JP4365617B2 - Organic waste liquid processing method and processing apparatus - Google Patents

Description

【００７０】
【表２】

【００７１】
表１から、機械的な分散処理と化学的な改質処理とを併用した場合のＶＳＳ濃度低下の効果は、併用する機械的処理および化学的処理の組合せによって多少異なる。しかし、いずれの処理を組み合わせた場合でも、機械的処理単独または化学的処理単独の場合よりＶＳＳ濃度の低下率が大きくなるのはもちろんのこと、これら単独処理におけるＶＳＳ濃度の低下率の和とくらべても、よりＶＳＳ濃度の低下率は大きくなる。したがって、機械的な方法による分散処理後、化学的な方法で改質処理を行なう併用処理は、超音波処理後オゾン処理を行なう併用処理に限らず、汚泥の溶解性向上に対してきわめて有効であることがわかった。
【００７２】
さらに、表２から、機械的な分散処理と化学的な改質処理とを併用した場合のリン溶出の効果は、併用する機械的処理および化学的処理の組合せによって多少異なる。しかし、いずれの処理を組み合わせた場合でも、機械的処理単独または化学的処理単独の場合よりリン溶出濃度が大きくなるのはもちろんのこと、これら単独処理におけるＶＳＳ濃度の低下率の和とくらべても、よりリン溶出濃度は大きくなる。したがって、機械的な方法による分散処理後、化学的な方法で改質処理を行なう併用処理は、超音波処理後オゾン処理を行なう併用処理に限らず、リンの溶出に対してもきわめて有効であることがわかった。
【００７３】
実施の形態１
つぎに、本発明による有機性廃液の処理装置およびそれを用いた有機性廃液の処理方法について説明する。
【００７４】
図１３は、本発明の一実施の形態における有機性廃液の処理装置について、その概略の構成および処理の流れを示した図である。
【００７５】
図１３に示すように、嫌気性消化槽１と有機性廃液導入路２のあいだに、超音波破砕処理槽９、オゾン処理槽１１および固液分離槽１７が設けられている。超音波破砕処理槽９内には超音波破砕器３０が設置されており、オゾン処理槽１１には、オゾンガス注入路３２を介してオゾン発生器３１が接続されている。超音波破砕処理槽９とオゾン処理槽１１は分散廃液排出路１０によって、オゾン処理槽１１と固液分離槽１７は処理液排出路１８によって、固液分離槽１７と嫌気性消化槽１は濃縮液導入路１９によって、それぞれ接続されている。また、有機性廃液導入路２には有機性廃液導入ポンプ３７が設置されている。
【００７６】
また、固液分離槽１７とリン回収槽２４が、分離液排出路２０によって接続されており、リン回収槽２４はリン回収後液導入路２６を介して嫌気性消化槽１に接続されている。分離液排出路２０には凝集剤導入路２３が接続され、凝集剤導入路２３の他端は凝集剤保持槽２１へと接続されている。さらに、凝集剤導入路２３には凝集剤導入ポンプ２２が設置されている。また、リン回収槽２４にはリン回収路２５が接続されている。
【００７７】
さらに、嫌気性消化槽１は消化汚泥排出路３を介して固液分離槽４に接続され、固液分離槽４には濃縮汚泥排出路５および処理水排出路８が接続されている。濃縮汚泥排出路５は汚泥廃棄路６と汚泥返送路７に分岐し、汚泥返送路７は嫌気性消化槽１に接続されている。また、嫌気性消化槽１には消化ガス排出路３６が接続されている。
【００７８】
つぎに本実施の形態の処理装置の動作について説明する。
【００７９】
有機性廃液導入ポンプ３７を動作させ、下水処理場の初沈汚泥と余剰汚泥を混合した有機汚泥を、有機性廃液として有機性廃液導入路２から超音波破砕処理槽９に導入する。導入した有機汚泥を、超音波破砕処理槽９にて超音波破砕機３０によって処理し、汚泥中の固形物質を分散させる。分散処理後の有機汚泥を分散廃液排出路１０を介してオゾン処理槽１１に送り、オゾン発生器３１で発生させたオゾンガスをオゾンガス注入路３２を通してオゾン処理槽１１に注入して、有機汚泥のオゾン処理を行なう。すなわち、分散処理後の有機汚泥にオゾンによる改質処理を加える。
【００８０】
