処理装置は、油分を含む第１有機性廃棄物、及び、該第１有機性廃棄物よりも油分濃度が低い第２有機性廃棄物をメタン生成菌で生物処理する生物処理槽を有する処理部と、
前記第１有機性廃棄物及び前記第２有機性廃棄物を前記生物処理槽に移送する移送部とを備えており、
前記移送部は、前記第１有機性廃棄物及び前記第２有機性廃棄物を混合することにより混合物を得る混合槽と、前記第１有機性廃棄物を前記混合槽に移送する第１移送部と、前記第２有機性廃棄物を前記混合槽に移送する第２移送部と、前記混合物を前記生物処理槽に移送する第３移送部とを有し、
前記混合槽内の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比が０．３２以下となるように前記混合槽内の混合物を調整する調整部をさらに備えている。
That is, the waste treatment apparatus according to another aspect of the present invention methane-generates a first organic waste containing oil and a second organic waste having a lower oil concentration than the first organic waste. A treatment unit having a biological treatment tank for biological treatment with bacteria;
A transfer unit for transferring the first organic waste and the second organic waste to the biological treatment tank,
The transfer unit includes a mixing tank that obtains a mixture by mixing the first organic waste and the second organic waste, and a first transfer unit that transfers the first organic waste to the mixing tank. A second transfer unit that transfers the second organic waste to the mixing tank, and a third transfer unit that transfers the mixture to the biological treatment tank,
The apparatus further includes an adjusting unit that adjusts the mixture in the mixing tank so that the ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the mixture in the mixing tank is 0.32 or less.
また、本発明の一及び他の局面に係る廃棄物処理装置は、前記処理部が、前記生物処理槽内の収容水のｐＨ及び前記収容水から発生するガスのメタン濃度の少なくとも一方の値を測定する測定部をさらに有し、
前記調整部が、前記測定部で測定した生物処理槽内の収容水のｐＨ及び前記収容水から発生するガスのメタン濃度の少なくとも一方の値に基づいて、前記調整をする調整部であってもよい。
Further, in the waste treatment apparatus according to one and other aspects of the present invention, the treatment unit has at least one value of the pH of the contained water in the biological treatment tank and the methane concentration of the gas generated from the contained water. It further has a measuring part to measure,
The adjustment unit may be an adjustment unit that performs the adjustment based on at least one value of the pH of the stored water in the biological treatment tank measured by the measurement unit and the methane concentration of the gas generated from the stored water. Good.
さらに、本発明の一及び他の局面に係る廃棄物処理装置は、前記第１有機性廃棄物が厨房排水を含有し、前記第２有機性廃棄物が厨芥を含有してもよい。 Furthermore, in the waste disposal apparatus according to one and other aspects of the present invention, the first organic waste may contain kitchen wastewater, and the second organic waste may contain soot.
また、本発明の一及び他の局面に係る廃棄物処理装置では、前記移送部は、加圧浮上法により、前記第１有機性廃棄物から、前記第１有機性廃棄物よりも油分濃度が低い分離水と、前記第１有機性廃棄物よりも油分濃度が高い濃縮物とを得る加圧浮上部と、該濃縮物を貯留する調整槽とを備えており、
前記調整部は、前記調整槽を用いることにより、前記生物処理槽に移送する前記第１有機性廃棄物の流量を調整する調整部であってもよい。
Moreover, in the waste disposal apparatus according to one and other aspects of the present invention, the transfer unit has an oil concentration higher than that of the first organic waste from the first organic waste by a pressure flotation method. A pressure floating part for obtaining a low separation water, a concentrate having a higher oil concentration than the first organic waste, and a regulating tank for storing the concentrate,
The adjustment unit may be an adjustment unit that adjusts a flow rate of the first organic waste transferred to the biological treatment tank by using the adjustment tank.
また、本発明の一の局面に係る廃棄物処理方法は、油分を含む第１有機性廃棄物、及び、該第１有機性廃棄物よりも油分濃度が低い第２有機性廃棄物を生物処理槽内でメタン生成菌により生物処理する生物処理工程を有する処理工程と、
前記第１有機性廃棄物及び前記第２有機性廃棄物を前記生物処理槽に移送する移送工程とを備えており、
下記（１）及び（２）の少なくとも何れか一方を満たすように前記生物処理槽内の収容水を調整する。
（１）前記生物処理槽内の収容水のノルマルヘキサン抽出物質濃度が２，２５０ｍｇ／Ｌ以下となる。
（２）前記生物処理槽内の収容水における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比が０．１５以下となる。
In addition, a waste treatment method according to one aspect of the present invention is a biological treatment of a first organic waste containing oil and a second organic waste having a lower oil concentration than the first organic waste. A treatment process having a biological treatment process for biological treatment with a methanogen in a tank;
A transfer step of transferring the first organic waste and the second organic waste to the biological treatment tank,
The stored water in the biological treatment tank is adjusted so as to satisfy at least one of the following (1) and (2).
(1) The normal hexane extract substance concentration of the water contained in the biological treatment tank is 2,250 mg / L or less.
(2) The ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the stored water in the biological treatment tank is 0.15 or less.
さらに、本発明の他の局面に係る廃棄物処理方法は、油分を含む第１有機性廃棄物、及び、該第１有機性廃棄物よりも油分濃度が低い第２有機性廃棄物を生物処理槽内でメタン生成菌により生物処理する生物処理工程を有する処理工程と、
前記第１有機性廃棄物及び前記第２有機性廃棄物を前記生物処理槽に移送する移送工程とを備えており、
前記移送工程は、前記第１有機性廃棄物を混合槽に移送する第１移送工程と、前記第２有機性廃棄物を前記混合槽に移送する第２移送工程と、前記第１有機性廃棄物及び前記第２有機性廃棄物を前記混合槽で混合することにより混合物を得る混合工程と、該混合物を前記生物処理槽に移送する第３移送工程とを有し、
前記混合槽内の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比が０．３２以下となるように前記混合槽内の混合物を調整する。
Furthermore, in the waste treatment method according to another aspect of the present invention, the first organic waste containing oil and the second organic waste having a lower oil concentration than the first organic waste are biologically treated. A treatment process having a biological treatment process for biological treatment with a methanogen in a tank;
A transfer step of transferring the first organic waste and the second organic waste to the biological treatment tank,
The transfer step includes a first transfer step for transferring the first organic waste to the mixing tank, a second transfer step for transferring the second organic waste to the mixing tank, and the first organic waste. A mixing step of obtaining a mixture by mixing the product and the second organic waste in the mixing tank, and a third transfer step of transferring the mixture to the biological treatment tank,
The mixture in the mixing tank is adjusted so that the ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the mixture in the mixing tank is 0.32 or less.
以上のように、本発明によれば、油分を含めた有機物を生物で分解させつつも、生物の活性の低下を抑制し得る。 As described above, according to the present invention, it is possible to suppress a decrease in the activity of a living organism while decomposing the organic matter including the oil in the living organism.
以下、厨房排水と厨芥とをメタン発酵処理する場合を例に、添付図面を参照しつつ本発明の一実施形態について説明する。
本実施形態においては油分を含む第１有機性廃棄物として、前記厨房排水を含有する第１有機性廃棄物を生物処理し、該第１有機性廃棄物よりも油分濃度が低い第２有機性廃棄物として、厨芥を含有する第２有機性廃棄物を生物処理する。
Hereinafter, an embodiment of the present invention will be described with reference to the accompanying drawings, taking as an example the case of subjecting kitchen wastewater and straw to methane fermentation.
In the present embodiment, the first organic waste containing the kitchen wastewater is biologically treated as the first organic waste containing oil, and the second organic is lower in oil concentration than the first organic waste. Biologically treating the second organic waste containing soot as waste.
図１に示すように、本実施形態に係る廃棄物処理装置１は、油分を含む第１有機性廃棄物、及び、該第１有機性廃棄物よりも油分濃度が低い第２有機性廃棄物をメタン生成菌で生物処理する生物処理槽２１を有する処理部２と、前記第１有機性廃棄物及び前記第２有機性廃棄物を前記生物処理槽２１に移送する移送部３とを備える。
また、本実施形態に係る廃棄物処理装置１は、前記生物処理槽２１内の収容水におけるノルマルヘキサン抽出物質濃度、及び、該収容水における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比の少なくとも何れか一の値を調整する調整部４をさらに備える。
As shown in FIG. 1, the waste treatment apparatus 1 according to this embodiment includes a first organic waste containing oil and a second organic waste having a lower oil concentration than the first organic waste. And a transfer unit 3 for transferring the first organic waste and the second organic waste to the biological treatment tank 21.
In addition, the waste treatment apparatus 1 according to the present embodiment is configured so that the normal hexane extractable substance concentration in the stored water in the biological treatment tank 21 and the normal hexane extractable substance with respect to the ignition loss of the total evaporation residue in the stored water. An adjustment unit 4 that adjusts at least one of the density ratios is further provided.
前記移送部３は、前記第１有機性廃棄物及び前記第２有機性廃棄物を混合することにより混合物を得る混合槽３５と、前記第１有機性廃棄物を前記混合槽３５に移送する第１移送部３１と、前記第２有機性廃棄物を前記混合槽３５に移送する第２移送部３２と、前記混合物を前記生物処理槽２１に移送する第３移送部３３とを有する。
また、前記移送部３は、前記混合槽３５を介さずに前記生物処理槽２１に前記第２有機性廃棄物を移送する第４移送部３４を有する。
さらに、前記移送部３は、前記第２移送部３２を移送する第２有機性廃棄物の流量、及び、前記第４移送部３４を移送する第２有機性廃棄物の流量の少なくとも何れか一方の流量を制御する制御部３６を有する。
The transfer unit 3 includes a mixing tank 35 that obtains a mixture by mixing the first organic waste and the second organic waste, and a first tank that transfers the first organic waste to the mixing tank 35. 1 transfer part 31, a second transfer part 32 for transferring the second organic waste to the mixing tank 35, and a third transfer part 33 for transferring the mixture to the biological treatment tank 21.
The transfer unit 3 includes a fourth transfer unit 34 that transfers the second organic waste to the biological treatment tank 21 without using the mixing tank 35.
Further, the transfer unit 3 is at least one of a flow rate of the second organic waste that transfers the second transfer unit 32 and a flow rate of the second organic waste that transfers the fourth transfer unit 34. It has the control part 36 which controls the flow volume.
なお、“第２有機性廃棄物が該第１有機性廃棄物よりも油分濃度が低い”という要件による効果を本実施形態の廃棄物処理装置において得るためには、前記第１有機性廃棄物及び前記第２有機性廃棄物が前記生物処理槽２１に供給される際に前記要件を満たしていればよく、また、前記第１有機性廃棄物及び前記第２有機性廃棄物が前記混合槽３５を介する場合には、前記第１有機性廃棄物及び前記第２有機性廃棄物が前記混合槽３５に供給される際に前記要件を満たしていればよい。 In order to obtain the effect of the requirement that “the second organic waste has a lower oil concentration than the first organic waste” in the waste treatment apparatus of the present embodiment, the first organic waste And the said 2nd organic waste should just satisfy | fill the said requirements when supplying to the said biological treatment tank 21, and the said 1st organic waste and the said 2nd organic waste are the said mixing tank In the case where the first organic waste and the second organic waste are supplied to the mixing tank 35, it is only necessary to satisfy the above requirements.
前記第１移送部３１は、厨房から排出された厨房排水Ａたる第１有機性廃棄物を貯留することにより、油分を上層に浮遊させる槽３１ａを有する。
また、前記第１移送部３１は、前記槽３１ａの上層の厨房排水Ａたる第１有機性廃棄物から、該上層の厨房排水Ａよりも油分濃度が低い分離水と、該上層の厨房排水Ａよりも油分濃度が高い濃縮物Ｄとを得るグリストラップ３１ｂを有する。
さらに、前記第１移送部３１は、前記槽３１ａの下層の厨房排水Ａたる第１有機性廃棄物から、該下層の厨房排水Ａよりも含水率が高い分離水と、該下層の厨房排水Ａよりも含水率が低い濃縮物Ｅとを得るスクリーン３１ｃを有する。
また、前記第１移送部３１は、前記スクリーン３１ｃで得られた分離水たる第１有機性廃棄物を貯留する槽３１ｄを有する。
さらに、前記第１移送部３１は、加圧浮上法により、前記槽３１ｄ内の収容水たる第１有機性廃棄物から、前記槽３１ｄ内の収容水よりも油分濃度が低い分離水と、前記槽３１ｄ内の収容水よりも油分濃度が高い濃縮物とを得る加圧浮上部３１ｅを有する。
また、前記第１移送部３１は、前記加圧浮上部３１ｅで得られた濃縮物たる第１有機性廃棄物を前記混合槽３５に移送する濃縮物移送管３１ｆを有する。さらに、前記第１移送部３１は、該濃縮物を該濃縮物移送管３１ｆ内にて移送させうるように前記濃縮物移送管３１ｆに配されたポンプ３１ｇを有してもよい。
さらに、前記第１移送部３１は、前記加圧浮上部３１ｅで得られた濃縮物たる第１有機性廃棄物を貯留する調整槽を更に備えてもよい。前記調整槽は、前記濃縮物移送管３１ｆの途中に設けられている。前記調整部４は、前記調整槽を用いることにより、前記生物処理槽に移送する前記第１有機性廃棄物の流量を調整する調整部である。
The said 1st transfer part 31 has the tank 31a which makes an upper layer float an oil component by storing the 1st organic waste which is the kitchen waste_water | drain A discharged | emitted from the kitchen.
In addition, the first transfer unit 31 includes a separated water having a lower oil concentration than the upper-layer kitchen drainage A from the first organic waste as the upper-layer kitchen drainage A of the tank 31a, and the upper-layer kitchen drainage A. It has a grease trap 31b for obtaining a concentrate D having a higher oil concentration.
Further, the first transfer unit 31 is configured to separate from the first organic waste as the lower-layer kitchen drainage A of the tank 31a, separated water having a higher moisture content than the lower-layer kitchen drainage A, and the lower-layer kitchen drainage A. A screen 31c for obtaining a concentrate E having a lower water content.
Moreover, the said 1st transfer part 31 has the tank 31d which stores the 1st organic waste which is the separated water obtained by the said screen 31c.
Furthermore, the first transfer unit 31 is separated from the first organic waste, which is the stored water in the tank 31d, by the pressurized flotation method, and the separated water having a lower oil concentration than the stored water in the tank 31d; It has a pressurized floating part 31e for obtaining a concentrate having a higher oil concentration than the water contained in the tank 31d.
In addition, the first transfer unit 31 includes a concentrate transfer pipe 31f that transfers the first organic waste, which is a concentrate obtained in the pressurized floating part 31e, to the mixing tank 35. Furthermore, the first transfer unit 31 may include a pump 31g disposed in the concentrate transfer pipe 31f so that the concentrate can be transferred in the concentrate transfer pipe 31f.
Furthermore, the said 1st transfer part 31 may further be equipped with the adjustment tank which stores the 1st organic waste which is the concentrate obtained in the said pressurization floating part 31e. The adjusting tank is provided in the middle of the concentrate transfer pipe 31f. The said adjustment part 4 is an adjustment part which adjusts the flow volume of the said 1st organic waste transferred to the said biological treatment tank by using the said adjustment tank.
前記第１移送部３１は、前記グリストラップ３１ｂで得られた分離水が厨房排水Ａとして前記槽３１ａに返送されるように構成されている。
また、前記第１移送部３１は、前記グリストラップ３１ｂで得られた濃縮物Ｄが廃棄物処理装置１外に移送されるように構成されている。
さらに、前記第１移送部３１は、前記スクリーン３１ｃで得られた濃縮物Ｅが廃棄物処理装置１外に移送されるように構成されている。
また、前記第１移送部３１は、前記加圧浮上部３１ｅで得られた分離水を前記移送部３外に移送するように構成されている。
The first transfer unit 31 is configured so that the separated water obtained by the grease strap 31b is returned to the tank 31a as kitchen drainage A.
The first transfer unit 31 is configured such that the concentrate D obtained by the grease strap 31b is transferred out of the waste treatment apparatus 1.
Further, the first transfer unit 31 is configured to transfer the concentrate E obtained by the screen 31c to the outside of the waste treatment apparatus 1.
Further, the first transfer unit 31 is configured to transfer the separated water obtained by the pressurized floating part 31 e to the outside of the transfer unit 3.
前記第２移送部３２は、厨芥Ｂたる第２有機性廃棄物を粉砕し、粉砕した厨芥Ｂと水とを混合することにより、ディスポーザ排水を得るディスポーザ部３２ａを有する。
また、前記第２移送部３２は、該ディスポーザ排水たる第２有機性廃棄物から、該ディスポーザ排水よりも含水率が高い分離水と、該ディスポーザ排水よりも含水率が低い濃縮物とを得るスクリーン３２ｂを有する。
即ち、本実施形態のスクリーン３２ｂは、粉砕された厨芥を主体とした有機性固形分を含む濃縮物を形成し得るように形成されている。
さらに、前記第２移送部３２は、ディスポーザ排水を貯留するディスポーザ排水槽３２ｃを有する。
また、前記第２移送部３２は、前記ディスポーザ排水をディスポーザ排水槽３２ｃを介さずに前記スクリーン３２ｂに移送する第１ディスポーザ排水移送管３２ｄと、前記ディスポーザ排水を前記ディスポーザ排水槽３２ｃを介して前記スクリーン３２ｂに移送する第２ディスポーザ排水移送管３２ｅとを有する。
さらに、前記第２移送部３２は、前記第１ディスポーザ排水移送管３２ｄと前記第２ディスポーザ排水移送管との間で、前記ディスポーザ排水の移送経路を相互に切り替え可能とする切り替え部３２ｆを有する。
また、前記第２移送部３２は、前記スクリーン３２ｂで得た濃縮物たる第２有機性廃棄物を前記混合槽３５に移送する濃縮物移送管３２ｇと、該濃縮物を該濃縮物移送管３２ｇ内にて移送させうるように前記スクリーン３２ｂまたは前記濃縮物移送管３２ｇに配されたポンプ３２ｈとを有する。
The said 2nd transfer part 32 has the disposer part 32a which obtains the disposer drainage by grind | pulverizing the 2nd organic waste which is the soot B, and mixing the ground soot B and water.
The second transfer unit 32 obtains, from the second organic waste as the disposer wastewater, separated water having a higher water content than the disposer wastewater and a concentrate having a lower water content than the disposer wastewater. 32b.
That is, the screen 32b of the present embodiment is formed so as to be able to form a concentrate containing an organic solid content mainly composed of crushed soot.
Furthermore, the said 2nd transfer part 32 has the disposer drainage tank 32c which stores a disposer drainage.
The second transfer unit 32 includes a first disposer drain transfer pipe 32d that transfers the disposer drain to the screen 32b without passing through the disposer drain 32c, and the disposer drain through the disposer drain 32c. And a second disposer drainage transfer pipe 32e for transfer to the screen 32b.
Further, the second transfer unit 32 includes a switching unit 32f that allows the transfer path of the disposer drain to be switched between the first disposer drain transfer pipe 32d and the second disposer drain transfer pipe.
The second transfer unit 32 includes a concentrate transfer pipe 32g for transferring the second organic waste, which is a concentrate obtained from the screen 32b, to the mixing tank 35, and the concentrate is supplied to the concentrate transfer pipe 32g. A pump 32h disposed on the screen 32b or the concentrate transfer pipe 32g so as to be transferred inside.
また、前記第２移送部３２は、前記スクリーン３２ｂで得られた分離水を前記槽３１ｄに移送するように構成されている。 The second transfer unit 32 is configured to transfer the separated water obtained by the screen 32b to the tank 31d.
前記切り替え部３２ｆは、前記第１ディスポーザ排水移送管３２ｄの流路を開閉する第３バルブ３２ｆ１と、前記第２ディスポーザ排水移送管３２ｅの流路を開閉する第４バルブ３２ｆ２とを有する。
また、前記第２移送部３２は、前記第３バルブ３２ｆ１を開状態にし、前記第４バルブ３２ｆ２を閉状態にすることにより、前記ディスポーザ排水を前記ディスポーザ排水槽３２ｃを介さずに前記スクリーン３２ｂに移送することができる。また、前記第２移送部３２は、前記第３バルブ３２ｆ１を閉状態にし、前記第４バルブ３２ｆ２を開状態にすることにより、前記ディスポーザ排水を前記スクリーン３２ｂに移送する前に前記ディスポーザ排水槽３２ｃで貯留することができる。すなわち、前記第２移送部３２は、平常時は前記ディスポーザ排水を前記スクリーン３２ｂに移送することができる。また、前記第２移送部３２は、前記ディスポーザ排水が多量に発生した時には前記ディスポーザ排水槽３２ｃで貯留しつつ、前記ディスポーザ排水槽３２ｃで貯留されるディスポーザ排水の一部を前記スクリーン３２ｂに移送することにより、前記スクリーン３２ｂに移送するディスポーザ排水の量を抑制することができる。
The switching unit 32f includes a third valve 32f1 that opens and closes the flow path of the first disposer drain transfer pipe 32d, and a fourth valve 32f2 that opens and closes the flow path of the second disposer drain transfer pipe 32e.
In addition, the second transfer unit 32 opens the third valve 32f1 and closes the fourth valve 32f2, thereby allowing the disposer drainage to flow to the screen 32b without passing through the disposer drain tank 32c. Can be transported. Further, the second transfer part 32 closes the third valve 32f1 and opens the fourth valve 32f2, so that the disposer drain tank 32c is transferred before the disposer drain is transferred to the screen 32b. Can be stored. That is, the second transfer unit 32 can transfer the disposer drainage to the screen 32b in normal times. Further, the second transfer part 32 transfers a part of the disposer drainage stored in the disposer drainage tank 32c to the screen 32b while storing in the disposer drainage tank 32c when a large amount of the disposer drainage is generated. Thus, the amount of disposer drainage transferred to the screen 32b can be suppressed.
前記混合槽３５は、前記濃縮物移送管３２ｇで移送された濃縮物たる第２有機性廃棄物と、前記濃縮物移送管３１ｆで移送された濃縮物たる第１有機性廃棄物とを混合して混合物を得る混合槽である。前記移送部３は、該混合槽３５内を撹拌する撹拌部３５ａを有する。 The mixing tank 35 mixes the second organic waste as the concentrate transferred through the concentrate transfer pipe 32g and the first organic waste as the concentrate transferred through the concentrate transfer pipe 31f. To obtain a mixture. The transfer unit 3 includes a stirring unit 35 a that stirs the inside of the mixing tank 35.
前記第３移送部３３は、前記混合物を、前記第１有機性廃棄物及び前記第２有機性廃棄物として前記生物処理槽２１に移送する混合物移送管３３ａと、該混合物を該混合物移送管３３ａ内にて移送させうるように前記混合物移送管３３ａに配されたポンプ３３ｂとを有する。 The third transfer unit 33 includes a mixture transfer pipe 33a that transfers the mixture as the first organic waste and the second organic waste to the biological treatment tank 21, and the mixture transfer pipe 33a. And a pump 33b arranged in the mixture transfer pipe 33a so that it can be transferred inside.
前記第４移送部３４は、前記濃縮物移送管３２ｇの前記ポンプ３２ｈより下流側の位置から分岐した分岐管３４ａを有する。
該分岐管３４ａは、前記スクリーン３２ｂで得た濃縮物たる第２有機性廃棄物を前記混合槽３５を介さずに前記生物処理槽２１に移送する管である。
The fourth transfer part 34 has a branch pipe 34a branched from a position downstream of the pump 32h of the concentrate transfer pipe 32g.
The branch pipe 34a is a pipe for transferring the second organic waste as the concentrate obtained by the screen 32b to the biological treatment tank 21 without passing through the mixing tank 35.
前記制御部３６は、前記混合槽３５と前記生物処理槽２１との間で、スクリーン３２ｂで得た濃縮物たる第２有機性廃棄物の移送先を相互に切り替え可能とする制御部である。
前記制御部３６は、前記濃縮物移送管３２ｇの流路を開閉する第１バルブ３６ａと、前記分岐管３４ａの流路を開閉する第２バルブ３６ｂとを有する。
前記移送部３は、前記第１バルブ３６ａを開状態にし、前記第２バルブ３６ｂを閉状態にすることにより、前記スクリーン３２ｂで得た濃縮物たる第２有機性廃棄物を前記混合槽３５に移送することができる。また、前記移送部３は、前記第１バルブ３６ａを閉状態にし、前記第２バルブ３６ｂを開状態にすることにより、前記スクリーン３２ｂで得た濃縮物たる第２有機性廃棄物を前記混合槽３５を介さずに前記生物処理槽２１に移送することができる。
The control unit 36 is a control unit that can switch between the transfer destinations of the second organic waste as the concentrate obtained by the screen 32b between the mixing tank 35 and the biological treatment tank 21.
The controller 36 includes a first valve 36a for opening and closing the flow path of the concentrate transfer pipe 32g and a second valve 36b for opening and closing the flow path of the branch pipe 34a.
The transfer unit 3 opens the first valve 36a and closes the second valve 36b, whereby the second organic waste, which is the concentrate obtained from the screen 32b, is transferred to the mixing tank 35. Can be transported. In addition, the transfer unit 3 closes the first valve 36a and opens the second valve 36b, so that the second organic waste, which is the concentrate obtained from the screen 32b, is mixed with the mixing tank. It can be transferred to the biological treatment tank 21 without going through 35.
前記処理部２は、前記生物処理槽２１に加え、前記生物処理槽２１内の収容水を固液分離することにより、前記収容水よりも含水率が高い分離水、及び、前記収容水よりも含水率が低い濃縮物Ｆを得る固液分離部２２と、前記収容水を前記生物処理槽２１から前記固液分離部２２に移送する収容水移送部２３ａと、前記固液分離部２２で得られた分離水を前記生物処理槽２１に移送する分離水移送部２３ｂと、前記固液分離部２２で得られた濃縮物Ｆを廃棄物処理装置１外に移送する濃縮物移送部２３ｃとを有する。
なお、前記固液分離部２２で得られた分離水を前記生物処理槽２１に移送する際には、該分離水を、前記ディスポーザ排水槽３２ｃまたは前記混合槽３５を介して前記生物処理槽２１に移送してもよい。
また、前記処理部２は、前記生物処理槽２１からのオーバーフロー水から、該オーバーフロー水よりも含水率が高い分離水と、該オーバーフロー水よりも含水率が低い濃縮物とを得るスクリーン２４を有する。
さらに、前記処理部２は、前記スクリーン２４で得られた分離水を曝気しながら好気性生物で処理することにより、浄化水Ｃを得る曝気部２５ａを有する。
また、前記処理部２は、浄化水Ｃを系外に排出する排出部２５ｂを有する。該排出部２５ｂは、槽とポンプとを備え、該槽は、前記曝気部２５ａで得られた浄化水Ｃを一時的に収容する槽であり、前記ポンプは、該槽内の浄化水Ｃを引き抜いて系外に排出させるためのポンプである。
また、前記処理部２は、前記生物処理槽２１で得られたバイオガスから硫黄分を除去する脱硫部２６ａと、該脱硫部２６ａで硫黄分が除去されたバイオガスを貯留するガス貯留部２６ｂと、該ガス貯留部２６ｂで貯留されたガスをエネルギーとして利用するガス利用設備２６ｃとを有する。
In addition to the biological treatment tank 21, the treatment unit 2 performs solid-liquid separation on the stored water in the biological treatment tank 21, thereby separating water having a higher moisture content than the stored water, and more than the stored water. Obtained by the solid-liquid separation unit 22 for obtaining the concentrate F having a low water content, the stored water transfer unit 23a for transferring the stored water from the biological treatment tank 21 to the solid-liquid separation unit 22, and the solid-liquid separation unit 22 A separated water transfer unit 23b for transferring the separated water to the biological treatment tank 21, and a concentrate transfer unit 23c for transferring the concentrate F obtained in the solid-liquid separation unit 22 to the outside of the waste treatment apparatus 1. Have.
When the separated water obtained in the solid-liquid separation unit 22 is transferred to the biological treatment tank 21, the separated water is supplied to the biological treatment tank 21 via the disposer drain tank 32 c or the mixing tank 35. May be transferred to.
Moreover, the said process part 2 has the screen 24 which obtains the separated water whose moisture content is higher than this overflow water, and the concentrate whose moisture content is lower than this overflow water from the overflow water from the said biological treatment tank 21. .
Further, the processing unit 2 includes an aeration unit 25a that obtains purified water C by processing the separated water obtained on the screen 24 with an aerobic organism while aerating.
Moreover, the said process part 2 has the discharge part 25b which discharges the purified water C out of the system. The discharge unit 25b includes a tank and a pump, the tank is a tank that temporarily stores the purified water C obtained in the aeration unit 25a, and the pump stores the purified water C in the tank. It is a pump that is pulled out and discharged out of the system.
The processing unit 2 includes a desulfurization unit 26a that removes sulfur from the biogas obtained in the biological treatment tank 21, and a gas storage unit 26b that stores the biogas from which sulfur has been removed by the desulfurization unit 26a. And a gas use facility 26c that uses the gas stored in the gas storage unit 26b as energy.
前記生物処理槽２１は、前記移送部３から移送されてきた第１有機性廃棄物と第２有機性廃棄物とをメタン生成菌で生物処理する生物処理槽である。
また、前記処理部２は、前記生物処理槽２１内の収容水を撹拌する撹拌部２１ａを有する。前記撹拌部２１ａは、回転軸２１ａ１と、回転軸に設けられた撹拌翼２１ａ２とを有する。なお、前記撹拌部２１ａは、回転軸に撹拌翼を設けたものに限らず、例えば、前記生物処理槽２１内の収容水にガスを吹き込むことにより該収容水を撹拌する装置であってもよい。また、前記撹拌部２１ａは、ポンプを用いて前記収容水を循環させることにより該収容水を撹拌する装置であってもよい。
さらに、前記処理部２は、前記生物処理槽２１内の収容水のｐＨ、及び、前記生物処理槽２１内の前記収容水から発生するガスのメタン濃度の少なくとも何れか一方を測定する測定部２１ｂを有する。
The biological treatment tank 21 is a biological treatment tank for biologically treating the first organic waste and the second organic waste transferred from the transfer unit 3 with methane-producing bacteria.
Moreover, the said process part 2 has the stirring part 21a which stirs the accommodation water in the said biological treatment tank 21. FIG. The stirring unit 21a includes a rotating shaft 21a1 and a stirring blade 21a2 provided on the rotating shaft. In addition, the said stirring part 21a is not restricted to what provided the stirring blade in the rotating shaft, For example, the apparatus which stirs this accommodation water by blowing gas in the accommodation water in the said biological treatment tank 21 may be sufficient. . Further, the stirring unit 21a may be a device that stirs the stored water by circulating the stored water using a pump.
Further, the processing unit 2 measures at least one of the pH of the stored water in the biological treatment tank 21 and the methane concentration of the gas generated from the stored water in the biological treatment tank 21. Have
前記収容水移送部２３ａは、前記収容水を前記生物処理槽２１から前記固液分離部２２に移送する収容水移送管２３ａ１と、前記収容水を該収容水移送管２３ａ１内にて移送させうるように該収容水移送管２３ａ１に配されたポンプ２３ａ２とを有する。
前記分離水移送部２３ｂは、前記混合槽３５を介して前記分離水を前記生物処理槽２１に移送する分離水移送部である。
The stored water transfer section 23a can transfer the stored water from the biological treatment tank 21 to the solid-liquid separation section 22 and the stored water transfer pipe 23a1 to transfer the stored water in the stored water transfer pipe 23a1. And a pump 23a2 arranged in the stored water transfer pipe 23a1.
The separation water transfer unit 23 b is a separation water transfer unit that transfers the separation water to the biological treatment tank 21 via the mixing tank 35.
なお、前記処理部２の生物処理槽２１は、前記生物処理槽２１内の収容水を沈殿分離することにより、前記収容水よりも含水率が高い分離水、及び、前記収容水よりも含水率が低い濃縮物を得る沈殿分離槽となっていてもよい。
この場合、前記収容水移送部２３ａは、前記沈殿分離槽で得られた濃縮物を前記収容水として前記生物処理槽２１から前記固液分離部２２に移送する収容水移送部である。
また、生物処理の時よりも前記撹拌部２１ａによる撹拌を緩やかにするか、或いは前記撹拌部２１ａによる撹拌を停止することで、前記生物処理槽２１が沈殿分離槽として機能する。なお、前記回転軸の回転数を低下させることで前記撹拌部２１ａによる撹拌を緩やかにすることができ、また、前記回転軸の回転を停止することで前記撹拌部２１ａによる撹拌を停止することができる。
また、前記生物処理槽２１たる沈殿分離槽の底面は、傾斜してもよく、例えば、テーパー状になってもよい。前記生物処理槽２１たる沈殿分離槽は、前記底面が傾斜していることで、含水率がより一層低い濃縮物を得やすくなる。
In addition, the biological treatment tank 21 of the said process part 2 carries out the sedimentation separation of the accommodation water in the said biological treatment tank 21, and the separated water whose moisture content is higher than the said accommodation water, and a moisture content than the said accommodation water May be a precipitation separation tank for obtaining a concentrate having a low concentration.
In this case, the stored water transfer unit 23 a is a stored water transfer unit that transfers the concentrate obtained in the precipitation separation tank as the stored water from the biological treatment tank 21 to the solid-liquid separation unit 22.
In addition, the biological treatment tank 21 functions as a precipitation separation tank by slowing the stirring by the stirring unit 21a or stopping the stirring by the stirring unit 21a as compared with the time of biological treatment. The stirring by the stirring unit 21a can be moderated by reducing the number of rotations of the rotating shaft, and the stirring by the stirring unit 21a can be stopped by stopping the rotation of the rotating shaft. it can.
Moreover, the bottom surface of the precipitation separation tank which is the biological treatment tank 21 may be inclined, for example, may be tapered. The sedimentation separation tank which is the biological treatment tank 21 is easy to obtain a concentrate having a lower moisture content because the bottom surface is inclined.
前記処理部２は、前記スクリーン２４で得た濃縮物Ｇを廃棄物処理装置１外に移送するように構成されている。
また、前記処理部２は、浄化水Ｃが廃棄物処理装置１外に移送されるように構成されている。浄化水Ｃは、例えば下水道に移送される。
The processing unit 2 is configured to transfer the concentrate G obtained by the screen 24 to the outside of the waste processing apparatus 1.
The treatment unit 2 is configured such that the purified water C is transferred to the outside of the waste treatment apparatus 1. The purified water C is transferred to the sewer, for example.
前記ガス利用設備２６ｃとしては、ボイラー、ガスエンジン発電機などが挙げられる。該ガス利用設備２６ｃでは、前記ボイラーによって蒸気が得られる。また、ガスエンジン発電機によって電気と温水とが得られる。 Examples of the gas utilization facility 26c include a boiler and a gas engine generator. In the gas utilization facility 26c, steam is obtained by the boiler. In addition, electricity and hot water are obtained by the gas engine generator.
さらに、前記処理部２は、前記ガス利用設備２６ｃで得られた蒸気又は温水で前記生物処理槽２１内の収容水を温めるように構成されている。収容水内のメタン生成菌の活性を高めるという観点から、収容水の温度は、中温メタン発酵では３５℃〜４０℃、高温メタン発酵では５０〜６０℃が好ましい。油分を多く含む有機性廃棄物を用いてメタン発酵する場合には、高温メタン発酵の方が、効率がよい。
具体的には、前記処理部２は、前記温水、又は、前記蒸気を貯留する槽２６ｄを有し、該温水、又は、前記蒸気で前記生物処理槽２１の収容水を温めるように構成されている。
例えば、前記処理部２は、熱交換器を介して前記温水を利用することにより、前記生物処理槽２１の収容水を温めるように構成されてもよく、また、前記生物処理槽２１の収容水に蒸気を直接吹き付けることにより、前記生物処理槽２１の収容水を温めるように構成されてもよい。
Furthermore, the said process part 2 is comprised so that the accommodation water in the said biological treatment tank 21 may be warmed with the steam or warm water obtained with the said gas utilization equipment 26c. From the viewpoint of increasing the activity of the methanogen in the stored water, the temperature of the stored water is preferably 35 ° C. to 40 ° C. for medium temperature methane fermentation and 50 ° C. to 60 ° C. for high temperature methane fermentation. When methane fermentation is performed using organic waste containing a large amount of oil, high-temperature methane fermentation is more efficient.
Specifically, the processing unit 2 includes a tank 26d for storing the warm water or the steam, and is configured to warm the water stored in the biological treatment tank 21 with the warm water or the steam. Yes.
For example, the processing unit 2 may be configured to warm the water contained in the biological treatment tank 21 by using the warm water via a heat exchanger, and the water contained in the biological treatment tank 21. The water stored in the biological treatment tank 21 may be warmed by directly spraying the steam.
前記調整部４は、前記生物処理槽内の収容水におけるノルマルヘキサン抽出物質濃度、及び、該収容水における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比の少なくとも一方の値を調整すべく、前記処理部２及び前記移送部３の少なくとも一方に制御する信号を発信する信号発信部４１と、該信号を前記処理部２及び前記移送部３の少なくとも一方に信号を伝達する制御信号伝達部４２とを有する。 The adjusting unit 4 determines at least one value of the normal hexane extract substance concentration in the stored water in the biological treatment tank and the ratio of the normal hexane extract substance concentration to the ignition loss of the total evaporation residue in the stored water. In order to adjust, a signal transmission unit 41 for transmitting a control signal to at least one of the processing unit 2 and the transfer unit 3, and a control for transmitting the signal to at least one of the processing unit 2 and the transfer unit 3 A signal transmission unit 42.
本実施形態に係る廃棄物処理装置１は、前記調整部４によって前記制御部３６が作動することにより、前記混合槽３５と前記生物処理槽２１との間で、前記スクリーン３２ｂで得た濃縮物たる第２有機性廃棄物の移送先を相互に切り替え可能となっている。
すなわち、前記制御信号伝達部４２は、前記制御部３６の前記第１、２バルブ３６ａ、３６ｂそれぞれに信号を伝達する第１、２制御信号伝達部４２ａ、４２ｂを有する。本実施形態に係る廃棄物処理装置１は、前記第１、２制御信号伝達部４２ａ、４２ｂによって、前記第１、２バルブ３６ａ、３６ｂが開閉されるように構成されている。
In the waste treatment apparatus 1 according to the present embodiment, the concentrate obtained by the screen 32b between the mixing tank 35 and the biological treatment tank 21 when the control unit 36 is operated by the adjusting unit 4. It is possible to switch the destination of the second organic waste.
That is, the control signal transmission unit 42 includes first and second control signal transmission units 42 a and 42 b that transmit signals to the first and second valves 36 a and 36 b of the control unit 36, respectively. The waste treatment apparatus 1 according to this embodiment is configured such that the first and second valves 36a and 36b are opened and closed by the first and second control signal transmission units 42a and 42b.
また、本実施形態に係る廃棄物処理装置１は、前記調整部４によって、前記移送部３で前記生物処理槽２１に移送する第１有機性廃棄物、第２有機性廃棄物との流量を調整するように構成されている。
すなわち、前記制御信号伝達部４２は、前記ポンプ３１ｇ、３２ｈ、３３ｂそれぞれに信号を伝達する第３、４、５制御信号伝達部４２ｃ、４２ｄ、４２ｅを有する。
本実施形態に係る廃棄物処理装置１は、前記第３、４、５制御信号伝達部４２ｃ、４２ｄ、４２ｅによって、前記ポンプ３１ｇ、３２ｈ、３３ｂの回転数を変化させることにより、前記移送部３で前記生物処理槽２１に移送する第１有機性廃棄物と第２有機性廃棄物との流量を調整するように構成されている。なお、前記第１有機性廃棄物と前記第２有機性廃棄物との流量の調整は、前記ポンプ３１ｇ、３２ｈ、３３ｂの回転数を変化させることによるに限るものではなく、例えば、前記ポンプ３１ｇ、３２ｈ、３３ｂの吐出配管中に制御弁を設けて、該制御弁の開度を変化させることによるものであってもよい。
Moreover, the waste treatment apparatus 1 which concerns on this embodiment is the said adjustment part 4, The flow volume with the 1st organic waste and 2nd organic waste which are transferred to the said biological treatment tank 21 by the said transfer part 3 is set. Configured to adjust.
That is, the control signal transmission unit 42 includes third, fourth, and fifth control signal transmission units 42c, 42d, and 42e that transmit signals to the pumps 31g, 32h, and 33b, respectively.
The waste treatment apparatus 1 according to the present embodiment changes the number of rotations of the pumps 31g, 32h, and 33b by the third, fourth, and fifth control signal transmission units 42c, 42d, and 42e, thereby changing the transfer unit 3. The flow rate of the first organic waste and the second organic waste transferred to the biological treatment tank 21 is adjusted. The adjustment of the flow rates of the first organic waste and the second organic waste is not limited to changing the rotational speeds of the pumps 31g, 32h, and 33b. For example, the pump 31g , 32h, 33b may be provided by providing a control valve in the discharge pipe and changing the opening of the control valve.
さらに、本実施形態に係る廃棄物処理装置１は、前記調整部４によって、前記生物処理槽２１から前記固液分離部２２に移送する前記生物処理槽２１の収容水の流量を調整するように構成されている。
すなわち、前記制御信号伝達部４２は、前記ポンプ２３ａ２に信号を伝達する第６制御信号伝達部４２ｆを有する。
本実施形態に係る廃棄物処理装置１は、前記第６制御信号伝達部４２ｆによって、前記ポンプ２３ａ２の回転数を変化させることにより、前記移送部３で前記生物処理槽２１から前記固液分離部２２に移送する生物処理槽２１の収容水の流量を調整するように構成されている。
Furthermore, in the waste treatment apparatus 1 according to the present embodiment, the adjustment unit 4 adjusts the flow rate of water contained in the biological treatment tank 21 that is transferred from the biological treatment tank 21 to the solid-liquid separation unit 22. It is configured.
That is, the control signal transmission unit 42 includes a sixth control signal transmission unit 42f that transmits a signal to the pump 23a2.
In the waste treatment apparatus 1 according to the present embodiment, the solid-liquid separation unit is moved from the biological treatment tank 21 by the transfer unit 3 by changing the rotational speed of the pump 23a2 by the sixth control signal transmission unit 42f. It is comprised so that the flow volume of the accommodation water of the biological treatment tank 21 transferred to 22 may be adjusted.
また、本実施形態に係る廃棄物処理装置１は、前記調整部４によって、前記生物処理槽２１を沈殿分離槽として機能させるように構成されている。
すなわち、前記制御信号伝達部４２は、前記撹拌部２１ａに信号で伝達する第７制御信号伝達部４２ｇを有する。
本実施形態に係る廃棄物処理装置１は、前記第７制御信号伝達部４２ｇによって、前記回転軸２１ａ１の回転数を変化させることにより、前記生物処理槽２１を沈殿分離槽として機能させるように構成されている。
In addition, the waste treatment apparatus 1 according to the present embodiment is configured so that the adjustment unit 4 causes the biological treatment tank 21 to function as a precipitation separation tank.
That is, the control signal transmission unit 42 includes a seventh control signal transmission unit 42g that transmits a signal to the stirring unit 21a.
The waste treatment apparatus 1 according to the present embodiment is configured to cause the biological treatment tank 21 to function as a precipitation separation tank by changing the rotation speed of the rotation shaft 21a1 by the seventh control signal transmission unit 42g. Has been.
さらに、本実施形態に係る廃棄物処理装置１は、前記調整部４によって、前記混合槽３５に供給される際の前記第１有機性廃棄物の油分の濃度を調整するように構成されている。
具体的には、前記制御信号伝達部４２は、前記加圧浮上部３１ｅに信号で伝達する第８制御信号伝達部４２ｈを有し、前記第８制御信号伝達部４２ｈによって、前記加圧浮上部３１ｅでの加圧条件（圧力、加圧時間等）を調整するように構成されている。
Furthermore, the waste treatment apparatus 1 according to the present embodiment is configured to adjust the concentration of the oil content of the first organic waste when supplied to the mixing tank 35 by the adjusting unit 4. .
Specifically, the control signal transmission unit 42 includes an eighth control signal transmission unit 42h that transmits a signal to the pressurization floating part 31e, and the pressurization floating part is provided by the eighth control signal transmission unit 42h. The pressurization condition (pressure, pressurization time, etc.) at 31e is adjusted.
また、前記調整部４は、下記（１）〜（３）の少なくとも何れか一を満たすようにする調整部である。
（１）前記生物処理槽内の収容水におけるノルマルヘキサン抽出物質濃度が２，２５０ｍｇ／Ｌ以下となる。
（２）前記生物処理槽内の収容水における、全蒸発残留物の強熱減量（ｍｇ／Ｌ）に対するノルマルヘキサン抽出物質濃度（ｍｇ／Ｌ）の比が０．１５以下となる。
（３）前記混合槽内の混合物における、全蒸発残留物における強熱減量（ｍｇ／Ｌ）に対するノルマルヘキサン抽出物質濃度（ｍｇ／Ｌ）の比が０．３２以下となる。
なお、本実施形態に係る対象試料におけるノルマルヘキサン抽出物質濃度は、ＪＩＳ Ｋ０１０２：２０１３に記載の方法に基づいて測定することができる。
また、本実施形態に係る対象試料における全蒸発残留物の強熱減量は、ＪＩＳ Ｋ０１０２：２０１３に記載の方法に基づいて測定することができ、下記式で求めることができる。
「対象試料における全蒸発残留物の強熱減量（ｍｇ／Ｌ）」 ＝ （全蒸発残留物の質量（ｍｇ） − 全蒸発残留物の強熱残留物の質量（ｍｇ））／対象試料の容量（Ｌ）
The adjusting unit 4 is an adjusting unit that satisfies at least one of the following (1) to (3).
(1) The normal hexane extractable substance concentration in the stored water in the biological treatment tank is 2,250 mg / L or less.
(2) The ratio of the normal hexane extractable substance concentration (mg / L) to the ignition loss (mg / L) of the total evaporation residue in the stored water in the biological treatment tank is 0.15 or less.
(3) The ratio of normal hexane extractable substance concentration (mg / L) to ignition loss (mg / L) in the total evaporation residue in the mixture in the mixing tank is 0.32 or less.
In addition, the normal hexane extract substance concentration in the target sample according to the present embodiment can be measured based on the method described in JIS K0102: 2013.
Moreover, the ignition loss of the total evaporation residue in the target sample according to the present embodiment can be measured based on the method described in JIS K0102: 2013, and can be obtained by the following equation.
“Ignition loss of total evaporation residue in target sample (mg / L)” = (mass of total evaporation residue (mg) −mass of ignition residue of total evaporation residue (mg)) / volume of target sample (L)
なお、上記（１）を満たす前記調整部４としては、前記収容水におけるノルマルヘキサン抽出物質濃度が２，２５０ｍｇ／Ｌを超えないよう、例えば、前記収容水におけるノルマルヘキサン抽出物質濃度が２，０００ｍｇ／Ｌを超えたときに、前記収容水におけるノルマルヘキサン抽出物質濃度を２，０００ｍｇ／Ｌ以下にすべく廃棄物処理装置の運転条件を調整するものが挙げられる。
即ち、前記調整部４としては、例えば、前記濃度に対して２，２５０ｍｇ／Ｌ以下の範囲内で設定された閾値に基づき廃棄物処理装置の構成機器類に対して制御を行い、前記濃度が閾値を超えた際に閾値以下に前記濃度を引き下げるとともに該濃度を処理期間通じて平均２，２５０ｍｇ／Ｌ以下、好ましくは、常時２，２５０ｍｇ／Ｌ以下とするものが挙げられる。
In addition, as the said adjustment part 4 which satisfy | fills said (1), the normal hexane extract substance density | concentration in the said accommodation water is 2000 mg so that the normal hexane extract substance density | concentration in the said accommodation water may not exceed 2,250 mg / L, for example. When it exceeds / L, the operating condition of the waste treatment apparatus is adjusted so that the normal hexane extractable substance concentration in the stored water is 2,000 mg / L or less.
That is, the adjustment unit 4 controls the constituent devices of the waste treatment apparatus based on a threshold value set within a range of 2,250 mg / L or less with respect to the concentration, for example. When the threshold value is exceeded, the concentration is lowered to the threshold value or less, and the concentration is averaged to 2,250 mg / L or less, preferably 2,250 mg / L or less throughout the treatment period.
上記（２）を満たす前記調整部４としては、例えば、前記収容水における、全蒸発残留物の強熱減量（ｍｇ／Ｌ）に対するノルマルヘキサン抽出物質濃度（ｍｇ／Ｌ）の比が０．１５を超えたときに、前記収容水における、全蒸発残留物の強熱減量（ｍｇ／Ｌ）に対するノルマルヘキサン抽出物質濃度（ｍｇ／Ｌ）の比を０．１５以下にすべく廃棄物処理装置の運転条件を調整するものが挙げられる。また、上記（２）を満たす前記調整部４としては、例えば、前記収容水における、全蒸発残留物の強熱減量（ｍｇ／Ｌ）に対するノルマルヘキサン抽出物質濃度（ｍｇ／Ｌ）の比の処理期間における平均値が０．１５以下になるように調整するものが挙げられる。また、前記調整部４は、前記収容水における、全蒸発残留物の強熱減量（ｍｇ／Ｌ）に対するノルマルヘキサン抽出物質濃度（ｍｇ／Ｌ）の比を常に０．１５以下にすることが好ましい。
即ち、前記調整部４としては、例えば、前記比に対して０．１５以下の範囲内で設定された閾値に基づき廃棄物処理装置の構成機器類に対して制御を行い、前記比が閾値を超えた際に閾値以下に前記比を引き下げるとともに該比を処理期間通じて平均０．１５以下、好ましくは、常時０．１５以下とするものが挙げられる。
As said adjustment part 4 which satisfy | fills said (2), the ratio of the normal hexane extract substance concentration (mg / L) with respect to the ignition loss (mg / L) of the total evaporation residue in the said accommodation water is 0.15, for example. Of the waste treatment apparatus so that the ratio of the normal hexane extractable substance concentration (mg / L) to the ignition loss (mg / L) of the total evaporation residue in the stored water is 0.15 or less. The thing which adjusts an operating condition is mentioned. Moreover, as the said adjustment part 4 satisfy | filling said (2), the process of the ratio of normal hexane extract substance concentration (mg / L) with respect to the ignition loss (mg / L) of the total evaporation residue in the said accommodation water, for example What adjusts so that the average value in a period may be 0.15 or less is mentioned. Moreover, it is preferable that the ratio of the normal hexane extract substance concentration (mg / L) to the ignition loss (mg / L) of the total evaporation residue in the stored water is always 0.15 or less. .
That is, for example, the adjustment unit 4 controls the constituent devices of the waste treatment apparatus based on a threshold value set within a range of 0.15 or less with respect to the ratio, and the ratio sets the threshold value. When the ratio is exceeded, the ratio is lowered to a threshold value or less, and the ratio is set to an average of 0.15 or less, preferably 0.15 or less throughout the processing period.
上記（３）を満たす前記調整部４としては、例えば、前記混合物における、全蒸発残留物における強熱減量（ｍｇ／Ｌ）に対するノルマルヘキサン抽出物質濃度（ｍｇ／Ｌ）の比が０．３２以下となるよう、例えば、前記混合物における、全蒸発残留物における強熱減量（ｍｇ／Ｌ）に対するノルマルヘキサン抽出物質濃度（ｍｇ／Ｌ）の比が０．３０を超えたときに、前記混合槽内の混合物における、全蒸発残留物における強熱減量（ｍｇ／Ｌ）に対するノルマルヘキサン抽出物質濃度（ｍｇ／Ｌ）の比を０．３０以下にすべく廃棄物処理装置の運転条件を調整するものが挙げられる。
即ち、前記調整部４としては、例えば、前記比に対して０．３２以下の範囲内で設定された閾値に基づき廃棄物処理装置の構成機器類に対して制御を行い、前記比が閾値を超えた際に閾値以下に前記比を引き下げるとともに該比を処理期間通じて平均０．３０以下、好ましくは、常時０．３０以下とするものが挙げられる。
As said adjustment part 4 which satisfy | fills said (3), the ratio of the normal hexane extract substance concentration (mg / L) with respect to the ignition loss (mg / L) in the total evaporation residue in the said mixture is 0.32 or less, for example For example, when the ratio of normal hexane extractable substance concentration (mg / L) to ignition loss (mg / L) in the total evaporation residue in the mixture exceeds 0.30, The operating conditions of the waste treatment apparatus are adjusted so that the ratio of the normal hexane extractable substance concentration (mg / L) to the ignition loss (mg / L) in the total evaporation residue is 0.30 or less. Can be mentioned.
That is, for example, the adjustment unit 4 controls the constituent devices of the waste treatment apparatus based on a threshold value set within a range of 0.32 or less with respect to the ratio, and the ratio sets the threshold value. When the ratio is exceeded, the ratio is lowered to the threshold value or less, and the ratio is set to an average of 0.30 or less, preferably 0.30 or less throughout the processing period.
前記混合槽内の混合物における、全蒸発残留物における強熱減量（ｍｇ／Ｌ）に対するノルマルヘキサン抽出物質濃度（ｍｇ／Ｌ）の比が０．２６以下となることが好ましい。
上記（３）を満たす前記調整部４としては、例えば、前記混合物における、全蒸発残留物における強熱減量（ｍｇ／Ｌ）に対するノルマルヘキサン抽出物質濃度（ｍｇ／Ｌ）の比が０．２６以下となるよう、例えば、前記混合物における、全蒸発残留物における強熱減量（ｍｇ／Ｌ）に対するノルマルヘキサン抽出物質濃度（ｍｇ／Ｌ）の比が０．２５を超えたときに、前記混合槽内の混合物における、全蒸発残留物における強熱減量（ｍｇ／Ｌ）に対するノルマルヘキサン抽出物質濃度（ｍｇ／Ｌ）の比を０．２５以下にすべく廃棄物処理装置の運転条件を調整するものが挙げられる。
即ち、前記調整部４としては、例えば、前記比に対して０．２６以下の範囲内で設定された閾値に基づき廃棄物処理装置の構成機器類に対して制御を行い、前記比が閾値を超えた際に閾値以下に前記比を引き下げるとともに該比を処理期間通じて平均０．２５以下、好ましくは、常時０．２５以下とするものが挙げられる。
It is preferable that the ratio of the normal hexane extractable substance concentration (mg / L) to the ignition loss (mg / L) in the total evaporation residue in the mixture in the mixing tank is 0.26 or less.
As said adjustment part 4 which satisfy | fills said (3), the ratio of the normal hexane extract substance concentration (mg / L) with respect to the ignition loss (mg / L) in the total evaporation residue in the said mixture is 0.26 or less, for example For example, when the ratio of normal hexane extractable substance concentration (mg / L) to ignition loss (mg / L) in the total evaporation residue in the mixture exceeds 0.25, In this mixture, the operating condition of the waste treatment apparatus is adjusted so that the ratio of the normal hexane extractable substance concentration (mg / L) to the ignition loss (mg / L) in the total evaporation residue is 0.25 or less. Can be mentioned.
That is, for example, the adjustment unit 4 controls the constituent devices of the waste treatment apparatus based on a threshold value set within a range of 0.26 or less with respect to the ratio, and the ratio sets the threshold value. When the ratio is exceeded, the ratio is lowered to a threshold value or less, and the ratio is set to an average of 0.25 or less, preferably 0.25 or less throughout the processing period.
本実施形態に係る廃棄物処理装置は、上記の如く構成されているが、次に、本実施形態に係る廃棄物処理方法について説明する。 The waste treatment apparatus according to this embodiment is configured as described above. Next, the waste treatment method according to this embodiment will be described.
本実施形態に係る廃棄物処理方法では、本実施形態に係る廃棄物処理装置を用いて廃棄物を生物処理する。 In the waste treatment method according to this embodiment, the waste is biologically treated using the waste treatment apparatus according to this embodiment.
一実施形態に係る廃棄物処理方法は、油分を含む第１有機性廃棄物、及び、該第１有機性廃棄物よりも油分濃度が低い第２有機性廃棄物を前記生物処理槽２１内でメタン生成菌により生物処理する生物処理工程を有する処理工程と、前記第１有機性廃棄物及び前記第２有機性廃棄物を前記生物処理槽２１に移送する移送工程とを備えており、下記（１）及び（２）の少なくとも何れか一方を満たすように前記生物処理槽２１内の収容水を調整する。
（１）前記生物処理槽２１内の収容水のノルマルヘキサン抽出物質濃度が２，２５０ｍｇ／Ｌ以下となる。
（２）前記生物処理槽２１内の収容水における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比が０．１５以下となる。
In the waste treatment method according to an embodiment, a first organic waste containing oil and a second organic waste having a lower oil concentration than the first organic waste are contained in the biological treatment tank 21. A treatment process having a biological treatment process for biological treatment with a methanogen, and a transfer process for transferring the first organic waste and the second organic waste to the biological treatment tank 21, The stored water in the biological treatment tank 21 is adjusted so as to satisfy at least one of 1) and (2).
(1) The normal hexane extract substance concentration of the water contained in the biological treatment tank 21 is 2,250 mg / L or less.
(2) The ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the stored water in the biological treatment tank 21 is 0.15 or less.
他の実施形態に係る廃棄物処理方法は、油分を含む第１有機性廃棄物、及び、該第１有機性廃棄物よりも油分濃度が低い第２有機性廃棄物を生物処理槽２１内でメタン生成菌により生物処理する生物処理工程を有する処理工程と、前記第１有機性廃棄物及び前記第２有機性廃棄物を前記生物処理槽２１に移送する移送工程とを備えている。
前記移送工程は、前記第１有機性廃棄物を混合槽３５に移送する第１移送工程と、前記第２有機性廃棄物を前記混合槽３５に移送する第２移送工程と、前記第１有機性廃棄物及び前記第２有機性廃棄物を前記混合槽３５で混合することにより混合物を得る混合工程と、該混合物を前記生物処理槽２１に移送する第３移送工程とを有する。
また、該廃棄物処理方法は、前記混合槽３５内の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比が０．３２以下となるように前記混合槽３５内の混合物を調整する。
In the waste treatment method according to another embodiment, the first organic waste containing oil and the second organic waste having a lower oil concentration than the first organic waste are contained in the biological treatment tank 21. A treatment process having a biological treatment process for biological treatment with a methane-producing bacterium, and a transfer process for transferring the first organic waste and the second organic waste to the biological treatment tank 21.
The transfer step includes a first transfer step of transferring the first organic waste to the mixing tank 35, a second transfer step of transferring the second organic waste to the mixing tank 35, and the first organic A mixing step of mixing the organic waste and the second organic waste in the mixing tank 35, and a third transfer step of transferring the mixture to the biological treatment tank 21.
The waste treatment method also includes a mixture in the mixing tank 35 such that the ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the mixture in the mixing tank 35 is 0.32 or less. Adjust.
本実施形態に係る廃棄物処理方法の前記移送工程は、前記第１有機性廃棄物を前記混合槽３５に移送する第１移送工程と、前記第２有機性廃棄物を前記混合槽３５に移送する第２移送工程と、前記第１有機性廃棄物及び前記第２有機性廃棄物を前記混合槽３５で混合することにより混合物を得る混合工程と、該混合物を前記生物処理槽２１に移送する第３移送工程と、前記混合槽３５を介さずに前記生物処理槽２１に前記第２有機性廃棄物を移送する第４移送工程とを有することが好ましい。 The transfer step of the waste treatment method according to the present embodiment includes a first transfer step of transferring the first organic waste to the mixing tank 35, and a transfer of the second organic waste to the mixing tank 35. A second transfer step, a mixing step of obtaining the mixture by mixing the first organic waste and the second organic waste in the mixing tank 35, and transferring the mixture to the biological treatment tank 21. It is preferable to include a third transfer step and a fourth transfer step of transferring the second organic waste to the biological treatment tank 21 without using the mixing tank 35.
本実施形態に係る廃棄物処理方法の前記処理工程は、前記生物処理槽２１内の収容水を前記生物処理槽２１から固液分離部に移送する収容水移送工程と、前記収容水を前記固液分離部２２で固液分離することにより、前記収容水よりも含水率が高い分離水、及び、前記収容水よりも含水率が低い濃縮物を得る固液分離工程と、前記分離水を前記生物処理槽２１に移送する分離水移送工程とをさらに有することが好ましい。 The treatment step of the waste treatment method according to the present embodiment includes: a contained water transfer step for transferring the contained water in the biological treatment tank 21 from the biological treatment tank 21 to a solid-liquid separation unit; Solid-liquid separation in the liquid separation unit 22 to obtain a separated water having a higher water content than the stored water, and a concentrate having a lower water content than the stored water, and the separated water to the It is preferable to further include a separated water transfer step for transferring to the biological treatment tank 21.
また、本実施形態に係る廃棄物処理方法の前記処理工程は、メタン生成菌により生物処理を実施し、前記生物処理槽２１内の収容水を前記生物処理槽２１で沈殿分離することにより、前記収容水よりも含水率が高い分離水、及び、前記収容水よりも含水率が低い濃縮物を得る固液分離工程と、前記濃縮物を前記生物処理槽２１外に移送する濃縮物移送工程をさらに有することが好ましい。 In addition, the treatment step of the waste treatment method according to the present embodiment performs biological treatment with methane-producing bacteria, and precipitates and separates the water contained in the biological treatment tank 21 in the biological treatment tank 21, thereby A separation water having a higher water content than the stored water, a solid-liquid separation step for obtaining a concentrate having a lower water content than the stored water, and a concentrate transfer step for transferring the concentrate to the outside of the biological treatment tank 21. Furthermore, it is preferable to have.
前記処理工程は、前記沈殿分離以前において前記生物処理槽２１内の収容水を該収容水内で回転する撹拌翼２１ａ２によって撹拌し、前記沈殿分離では、前記撹拌翼２１ａ２の回転速度を低下させることが好ましい。
このように前記撹拌翼２１ａ２の回転速度を低下させることで、油分が付着して活性の低下した汚泥の沈殿を促進させることができる。
なお、この沈殿分離に際しては、前記撹拌翼２１ａ２が停止状態となるまで回転速度を低下させることが好ましい。
In the treatment step, the stored water in the biological treatment tank 21 is stirred by the stirring blade 21a2 rotating in the stored water before the precipitation separation, and in the precipitation separation, the rotation speed of the stirring blade 21a2 is reduced. Is preferred.
Thus, by lowering the rotation speed of the agitating blade 21a2, it is possible to promote sedimentation of sludge having a reduced activity due to oil adhesion.
In this precipitation separation, it is preferable to reduce the rotation speed until the stirring blade 21a2 is stopped.
本実施形態に係る廃棄物処理装置および廃棄物処理方法は、上記のように構成されているので、以下の利点を有するものである。 Since the waste processing apparatus and the waste processing method according to the present embodiment are configured as described above, they have the following advantages.
即ち、本実施形態に係る廃棄物処理装置１は、油分を含む第１有機性廃棄物、及び、該第１有機性廃棄物よりも油分濃度が低い第２有機性廃棄物をメタン生成菌で生物処理する生物処理槽２１を有する処理部２と、前記第１有機性廃棄物及び前記第２有機性廃棄物を前記生物処理槽２１に移送する移送部３と、下記（１）及び（２）の少なくとも何れか一方を満たすように前記生物処理槽２１内の収容水を調整する調整部４とを備えている。
（１）前記生物処理槽２１内の収容水のノルマルヘキサン抽出物質濃度が２，２５０ｍｇ／Ｌ以下となる。
（２）前記生物処理槽２１内の収容水における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比が０．１５以下となる。
対象試料におけるノルマルヘキサン抽出物質濃度は、対象試料における油分濃度の指標となる。
よって、斯かる廃棄物処理装置１によれば、前記生物処理槽２１内の収容水のノルマルヘキサン抽出物質濃度を２，２５０ｍｇ／Ｌ以下にすることにより、前記生物処理槽２１内の収容水中の汚泥に付着する油分の量をより一層抑制することができる。その結果、斯かる廃棄物処理装置１によれば、生物たるメタン生成菌の活性の低下をより一層抑制し得る。
また、対象試料における、全蒸発残留物の強熱減量は、対象試料における、メタン生成菌で分解できる有機物濃度の指標となる。
よって、斯かる廃棄物処理装置１によれば、前記生物処理槽２１内の収容水における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比を０．１５以下にすることにより、前記生物処理槽２１内の収容水に含まれる油分を前記第２有機性廃棄物に付着させることができる。その結果、斯かる廃棄物処理装置１によれば、生物たるメタン生成菌の活性の低下を抑制し得る。
That is, the waste treatment apparatus 1 according to the present embodiment uses a methanogenic bacterium to produce a first organic waste containing oil and a second organic waste having a lower oil concentration than the first organic waste. A treatment unit 2 having a biological treatment tank 21 for biological treatment, a transfer unit 3 for transferring the first organic waste and the second organic waste to the biological treatment tank 21, and the following (1) and (2 ) To adjust the water contained in the biological treatment tank 21 so as to satisfy at least one of them.
(1) The normal hexane extract substance concentration of the water contained in the biological treatment tank 21 is 2,250 mg / L or less.
(2) The ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the stored water in the biological treatment tank 21 is 0.15 or less.
The normal hexane extractable substance concentration in the target sample is an index of the oil concentration in the target sample.
Therefore, according to the waste treatment apparatus 1, by setting the normal hexane extract substance concentration of the water contained in the biological treatment tank 21 to 2,250 mg / L or less, The amount of oil adhering to the sludge can be further suppressed. As a result, according to the waste treatment apparatus 1, it is possible to further suppress the decrease in the activity of the biological methanogen.
Further, the loss on ignition of the total evaporation residue in the target sample is an index of the organic matter concentration in the target sample that can be decomposed by the methanogen.
Therefore, according to the waste treatment apparatus 1, by setting the ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the stored water in the biological treatment tank 21 to 0.15 or less, The oil contained in the stored water in the biological treatment tank 21 can be attached to the second organic waste. As a result, according to the waste treatment apparatus 1, it is possible to suppress a decrease in the activity of the biological methanogen.
また、本実施形態に係る廃棄物処理装置１では、前記移送部３は、前記第１有機性廃棄物及び前記第２有機性廃棄物を混合することにより混合物を得る混合槽３５と、前記第１有機性廃棄物を前記混合槽３５に移送する第１移送部３１と、前記第２有機性廃棄物を前記混合槽３５に移送する第２移送部３２と、前記混合物を前記生物処理槽２１に移送する第３移送部３３とを有する。
斯かる廃棄物処理装置１によれば、処理すべき第１有機性廃棄物の量が多くなった場合や、第１有機性廃棄物の油分濃度が高くなった場合でも、前記第１有機性廃棄物及び前記第２有機性廃棄物を前記混合槽３５で一旦貯めることができるので、前記生物処理槽２１における油分濃度の上昇を抑制することができる。その結果、前記生物処理槽２１内の汚泥に付着する油分の量を抑制することができる。
Further, in the waste treatment apparatus 1 according to the present embodiment, the transfer unit 3 includes a mixing tank 35 that obtains a mixture by mixing the first organic waste and the second organic waste, and the first 1st transfer part 31 which transfers 1 organic waste to the said mixing tank 35, 2nd transfer part 32 which transfers the said 2nd organic waste to the said mixing tank 35, and the said biological treatment tank 21 And a third transfer part 33 for transferring to
According to such a waste treatment apparatus 1, even when the amount of the first organic waste to be processed increases or when the oil concentration of the first organic waste increases, the first organic waste Since the waste and the second organic waste can be temporarily stored in the mixing tank 35, an increase in the oil concentration in the biological treatment tank 21 can be suppressed. As a result, the amount of oil adhering to the sludge in the biological treatment tank 21 can be suppressed.
また、本実施形態に係る廃棄物処理装置１では、前記調整部４は、前記混合槽３５内の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比が０．３２以下となるように前記混合槽３５内の混合物を調整する調整部である。
斯かる廃棄物処理装置１によれば、前記混合槽３５内の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比を０．３２以下にすることにより、前記混合槽３５内の収容水中の汚泥に付着する油分の量を抑制することができる。その結果、斯かる廃棄物処理装置１によれば、前記生物処理槽２１内の収容水中の汚泥に付着する油分の量もより一層抑制することができ、生物たるメタン生成菌の活性の低下をより一層抑制し得る。
Further, in the waste treatment apparatus 1 according to the present embodiment, the adjustment unit 4 is configured such that the ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the mixture in the mixing tank 35 is 0.32 or less. It is an adjustment part which adjusts the mixture in the said mixing tank 35 so that it may become.
According to the waste treatment apparatus 1, the ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the mixture in the mixing tank 35 is set to 0.32 or less, thereby the mixing tank 35. The amount of oil adhering to the sludge in the contained water can be suppressed. As a result, according to the waste treatment apparatus 1, the amount of oil adhering to the sludge in the stored water in the biological treatment tank 21 can be further suppressed, and the decrease in the activity of the biological methanogen is reduced. It can be further suppressed.
また、本実施形態に係る廃棄物処理装置１は、油分を含む第１有機性廃棄物、及び、該第１有機性廃棄物よりも油分濃度が低い第２有機性廃棄物をメタン生成菌で生物処理する生物処理槽２１を有する処理部２と、前記第１有機性廃棄物及び前記第２有機性廃棄物を前記生物処理槽に移送する移送部３とを備えている。前記移送部３は、前記第１有機性廃棄物及び前記第２有機性廃棄物を混合することにより混合物を得る混合槽３５と、前記第１有機性廃棄物を前記混合槽３５に移送する第１移送部３１と、前記第２有機性廃棄物を前記混合槽３５に移送する第２移送部３２と、前記混合物を前記生物処理槽２１に移送する第３移送部３３とを有する。本実施形態に係る廃棄物処理装置１は、前記混合槽３５内の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比が０．３２以下となるように前記混合槽３５内の混合物を調整する調整部をさらに備えている。 Moreover, the waste treatment apparatus 1 which concerns on this embodiment is the 1st organic waste containing oil content, and the 2nd organic waste whose oil content concentration is lower than this 1st organic waste by methanogen. A treatment unit 2 having a biological treatment tank 21 for biological treatment and a transfer unit 3 for transferring the first organic waste and the second organic waste to the biological treatment tank are provided. The transfer unit 3 includes a mixing tank 35 that obtains a mixture by mixing the first organic waste and the second organic waste, and a first tank that transfers the first organic waste to the mixing tank 35. 1 transfer part 31, a second transfer part 32 for transferring the second organic waste to the mixing tank 35, and a third transfer part 33 for transferring the mixture to the biological treatment tank 21. In the waste treatment apparatus 1 according to this embodiment, the mixing tank 35 is configured such that the ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the mixture in the mixing tank 35 is 0.32 or less. An adjustment unit for adjusting the inner mixture is further provided.
さらに、本実施形態に係る廃棄物処理装置１では、前記生物処理槽２１は、前記生物処理槽２１内の収容水のｐＨ及び前記収容水から発生するガスのメタン濃度の少なくとも一方の値を測定する測定部２１ｂを有する。前記調整部４は、前記測定部２１ｂで測定した生物処理槽２１内の収容水のｐＨ及び前記収容水から発生するガスのメタン濃度の少なくとも一方の値に基づいて、前記調整をする調整部である。
前記生物処理槽２１内の収容水のｐＨ及び前記収容水から発生するガスのメタン濃度はそれぞれメタン生成菌の活性状態の指標となるので、斯かる廃棄物処理装置１によれば、生物たるメタン生成菌の活性の低下をより一層抑制し得る。
有機物のメタン発酵に機能する菌は、通常、至適ｐＨが中性（ｐＨ７）付近に存在し、有機物から有機酸を経由してメタンを生成する。このとき、メタンとともに二酸化炭素も発生し、メタンと二酸化炭素との合計に占めるメタンの割合は、概ね、５０体積％以上である。
そして、メタン生成菌に油分が付着するなどして菌が十分に活動できなくなると、生物処理槽の収容水のｐＨが低下し、該収容水から発生するガスのメタン濃度が低下する。
従って、本実施形態においては、ｐＨが６．５以下に低下したときやガスのメタン濃度が６０体積％以下に低下したときに前記調整部４によって廃棄物処理装置１の運転条件を調整することが好ましい。
Furthermore, in the waste treatment apparatus 1 according to the present embodiment, the biological treatment tank 21 measures at least one of the pH of the contained water in the biological treatment tank 21 and the methane concentration of the gas generated from the contained water. Measuring part 21b. The adjusting unit 4 is an adjusting unit that performs the adjustment based on at least one value of the pH of the stored water in the biological treatment tank 21 measured by the measuring unit 21b and the methane concentration of the gas generated from the stored water. is there.
Since the pH of the stored water in the biological treatment tank 21 and the methane concentration of the gas generated from the stored water are indicators of the active state of the methane producing bacteria, according to the waste treatment apparatus 1, the biological methane A decrease in the activity of the producing bacteria can be further suppressed.
Bacteria that function in methane fermentation of organic matter usually have an optimum pH near neutral (pH 7), and produce methane from the organic matter via an organic acid. At this time, carbon dioxide is generated together with methane, and the proportion of methane in the total of methane and carbon dioxide is approximately 50% by volume or more.
And when oil becomes attached to methanogenic bacteria and the bacteria cannot sufficiently act, the pH of the stored water in the biological treatment tank decreases, and the methane concentration of the gas generated from the stored water decreases.
Therefore, in this embodiment, the operating condition of the waste treatment apparatus 1 is adjusted by the adjusting unit 4 when the pH is lowered to 6.5 or less or when the gas methane concentration is lowered to 60% by volume or less. Is preferred.
さらに、本実施形態に係る廃棄物処理装置１は、前記第１有機性廃棄物が厨房排水を含有し、前記第２有機性廃棄物が厨芥を含有してもよい。 Furthermore, in the waste treatment apparatus 1 according to this embodiment, the first organic waste may contain kitchen wastewater, and the second organic waste may contain soot.
また、本実施形態に係る廃棄物処理装置１では、前記移送部３は、前記混合槽３５を介さずに前記生物処理槽２１に前記第２有機性廃棄物を移送する第４移送部３４を備えている。
斯かる廃棄物処理装置１によれば、前記混合槽３５を介さずに前記生物処理槽２１に前記第２有機性廃棄物を前記第４移送部３４で移送することにより、前記生物処理槽２１内の収容水に含まれる油分を前記第２有機性廃棄物に付着させることができる。その結果、前記生物処理槽２１内の汚泥に油分が付着するのを抑制することができる。
よって、斯かる廃棄物処理装置１によれば、油分を含めた有機物を生物で分解させつつも、生物の活性の低下を抑制し得る。
上記効果をより顕著に発揮させる上において、混合槽を介さずに生物処理槽に導入させる第２有機性廃棄物は、ノルマルヘキサン抽出物質濃度が１０，０００ｍｇ／Ｌ以下であることが好ましい。
また、混合槽を介さずに生物処理槽に導入される第２有機性廃棄物は、厨芥の粉砕物などの有機性固形分を１０質量％以上含有していることが好ましい。
さらに、第２有機性廃棄物に含まれる有機性固形分は、第２有機性廃棄物の全量が４０ｍｍメッシュのふるいを通過するように微粉砕されていることが、油分を付着させるために表面積を大きく確保できる点において好適である。
In the waste treatment apparatus 1 according to this embodiment, the transfer unit 3 includes a fourth transfer unit 34 that transfers the second organic waste to the biological treatment tank 21 without using the mixing tank 35. I have.
According to such a waste treatment apparatus 1, the second organic waste is transferred to the biological treatment tank 21 by the fourth transfer unit 34 without passing through the mixing tank 35, thereby the biological treatment tank 21. The oil contained in the contained water can be attached to the second organic waste. As a result, oil can be prevented from adhering to the sludge in the biological treatment tank 21.
Therefore, according to such a waste treatment apparatus 1, it is possible to suppress a decrease in the activity of the organism while decomposing the organic matter including the oil in the organism.
In order to exert the above effect more remarkably, the second organic waste introduced into the biological treatment tank without going through the mixing tank preferably has a normal hexane extract substance concentration of 10,000 mg / L or less.
Moreover, it is preferable that the 2nd organic waste introduce | transduced into a biological treatment tank without passing through a mixing tank contains 10 mass% or more of organic solid content, such as a ground material of a firewood.
Furthermore, the organic solid content contained in the second organic waste is pulverized so that the entire amount of the second organic waste passes through a 40 mm mesh screen. This is preferable in that it can be ensured.
また、本実施形態に係る廃棄物処理装置１では、前記処理部２は、前記生物処理槽２１内の収容水を固液分離することにより、前記収容水よりも含水率が高い分離水、及び、前記収容水よりも含水率が低い濃縮物を得る固液分離部２２と、前記収容水を前記生物処理槽２１から前記固液分離部２２に移送する収容水移送部２３ａと、前記分離水を前記生物処理槽２１に移送する分離水移送部２３ｂとを有する。
油分は汚泥に吸着しやすいので、斯かる廃棄物処理装置１によれば、前記生物処理槽２１内の収容水を固液分離することにより、油分を濃縮物に濃縮させることができる。また、油分が付着することにより活性が低下した生物を有する汚泥も濃縮物に濃縮させることができる。よって、該濃縮物を前記生物処理槽２１外に排出すれば、前記生物処理槽２１におけるメタン生成菌たる生物の活性の低下を抑制することができる。
また、前記分離水を前記生物処理槽２１に移送することにより、分離水に含まれる未分解の有機物を前記生物処理槽２１に戻すことができる。その結果、分離水に含まれる有機物を前記生物処理槽２１で分解させつつも、前記生物処理槽２１のメタン生成菌たる生物の活性を高めることができる。
よって、斯かる廃棄物処理装置１によれば、メタン生成菌たる生物の活性の低下をより一層抑制し得る。
Further, in the waste treatment apparatus 1 according to the present embodiment, the treatment unit 2 separates the contained water in the biological treatment tank 21 by solid-liquid separation, thereby separating water having a higher water content than the contained water, and The solid-liquid separation unit 22 for obtaining a concentrate having a lower water content than the stored water, the stored water transfer unit 23a for transferring the stored water from the biological treatment tank 21 to the solid-liquid separation unit 22, and the separated water And a separated water transfer section 23b for transferring the water to the biological treatment tank 21.
Since the oil component is easily adsorbed by the sludge, according to the waste treatment apparatus 1, the oil component can be concentrated to the concentrate by solid-liquid separation of the water stored in the biological treatment tank 21. In addition, sludge having organisms whose activity has decreased due to the adhesion of oil can also be concentrated to a concentrate. Therefore, if this concentrate is discharged | emitted out of the said biological treatment tank 21, the fall of the activity of the organism which is a methanogen in the said biological treatment tank 21 can be suppressed.
Further, by transferring the separated water to the biological treatment tank 21, undecomposed organic matter contained in the separated water can be returned to the biological treatment tank 21. As a result, it is possible to increase the activity of the organism that is a methanogen in the biological treatment tank 21 while decomposing the organic matter contained in the separated water in the biological treatment tank 21.
Therefore, according to such a waste treatment apparatus 1, it is possible to further suppress the decrease in the activity of the organism that is a methane-producing bacterium.
なお、本実施形態に係る廃棄物処理装置１では、生物処理槽の収容水のノルマルヘキサン抽出物質濃度が上昇傾向にある場合は、生物処理槽に移送する第１有機性廃棄物の流量、及び、第２有機性廃棄物の流量を調整するように構成されている。
また、本実施形態に係る廃棄物処理装置１では、生物処理槽の収容水のノルマルヘキサン抽出物質濃度が２，２５０ｍｇ／Ｌを超える等した場合には、生物処理槽に移送する第１有機性廃棄物の流量を減少させる。
さらに、本実施形態に係る廃棄物処理装置１では、生物処理槽に移送する第２有機性廃棄物の流量を増加させるには、生物処理槽の油分濃度の上昇が緩やかである場合（緊急の対応を要さない場合）には、混合槽に移送する第２有機性廃棄物の流量を増加させ、生物処理槽の油分濃度の上昇が急激である場合（緊急の対応を要する場合）には、混合槽を介さずに生物処理槽に移送する第２有機性廃棄物の流量を増加させるように構成されている。また、緊急の対応を要する場合には、生物処理槽に移送する第１有機性廃棄物の流量も減少させるように構成されている。
In the waste treatment apparatus 1 according to the present embodiment, when the normal hexane extractable substance concentration in the water stored in the biological treatment tank tends to increase, the flow rate of the first organic waste transferred to the biological treatment tank, and The flow rate of the second organic waste is adjusted.
Moreover, in the waste treatment apparatus 1 which concerns on this embodiment, when the normal hexane extract substance density | concentration of the accommodation water of a biological treatment tank exceeds 2,250 mg / L etc., the 1st organic property transferred to a biological treatment tank. Reduce waste flow.
Furthermore, in the waste treatment apparatus 1 according to the present embodiment, in order to increase the flow rate of the second organic waste transferred to the biological treatment tank, when the oil concentration in the biological treatment tank is gradually increased (emergency If no action is required), increase the flow rate of the second organic waste to be transferred to the mixing tank, and if the oil concentration in the biological treatment tank rises rapidly (when urgent action is required) The flow rate of the second organic waste transferred to the biological treatment tank without going through the mixing tank is increased. Moreover, when an urgent response is required, it is comprised so that the flow volume of the 1st organic waste transferred to a biological treatment tank may also be reduced.
さらに、本実施形態に係る廃棄物処理装置１では、前記処理部２の生物処理槽２１は、前記生物処理槽２１内の収容水を沈殿分離することにより、前記収容水よりも含水率が高い分離水、及び、前記収容水よりも含水率が低い濃縮物を得る沈殿分離槽であり、前記収容水移送部２３ａは、前記沈殿分離槽で得られた濃縮物を前記収容水として前記生物処理槽２１から前記固液分離部２２に移送する収容水移送部である。
斯かる廃棄物処理装置１によれば、前記生物処理槽２１で得られた分離水を該生物処理槽２１に留め、更に、前記生物処理槽２１で得られた濃縮物をさらに前記固液分離部２２で固液分離し、該固液分離部２２で得られた分離水を前記生物処理槽２１に戻すので、未分解の有機物を前記生物処理槽２１で生物処理することができる。その結果、分離水に含まれる有機物を前記生物処理槽２１で分解させつつも、前記生物処理槽２１のメタン生成菌たる生物の活性を高めることができる。
Furthermore, in the waste treatment apparatus 1 according to the present embodiment, the biological treatment tank 21 of the processing unit 2 has a higher water content than the stored water by precipitating and separating the stored water in the biological treatment tank 21. A separation / separation tank for obtaining separated water and a concentrate having a lower water content than the stored water, and the stored water transfer unit 23a uses the concentrate obtained in the precipitation / separation tank as the stored water for the biological treatment. It is a stored water transfer section that transfers the tank 21 to the solid-liquid separation section 22.
According to such a waste treatment apparatus 1, the separated water obtained in the biological treatment tank 21 is retained in the biological treatment tank 21, and the concentrate obtained in the biological treatment tank 21 is further separated into the solid-liquid separation. Since the solid-liquid separation is performed in the unit 22 and the separated water obtained in the solid-liquid separation unit 22 is returned to the biological treatment tank 21, undecomposed organic matter can be biologically treated in the biological treatment tank 21. As a result, it is possible to increase the activity of the organism that is a methanogen in the biological treatment tank 21 while decomposing the organic matter contained in the separated water in the biological treatment tank 21.
なお、本発明に係る廃棄物処理装置および廃棄物処理方法は、上記実施形態に限定されるものではない。また、本発明に係る廃棄物処理装置および廃棄物処理方法は、上記した作用効果に限定されるものでもない。本発明に係る廃棄物処理装置および廃棄物処理方法は、本発明の要旨を逸脱しない範囲で種々の変更が可能である。 Note that the waste treatment apparatus and the waste treatment method according to the present invention are not limited to the above embodiment. Further, the waste treatment apparatus and the waste treatment method according to the present invention are not limited to the above-described effects. The waste treatment apparatus and the waste treatment method according to the present invention can be variously modified without departing from the gist of the present invention.
例えば、本実施形態に係る廃棄物処理装置１は、前記生物処理槽２１と別体の前記固液分離部２２を備えているが、図２に示すように、他の実施形態に係る廃棄物処理装置１は、前記固液分離部２２を備えず、前記生物処理槽２１で沈殿分離して得られた濃縮物Ｆ’を収容水として前記生物処理槽２１外に移送する収容水移送部２３ａを備えている。
斯かる廃棄物処理装置１によれば、前記生物処理槽２１で得られた分離水を該生物処理槽２１に留め、更に、前記生物処理槽２１で得られた濃縮物Ｆ’を前記生物処理槽２１外に移送するので、未分解の有機物を多く前記生物処理槽２１に留めつつ、油分と、活性が低下した生物を有する汚泥とを多く前記生物処理槽２１外に排出することができる。その結果、分離水に含まれる有機物を前記生物処理槽２１で分解させつつも、前記生物処理槽２１のメタン生成菌たる生物の活性を高めることができる。
For example, the waste treatment apparatus 1 according to the present embodiment includes the solid-liquid separation unit 22 that is separate from the biological treatment tank 21, but as illustrated in FIG. 2, the waste according to another embodiment. The treatment apparatus 1 does not include the solid-liquid separation unit 22, and the stored water transfer unit 23 a that transfers the concentrate F ′ obtained by precipitation separation in the biological treatment tank 21 to the outside of the biological treatment tank 21 as stored water. It has.
According to the waste treatment apparatus 1, the separated water obtained in the biological treatment tank 21 is retained in the biological treatment tank 21, and the concentrate F ′ obtained in the biological treatment tank 21 is further treated with the biological treatment tank 21. Since it is transferred to the outside of the tank 21, a large amount of oil and sludge having organisms with reduced activity can be discharged out of the biological treatment tank 21 while retaining a large amount of undecomposed organic matter in the biological treatment tank 21. As a result, it is possible to increase the activity of the organism that is a methanogen in the biological treatment tank 21 while decomposing the organic matter contained in the separated water in the biological treatment tank 21.
次に、試験例を挙げて本発明についてさらに具体的に説明する。 Next, the present invention will be described more specifically with reference to test examples.
（試験例１）
メタン生成菌で生物処理する生物処理槽たるジャーファメンター（容積：１０Ｌ）に８Ｌの種汚泥を投入して、実験を開始した。
種汚泥については、食品工場の高温メタン発酵槽から採取した発酵液を保温容器に入れて持ち帰ったものを種汚泥として実験に供した。
ジャーファメンターたる生物処理槽の温度は５５℃（生物処理槽におけるメタン発酵が高温メタン発酵となる温度）とした。
複数のレストランから排出される厨芥をディスポーザで破砕した後、約１０倍量の希釈水で希釈して、流動性をもたせて配管で輸送し、生物処理槽投入前に１ｍｍ目のスクリーンで固液分離した厨芥固形物を第２有機性廃棄物として用いた。
また、同じくレストランから排出される厨房排水を加圧浮上分離して得られたスカムを第１有機性廃棄物として用いた。
そして、厨芥固形物とスカムとを質量混合比１：０〜１：２で混合槽に投入し、混合物を得た。この質量混合比を変化させることで、混合槽の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比（ｎ−Ｈｅｘ／ＶＳ）を０．０７〜０．３３に変化させた。
そして、チューブポンプを用いて混合物を１日あたり１回から８回に分けてジャーファメンターたる生物処理槽に投入した。
なお、チューブポンプ等が詰まるのを防止するために、チューブポンプを用いて混合物を移送させる前に、混合物をミキサーで細かく粉砕した。
(Test Example 1)
An experiment was started by introducing 8 L of seed sludge into a jar fermenter (volume: 10 L) which is a biological treatment tank for biological treatment with methanogens.
For the seed sludge, the fermented liquor collected from the high-temperature methane fermenter in the food factory was put in a heat-retaining container and brought back to the experiment as seed sludge.
The temperature of the biological treatment tank as a jar fermenter was 55 ° C. (temperature at which methane fermentation in the biological treatment tank becomes high-temperature methane fermentation).
After crushing the potatoes discharged from multiple restaurants with a disposer, dilute it with about 10 times the amount of diluted water, give it fluidity and transport it through a pipe. The separated soot solid was used as the second organic waste.
Similarly, scum obtained by pressurizing and separating the kitchen wastewater discharged from the restaurant was used as the first organic waste.
And soot solid substance and scum were thrown into the mixing tank by mass mixing ratio 1: 0 to 1: 2, and the mixture was obtained. By changing this mass mixing ratio, the ratio of n-hexane extract substance concentration (n-Hex / VS) to the ignition loss of the total evaporation residue in the mixture in the mixing tank was changed to 0.07 to 0.33. It was.
Then, the mixture was divided into 1 to 8 times per day using a tube pump and charged into a biological treatment tank as a jar fermenter.
In order to prevent clogging of the tube pump or the like, the mixture was finely pulverized with a mixer before the mixture was transferred using the tube pump.
（試験例１の結果）
図３には、混合槽の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比（混合槽内ｎ−Ｈｅｘ／ＶＳ）と、生物処理槽内の収容水のノルマルヘキサン抽出物質濃度（生物処理槽内ｎ−Ｈｅｘ）との関係を示す。
また、図４には、混合槽の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比（混合槽内ｎ−Ｈｅｘ／ＶＳ）と、生物処理槽内ガス中のメタン濃度（生物処理槽内ガス中ＣＨ４）との関係を示す。
なお、各図に示す、生物処理槽内ガス中のメタン濃度は、体積％を意味する。
混合槽の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比（混合槽内ｎ−Ｈｅｘ／ＶＳ）が０．２６以下であると、生物処理槽内の収容水のノルマルヘキサン抽出物質濃度（生物処理槽内ｎ−Ｈｅｘ）を低く抑えられる傾向が認められ、同時に生物処理槽内ガス中のメタン濃度（生物処理槽内ガス中ＣＨ４）を高く維持できる傾向が認められた。
これは、混合槽の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比（混合槽内ｎ−Ｈｅｘ／ＶＳ）が低くなることにより、生物処理槽内のメタン生成菌の活性が高められたため、すなわち、メタン発酵が促進されたためと推察される。
なお、通常、生物処理する場合には、生物処理槽に供給する、生物処理の対象となる物質の量を急激に上げずに少しずつ上げることにより、生物を含む汚泥を馴養させながら生物処理する。
しかし、試験例１では、通常よりも馴養を簡略化し、混合槽の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比を急激に変化させた条件下で試験を行った。
したがって、通常よりも馴養を簡略化し、混合槽の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比を急激に変化させた条件下では、混合槽の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比は、０．２６以下であることが好ましい。
(Result of Test Example 1)
FIG. 3 shows the ratio of the normal hexane extractable substance concentration to the loss on ignition of the total evaporation residue in the mixture in the mixing tank (n-Hex / VS in the mixing tank) and the normal hexane extraction of the water contained in the biological treatment tank. The relationship with substance concentration (n-Hex in a biological treatment tank) is shown.
FIG. 4 also shows the ratio of the normal hexane extractable substance concentration to the loss on ignition of the total evaporation residue in the mixture in the mixing tank (n-Hex / VS in the mixing tank) and the methane concentration in the gas in the biological treatment tank. The relationship with (CH4 in the gas in a biological treatment tank) is shown.
In addition, the methane density | concentration in the gas in a biological treatment tank shown in each figure means volume%.
When the ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the mixture in the mixing tank (n-Hex / VS in the mixing tank) is 0.26 or less, the normality of the water contained in the biological treatment tank A tendency to keep the hexane extractant concentration (n-Hex in the biological treatment tank) low was observed, and at the same time, a tendency to maintain a high methane concentration in the biological treatment tank gas (CH4 in the biological treatment tank gas) was observed. .
This is because the ratio of the normal hexane extractable substance concentration to the loss on ignition of the total evaporation residue in the mixture in the mixing tank (n-Hex / VS in the mixing tank) becomes low, so that the methanogenic bacteria in the biological treatment tank It is assumed that the activity was increased, that is, methane fermentation was promoted.
In general, in the case of biological treatment, biological treatment is carried out while acclimatizing sludge containing living organisms by gradually increasing the amount of the substance to be biologically supplied supplied to the biological treatment tank without abruptly increasing it. .
However, in Test Example 1, the habituation was simplified than usual, and the test was performed under a condition in which the ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the mixture in the mixing tank was rapidly changed. .
Therefore, in the mixing tank mixture, under the conditions that the acclimatization is simplified than usual and the ratio of the normal hexane extractable substance concentration to the loss on ignition of the total evaporation residue in the mixing tank mixture is changed rapidly, the total evaporation in the mixing tank mixture The ratio of the normal hexane extract substance concentration to the loss on ignition of the residue is preferably 0.26 or less.
（試験例２）
試験例１では、通常よりも馴養を簡略化し、混合槽の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比を急激に変化させた条件下で試験を行ったが、試験例２では、生物を含む汚泥を通常条件で馴養させながら生物処理をした。
すなわち、試験例２では、生物を含む汚泥を通常条件で馴養させながら生物処理をしたこと以外は、試験例１と同じ装置を用い、同様な方法で試験を行った。
具体的には、混合槽の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比（混合槽内ｎ−Ｈｅｘ／ＶＳ）が０．１〜０．３３となるように、厨芥固形物とスカムとの質量混合比を変化させながら厨芥固形物とスカムとを混合槽に投入した。
また、試験例１とは異なり、混合槽の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比（混合槽内ｎ−Ｈｅｘ／ＶＳ）を０．２２〜０．２６の間で１ヶ月以上保持させて、汚泥を馴養させ、その後、混合槽の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比（混合槽内ｎ−Ｈｅｘ／ＶＳ）を０．２７以上にした。
(Test Example 2)
In Test Example 1, the acclimatization was simplified than usual, and the test was performed under a condition in which the ratio of the normal hexane extract substance concentration to the loss on ignition of the total evaporation residue in the mixture in the mixing tank was rapidly changed. In Test Example 2, biological treatment was performed while acclimatizing sludge containing organisms under normal conditions.
That is, in Test Example 2, a test was performed in the same manner using the same apparatus as Test Example 1 except that biological treatment was performed while acclimatizing sludge containing organisms under normal conditions.
Specifically, in the mixture in the mixing tank, the ratio of the normal hexane extractable substance concentration to the ignition loss of the entire evaporation residue (n-Hex / VS in the mixing tank) is 0.1 to 0.33. The solid matter and scum were charged into the mixing tank while changing the mass mixing ratio of the solid matter and scum.
Further, unlike Test Example 1, the ratio of the normal hexane extractable substance concentration to the loss on ignition of the total evaporation residue in the mixture in the mixing tank (n-Hex / VS in the mixing tank) was 0.22 to 0.26. The sludge is acclimatized for 1 month or more, and then the ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the mixture in the mixing tank (n-Hex / VS in the mixing tank) is 0. .27 or more.
（試験例２の結果）
図５には、混合槽の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比（混合槽内ｎ−Ｈｅｘ／ＶＳ）と、生物処理槽内の収容水のノルマルヘキサン抽出物質濃度（生物処理槽内ｎ−Ｈｅｘ）との関係を示す。
また、図６には、混合槽の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比（混合槽内ｎ−Ｈｅｘ／ＶＳ）と、生物処理槽内ガス中のメタン濃度（生物処理槽内ガス中ＣＨ４）との関係を示す。
なお、各図に示す、生物処理槽内ガス中のメタン濃度は、体積％を意味する。
試験例２では、生物処理槽内の収容水のノルマルヘキサン抽出物質濃度（生物処理槽内ｎ−Ｈｅｘ）を低く抑えられるとともに、同時に生物処理槽内ガス中のメタン濃度（生物処理槽内ガス中ＣＨ４）を高く維持できた。
したがって、混合槽の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比は、０．３２以下であることが好ましい。
(Result of Test Example 2)
FIG. 5 shows the ratio of the normal hexane extractable substance concentration to the loss on ignition of the total evaporation residue in the mixture in the mixing tank (n-Hex / VS in the mixing tank) and the normal hexane extraction of the water contained in the biological treatment tank. The relationship with substance concentration (n-Hex in a biological treatment tank) is shown.
FIG. 6 also shows the ratio of the normal hexane extractable substance concentration to the loss on ignition of the total evaporation residue in the mixture in the mixing tank (n-Hex / VS in the mixing tank) and the methane concentration in the gas in the biological treatment tank. The relationship with (CH4 in the gas in a biological treatment tank) is shown.
In addition, the methane density | concentration in the gas in a biological treatment tank shown in each figure means volume%.
In Test Example 2, the normal hexane extractable substance concentration (n-Hex in the biological treatment tank) of the water contained in the biological treatment tank can be kept low, and at the same time, the methane concentration in the biological treatment tank gas (in the biological treatment tank gas) CH4) could be kept high.
Therefore, the ratio of the normal hexane extractable substance concentration to the loss on ignition of the total evaporation residue in the mixture in the mixing tank is preferably 0.32 or less.
（試験例１、２のまとめ）
試験例１、２より、混合槽の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比は、好ましくは０．３２以下、より好ましくは０．２６以下である。
(Summary of Test Examples 1 and 2)
From Test Examples 1 and 2, the ratio of the normal hexane extractable substance concentration to the loss on ignition of the total evaporation residue in the mixture in the mixing tank is preferably 0.32 or less, more preferably 0.26 or less.
（試験例３）
第２有機性廃棄物たる厨芥ディスポーザ排水と第１有機性廃棄物たる厨房排水を生物処理槽で処理する設備において、厨芥ディスポーザ排水をスクリーンで固液分離した固形分（厨芥固形物）と、厨房排水を加圧浮上して分離したスカムとを混合槽で混合して混合物を得、メタン生成菌で生物処理する生物処理槽で前記混合物を処理した。結果を図７〜１２に示す。
(Test Example 3)
In a facility that treats the wastewater from the disposer, which is the second organic waste, and the kitchen wastewater, which is the first organic waste, in the biological treatment tank, The scum separated by raising the waste water by pressurization was mixed in a mixing tank to obtain a mixture, and the mixture was processed in a biological treatment tank for biological treatment with methanogens. The results are shown in FIGS.
図７には、生物処理槽内の収容水のノルマルヘキサン抽出物質濃度（生物処理槽内ｎ−Ｈｅｘ）、生物処理槽内の収容水の揮発性脂肪酸濃度（生物処理槽内ＶＦＡ）、生物処理槽内のガス中メタン濃度（生物処理槽内ガス中ＣＨ４）、生物処理槽の収容水のノルマルヘキサン抽出物質の除去率（ｎ−Ｈｅｘ除去率）、混合槽の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比（混合槽内ｎ−Ｈｅｘ／ＶＳ）、及び、生物処理槽内の収容水における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比（生物処理槽内ｎ−Ｈｅｘ／ＶＳ）の時間変化を示す。
なお、図７に示す各値は、１日ごとに測定した値である。
また、生物処理槽の収容水のノルマルヘキサン抽出物質の除去率（ｎ−Ｈｅｘ除去率）は、下記式で求めたものを意味する。
ｎ−Ｈｅｘ除去率 ＝ １ − （生物処理槽から取り出した収容水のノルマルヘキサン抽出物質濃度／混合槽から生物処理槽に投入される混合物のノルマルヘキサン抽出物質濃度）
図８には、混合槽への厨芥固形物の投入量、混合槽へのスカムの投入量、及び、混合槽の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比（混合槽内ｎ−Ｈｅｘ／ＶＳ）の時間変化を示す。
図９には、生物処理槽内の収容水のノルマルヘキサン抽出物質濃度（生物処理槽内ｎ−Ｈｅｘ）、生物処理槽内のガス中メタン濃度（生物処理槽内ガス中ＣＨ４）、生物処理槽の収容水のノルマルヘキサン抽出物質の除去率（ｎ−Ｈｅｘ除去率）の時間変化を示す。
なお、図８、９に示す各値は、１日ごとに測定した値を１週間ごとに算術平均した値である。
FIG. 7 shows the normal hexane extractable substance concentration in the biological treatment tank (n-Hex in the biological treatment tank), the volatile fatty acid concentration in the biological treatment tank (VFA in the biological treatment tank), and biological treatment. The concentration of methane in the gas in the tank (CH4 in the gas in the biological treatment tank), the removal rate of the normal hexane extract of the water contained in the biological treatment tank (n-Hex removal rate), the total evaporation residue in the mixture in the mixing tank Ratio of normal hexane extractable substance concentration to ignition loss (n-Hex / VS in mixing tank), and ratio of normal hexane extractant concentration to ignition loss of total evaporation residue in water contained in biological treatment tank ( The time change of n-Hex / VS in a biological treatment tank is shown.
Each value shown in FIG. 7 is a value measured every day.
Moreover, the removal rate (n-Hex removal rate) of the normal hexane extract substance of the accommodation water of a biological treatment tank means what was calculated | required by the following formula.
n-Hex removal rate = 1-(normal hexane extractable substance concentration of stored water taken out from the biological treatment tank / normal hexane extractable substance concentration of the mixture charged into the biological treatment tank from the mixing tank)
FIG. 8 shows the ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the mixing amount of the soot solid in the mixing vessel, the amount of scum in the mixing vessel, and the ignition loss in the mixture in the mixing vessel ( The time change of n-Hex / VS) in a mixing tank is shown.
FIG. 9 shows the normal hexane extractable substance concentration in the biological treatment tank (n-Hex in the biological treatment tank), the methane concentration in the gas in the biological treatment tank (CH4 in the gas in the biological treatment tank), the biological treatment tank The time change of the removal rate (n-Hex removal rate) of the normal hexane extract substance of the stored water is shown.
Each value shown in FIGS. 8 and 9 is a value obtained by arithmetically averaging the values measured every day for every week.
図１０〜１２は、図７に示すデータを用いて作成した図である。
図１０には、生物処理槽内の収容水における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比（生物処理槽内ｎ−Ｈｅｘ／ＶＳ）と、生物処理槽内のガス中メタン濃度（生物処理槽内ガス中ＣＨ４）との関係を示す。
図１１には、生物処理槽内の収容水のノルマルヘキサン抽出物質濃度（生物処理槽内ｎ−Ｈｅｘ）と、生物処理槽内のガス中メタン濃度（生物処理槽内ガス中ＣＨ４）との関係を示す。
図１２には、生物処理槽内のガス中メタン濃度（生物処理槽内ガス中ＣＨ４）と、生物処理槽内の収容水の揮発性脂肪酸濃度（生物処理槽内ＶＦＡ）との関係を示す。
10 to 12 are diagrams created using the data shown in FIG.
FIG. 10 shows the ratio of the normal hexane extractable substance concentration to the loss on ignition of the total evaporation residue in the stored water in the biological treatment tank (n-Hex / VS in the biological treatment tank) and the gas in the biological treatment tank. The relationship with methane concentration (CH4 in the gas in a biological treatment tank) is shown.
FIG. 11 shows the relationship between the normal hexane extractable substance concentration in the biological treatment tank (n-Hex in the biological treatment tank) and the methane concentration in the gas in the biological treatment tank (CH4 in the gas in the biological treatment tank). Indicates.
FIG. 12 shows the relationship between the methane concentration in the gas in the biological treatment tank (CH4 in the gas in the biological treatment tank) and the volatile fatty acid concentration in the biological treatment tank (VFA in the biological treatment tank).
図１０に示すように、生物処理槽内の収容水における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比（生物処理槽内ｎ−Ｈｅｘ／ＶＳ）が０．１５以下であると、生物処理槽内のガス中メタン濃度が高くなりやすい傾向が示された。
すなわち、生物処理槽内の収容水における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比が０．１５以下であると、メタン発酵が促進されやすくなると考えられる。
したがって、生物処理槽内の収容水における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比は、０．１５以下であることが好ましい。
As shown in FIG. 10, the ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the stored water in the biological treatment tank (n-Hex / VS in the biological treatment tank) is 0.15 or less. And the tendency that the methane concentration in the gas in the biological treatment tank tends to become high was shown.
That is, it is considered that methane fermentation is likely to be promoted when the ratio of the normal hexane extract substance concentration to the ignition loss of the total evaporation residue in the stored water in the biological treatment tank is 0.15 or less.
Therefore, the ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the stored water in the biological treatment tank is preferably 0.15 or less.
また、図１１に示すように、試験例２では、生物処理槽内の収容水のノルマルヘキサン抽出物質濃度（生物処理槽内ｎ−Ｈｅｘ）が２，２５０ｍｇ／Ｌ以下であると、生物処理槽内のガス中メタン濃度が高くなりやすい傾向が示された。
すなわち、生物処理槽内の収容水のノルマルヘキサン抽出物質濃度が２，２５０ｍｇ／Ｌ以下であると、メタン発酵が促進されやすくなると考えられる。
したがって、生物処理槽内の収容水のノルマルヘキサン抽出物質濃度は、２，２５０ｍｇ／Ｌ以下であることが好ましい。
Moreover, as shown in FIG. 11, in Test Example 2, when the normal hexane extract substance concentration (n-Hex in the biological treatment tank) of the contained water in the biological treatment tank is 2,250 mg / L or less, the biological treatment tank The methane concentration in the gas tends to be high.
That is, it is considered that methane fermentation is easily promoted when the concentration of the normal hexane extract in the biological treatment tank is 2250 mg / L or less.
Therefore, it is preferable that the normal hexane extractable substance density | concentration of the accommodation water in a biological treatment tank is 2,250 mg / L or less.
なお、図１２に示すように、試験例２では、生物処理槽内のガス中メタン濃度５５〜６５％の範囲を境にして、生物処理槽内の収容水の揮発性脂肪酸濃度が大きく変化した。
すなわち、生物処理槽内の収容水の揮発性脂肪酸濃度が低いと、生物処理槽内のガス中メタン濃度が高くなりやすい傾向にあると考えられる。そして、その結果、メタン発酵が促進されやすくなると考えられる。
As shown in FIG. 12, in Test Example 2, the volatile fatty acid concentration of the stored water in the biological treatment tank greatly changed at the boundary of the methane concentration in the gas in the biological treatment tank of 55 to 65%. .
That is, if the volatile fatty acid concentration of the stored water in the biological treatment tank is low, the methane concentration in the gas in the biological treatment tank tends to increase. As a result, methane fermentation is likely to be promoted.
Ａ：厨房排水、Ｂ：厨芥、Ｃ：浄化水、Ｄ：濃縮物、Ｅ：濃縮物、Ｆ：濃縮物、Ｆ’：濃縮物、Ｇ：濃縮物、
１：廃棄物処理装置、２：処理部、３：移送部、４：調整部、
２１：生物処理槽、２１ａ：撹拌部、２１ａ１：回転軸、２１ａ２：撹拌翼、２１ｂ：測定部、２２：固液分離部、２３ａ：収容水移送部、２３ａ１：収容水移送管、２３ａ２：ポンプ、２３ｂ：分離水移送部、２３ｃ：濃縮物移送部、２４：スクリーン、２５ａ：曝気部、２５ｂ：排出部、２６ａ：脱硫部、２６ｂ：ガス貯留部、２６ｃ：ガス利用設備、２６ｄ：槽、
３１：第１移送部、３１ａ：槽、３１ｂ：グリストラップ、３１ｃ：スクリーン、３１ｄ：槽、３１ｄ１：撹拌部、３１ｅ：加圧浮上部、３１ｆ：濃縮物移送管、３１ｇ：ポンプ、
３２：第２移送部、３２ａ：ディスポーザ部、３２ｂ：スクリーン、３２ｃ：ディスポーザ排水槽、３２ｄ：第１ディスポーザ排水移送管、３２ｅ：第２ディスポーザ排水移送管、３２ｆ：切り替え部、３２ｆ１：第３バルブ、３２ｆ２：第４バルブ、３２ｇ：濃縮物移送管、３２ｈ：ポンプ、
３３：第３移送部、３３ａ、混合物移送管、３３ｂ：ポンプ、
３４：第４移送部、３４ａ：分岐管、
３５：混合槽、３５ａ：撹拌部、
３６：制御部、３６ａ：第１バルブ、３６ｂ：第２バルブ、
４１：信号発信部、４２：制御信号伝達部、４２ａ：第１制御信号伝達部、４２ｂ：第２制御信号伝達部、４２ｃ：第３制御信号伝達部、４２ｄ：第４制御信号伝達部、４２ｅ：第５制御信号伝達部、４２ｆ：第６制御信号伝達部、４２ｇ：第７制御信号伝達部、４２ｈ：第８制御信号伝達部
A: Kitchen drainage, B: Coffee, C: Purified water, D: Concentrate, E: Concentrate, F: Concentrate, F ′: Concentrate, G: Concentrate,
1: waste treatment device, 2: treatment unit, 3: transfer unit, 4: adjustment unit,
21: biological treatment tank, 21a: stirring unit, 21a1: rotating shaft, 21a2: stirring blade, 21b: measurement unit, 22: solid-liquid separation unit, 23a: stored water transfer unit, 23a1: stored water transfer pipe, 23a2: pump 23b: separation water transfer section, 23c: concentrate transfer section, 24: screen, 25a: aeration section, 25b: discharge section, 26a: desulfurization section, 26b: gas storage section, 26c: gas utilization equipment, 26d: tank,
31: 1st transfer part, 31a: tank, 31b: grease trap, 31c: screen, 31d: tank, 31d1: stirring part, 31e: pressurized floating part, 31f: concentrate transfer pipe, 31g: pump,
32: Second transfer section, 32a: Disposer section, 32b: Screen, 32c: Disposer drain tank, 32d: First disposer drain transfer pipe, 32e: Second disposer drain transfer pipe, 32f: Switching section, 32f1: Third valve , 32f2: fourth valve, 32g: concentrate transfer pipe, 32h: pump,
33: 3rd transfer part, 33a, mixture transfer pipe, 33b: pump,
34: 4th transfer part, 34a: Branch pipe,
35: mixing tank, 35a: stirring unit,
36: control unit, 36a: first valve, 36b: second valve,
41: signal transmitter, 42: control signal transmitter, 42a: first control signal transmitter, 42b: second control signal transmitter, 42c: third control signal transmitter, 42d: fourth control signal transmitter, 42e : Fifth control signal transmission unit, 42f: sixth control signal transmission unit, 42g: seventh control signal transmission unit, 42h: eighth control signal transmission unit
Claims (11)
前記第１有機性廃棄物及び前記第２有機性廃棄物を前記生物処理槽に移送する移送部と、
下記（１）及び（２）の少なくとも何れか一方を満たすように前記生物処理槽内の収容水を調整する調整部とを備えており、
前記移送部は、前記第１有機性廃棄物及び前記第２有機性廃棄物を混合することにより混合物を得る混合槽と、前記第１有機性廃棄物を前記混合槽に移送する第１移送部と、前記第２有機性廃棄物を前記混合槽に移送する第２移送部と、前記混合物を前記生物処理槽に移送する第３移送部と、前記混合槽を介さずに前記生物処理槽に前記第２有機性廃棄物を移送する第４移送部とを有し、
前記混合槽が、前記生物処理槽と別体となっており、
前記生物処理槽は、前記メタン生成菌を含む汚泥で前記生物処理をする生物処理槽であり、
前記調整部が、前記汚泥を馴養させる馴養工程を実施する調整部である、廃棄物処理装置。
（１）前記生物処理槽内の収容水のノルマルヘキサン抽出物質濃度が２，２５０ｍｇ／Ｌ以下となる。
（２）前記生物処理槽内の収容水における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比が０．１５以下となる。 A first organic waste containing oil, and a treatment unit having a biological treatment tank for biologically treating a second organic waste having a lower oil concentration than the first organic waste with a methanogen;
A transfer unit for transferring the first organic waste and the second organic waste to the biological treatment tank;
An adjustment unit that adjusts the stored water in the biological treatment tank so as to satisfy at least one of the following (1) and (2):
The transfer unit includes a mixing tank that obtains a mixture by mixing the first organic waste and the second organic waste, and a first transfer unit that transfers the first organic waste to the mixing tank. A second transfer unit that transfers the second organic waste to the mixing tank, a third transfer unit that transfers the mixture to the biological treatment tank, and the biological treatment tank without passing through the mixing tank. A fourth transfer unit for transferring the second organic waste ,
The mixing tank is separate from the biological treatment tank,
The biological treatment tank is a biological treatment tank that performs the biological treatment with sludge containing the methanogen.
The waste treatment apparatus, wherein the adjustment unit is an adjustment unit that performs a habituation process for acclimating the sludge.
(1) The normal hexane extract substance concentration of the water contained in the biological treatment tank is 2,250 mg / L or less.
(2) The ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the stored water in the biological treatment tank is 0.15 or less.
前記第１有機性廃棄物及び前記第２有機性廃棄物を前記生物処理槽に移送する移送部とを備えており、
前記移送部は、前記第１有機性廃棄物及び前記第２有機性廃棄物を混合することにより混合物を得る混合槽と、前記第１有機性廃棄物を前記混合槽に移送する第１移送部と、前記第２有機性廃棄物を前記混合槽に移送する第２移送部と、前記混合物を前記生物処理槽に移送する第３移送部と、前記混合槽を介さずに前記生物処理槽に前記第２有機性廃棄物を移送する第４移送部とを有し、
前記混合槽内の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比が０．３２以下となるように前記混合槽内の混合物を調整する調整部をさらに備え、
前記混合槽が、前記生物処理槽と別体となっており、
前記生物処理槽は、前記メタン生成菌を含む汚泥で前記生物処理をする生物処理槽であり、
前記調整部が、前記汚泥を馴養させる馴養工程を実施する調整部である、廃棄物処理装置。 A first organic waste containing oil, and a treatment unit having a biological treatment tank for biologically treating a second organic waste having a lower oil concentration than the first organic waste with a methanogen;
A transfer unit for transferring the first organic waste and the second organic waste to the biological treatment tank,
The transfer unit includes a mixing tank that obtains a mixture by mixing the first organic waste and the second organic waste, and a first transfer unit that transfers the first organic waste to the mixing tank. A second transfer unit that transfers the second organic waste to the mixing tank, a third transfer unit that transfers the mixture to the biological treatment tank, and the biological treatment tank without passing through the mixing tank. A fourth transfer unit for transferring the second organic waste ,
An adjusting unit for adjusting the mixture in the mixing tank so that the ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the mixture in the mixing tank is 0.32 or less;
The mixing tank is separate from the biological treatment tank,
The biological treatment tank is a biological treatment tank that performs the biological treatment with sludge containing the methanogen.
The waste treatment apparatus, wherein the adjustment unit is an adjustment unit that performs a habituation process for acclimating the sludge.
前記調整部は、前記測定部で測定した生物処理槽内の収容水のｐＨ及び前記収容水から発生するガスのメタン濃度の少なくとも一方の値に基づいて、前記調整をする調整部である、請求項１〜６の何れか１項に記載の廃棄物処理装置。 The processing unit further includes a measuring unit that measures at least one of the pH of the stored water in the biological treatment tank and the methane concentration of the gas generated from the stored water,
The adjustment unit is an adjustment unit that performs the adjustment based on at least one of the pH of the stored water in the biological treatment tank measured by the measurement unit and the methane concentration of the gas generated from the stored water. Item 7. The waste treatment apparatus according to any one of Items 1 to 6.
前記調整部は、前記調整槽を用いることにより、前記生物処理槽に移送する前記第１有機性廃棄物の流量を調整する調整部である、請求項１〜８の何れか１項に記載の廃棄物処理装置。 The transfer unit is separated from the first organic waste by a pressurized flotation method, and has a lower oil concentration than the first organic waste and a higher oil concentration than the first organic waste. A pressure floating part for obtaining a concentrate, and a regulating tank for storing the concentrate,
The said adjustment part is an adjustment part which adjusts the flow volume of the said 1st organic waste transferred to the said biological treatment tank by using the said adjustment tank, The any one of Claims 1-8. Waste treatment equipment.
前記第１有機性廃棄物及び前記第２有機性廃棄物を前記生物処理槽に移送する移送工程とを備えており、
下記（１）及び（２）の少なくとも何れか一方を満たすように前記生物処理槽内の収容水を調整し、
前記移送工程は、前記第１有機性廃棄物を混合槽に移送する第１移送工程と、前記第２有機性廃棄物を前記混合槽に移送する第２移送工程と、前記第１有機性廃棄物及び前記第２有機性廃棄物を前記混合槽で混合することにより混合物を得る混合工程と、該混合物を前記生物処理槽に移送する第３移送工程と、前記混合槽を介さずに前記生物処理槽に前記第２有機性廃棄物を移送する第４移送工程とを有し、
前記混合槽が、前記生物処理槽と別体となっており、
前記生物処理槽は、前記メタン生成菌を含む汚泥で前記生物処理をする生物処理槽であり、
前記調整では、前記汚泥を馴養させる馴養工程を実施する、廃棄物処理方法。
（１）前記生物処理槽内の収容水のノルマルヘキサン抽出物質濃度が２，２５０ｍｇ／Ｌ以下となる。
（２）前記生物処理槽内の収容水における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比が０．１５以下となる。 The process which has the biological treatment process which carries out the biological treatment of the 1st organic waste containing an oil content, and the 2nd organic waste whose oil content concentration is lower than this 1st organic waste by a methanogen in a biological treatment tank Process,
A transfer step of transferring the first organic waste and the second organic waste to the biological treatment tank,
Adjusting the stored water in the biological treatment tank so as to satisfy at least one of the following (1) and (2),
The transfer step includes a first transfer step for transferring the first organic waste to the mixing tank, a second transfer step for transferring the second organic waste to the mixing tank, and the first organic waste. A mixing step in which the mixture and the second organic waste are mixed in the mixing tank, a third transfer step in which the mixture is transferred to the biological treatment tank, and the organism without passing through the mixing tank. A fourth transfer step of transferring the second organic waste to the treatment tank ,
The mixing tank is separate from the biological treatment tank,
The biological treatment tank is a biological treatment tank that performs the biological treatment with sludge containing the methanogen.
In the adjustment, the waste treatment method is carried out by performing a habituation process for acclimating the sludge.
(1) The normal hexane extract substance concentration of the water contained in the biological treatment tank is 2,250 mg / L or less.
(2) The ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the stored water in the biological treatment tank is 0.15 or less.
前記第１有機性廃棄物及び前記第２有機性廃棄物を前記生物処理槽に移送する移送工程とを備えており、
前記移送工程は、前記第１有機性廃棄物を混合槽に移送する第１移送工程と、前記第２有機性廃棄物を前記混合槽に移送する第２移送工程と、前記第１有機性廃棄物及び前記第２有機性廃棄物を前記混合槽で混合することにより混合物を得る混合工程と、該混合物を前記生物処理槽に移送する第３移送工程と、前記混合槽を介さずに前記生物処理槽に前記第２有機性廃棄物を移送する第４移送工程とを有し、
前記混合槽内の混合物における、全蒸発残留物の強熱減量に対するノルマルヘキサン抽出物質濃度の比が０．３２以下となるように前記混合槽内の混合物を調整し、
前記混合槽が、前記生物処理槽と別体となっており、
前記生物処理槽は、前記メタン生成菌を含む汚泥で前記生物処理をする生物処理槽であり、
前記調整では、前記汚泥を馴養させる馴養工程を実施する、廃棄物処理方法。 The process which has the biological treatment process which carries out the biological treatment of the 1st organic waste containing an oil content, and the 2nd organic waste whose oil content concentration is lower than this 1st organic waste by a methanogen in a biological treatment tank Process,
A transfer step of transferring the first organic waste and the second organic waste to the biological treatment tank,
The transfer step includes a first transfer step for transferring the first organic waste to the mixing tank, a second transfer step for transferring the second organic waste to the mixing tank, and the first organic waste. A mixing step in which the mixture and the second organic waste are mixed in the mixing tank, a third transfer step in which the mixture is transferred to the biological treatment tank, and the organism without passing through the mixing tank. A fourth transfer step of transferring the second organic waste to the treatment tank ,
Adjusting the mixture in the mixing tank so that the ratio of the normal hexane extractable substance concentration to the ignition loss of the total evaporation residue in the mixture in the mixing tank is 0.32 or less;
The mixing tank is separate from the biological treatment tank,
The biological treatment tank is a biological treatment tank that performs the biological treatment with sludge containing the methanogen.
In the adjustment, the waste treatment method is carried out by performing a habituation process for acclimating the sludge.
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