このオゾン処理した有機汚泥を、処理液排出路１８を通して固液分離槽１７へと送り、固液分離槽１７で固形物と溶液に分ける。固形物を濃縮液導入路１９から嫌気性消化槽１に導入し、処理した有機汚泥を微生物によって分解する。一方、リンを多く含む溶液を分離液排出路２０を通してリン回収槽２４に送る。この際、凝集剤導入ポンプ２２を動作させ、凝集剤保持槽２１に保持した炭酸カルシウム溶液を、凝集剤導入路２３を通して分離液排出路２０へと供給し、分離液排出路２０を通るリン含有処理水に、炭酸カルシウム溶液を導入する。リン回収槽２４では析出したリン酸カルシウムを分離し、リン回収路２５から引き抜くとともに、リンを含まない溶液をリン回収後液導入路２６を通して嫌気性消化槽１に導入する。
【００８１】
嫌気性消化槽１内で微生物によって有機汚泥を消化した後、嫌気性消化槽１内の汚泥を消化汚泥排出路３から排出し、固液分離槽４で固形物と溶液に分け、溶液を処理水排出路８から、固形物を濃縮汚泥排出路５からそれぞれ排出する。また、濃縮汚泥排出路５中の固形物を汚泥返送路７を介して嫌気性消化槽１に返送するとともに、一部は汚泥廃棄路６から系外に排出する。また、嫌気性消化槽１で発生する消化ガスを、消化ガス排出路３６によって排出する。
【００８２】
有機汚泥にオゾンを反応させると、オゾンの強い酸化作用によって有機汚泥の固形物中の繊維質や細胞壁などの難溶解性物質を改質し、消化槽内の汚泥によって溶解されやすい易溶解性物質へと変換することができる。また、オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理のみを行なう場合にくらべ、注入したオゾンと固形物との接触効率が大幅に高くなり、効率的に難溶解性物質の溶解性を向上することができる。このように、超音波処理とオゾン処理との併用によって難溶解性物質を改質した有機汚泥を嫌気性消化槽に導入して微生物処理を行なうと、超音波処理単独やオゾン処理単独の場合、およびこれらの処理の単純な和とくらべ、汚泥の溶解量およびメタンへの変換量を大幅に増大することができる。また、これに対応して、処分すべき汚泥の発生量も大幅に低減できる。
【００８３】
同時に、オゾンの強い酸化作用によって細胞壁の分解が進むため、有機汚泥の固形物中に含有されるリンを固形物外の溶液中へ高い効率で溶出させることができる。オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理のみを行なう場合にくらべ、注入したオゾンによる細胞壁の分解がより進み、より効率的にリンの溶出量を増大することができる。さらに、この処理後の汚泥を固液分離することで、溶液中のリンを凝集剤を用いて固形状のリンにすることができ、再利用可能なリンとして回収することができる。
【００８４】
したがって、嫌気性消化槽へ導入する有機汚泥を超音波処理で分散させた後にオゾン処理で改質することによって、エネルギー、リン同時回収型のより効率的な有機汚泥の処理が可能となる。
【００８５】
なお、本実施の形態では、嫌気性消化槽へ導入する有機汚泥の全てを超音波処理およびオゾン処理したが、導入する有機汚泥の一部に超音波処理およびオゾン処理を行ない、残りは処理を行なわずに嫌気性消化槽へ導入するようにしてもよい。
【００８６】
実施の形態２
本発明のほかの実施の形態における有機性廃液の処理装置およびそれを用いた有機性廃液の処理方法について説明する。
【００８７】
図１４は、本実施の形態の有機性廃液の処理装置について、その構成の概略と処理の流れを示した図であり、嫌気性消化を酸生成槽とメタン生成槽の２つの槽で行なう場合に本発明を適用した例を示している。
【００８８】
図１４に示すように、酸生成槽３３と有機性廃液導入路２のあいだに、超音波破砕処理槽９、オゾン処理槽１１および固液分離槽１７が設けられている。超音波破砕処理槽９内には超音波破砕器３０が設置されており、オゾン処理槽１１にはオゾンガス注入路３２を介してオゾン発生器３１が接続されている。超音波破砕処理槽９とオゾン処理槽１１は分散廃液排出路１０によって、オゾン処理槽１１と固液分離槽１７は処理液排出路１８によって、固液分離槽１７と酸生成槽３３は濃縮液導入路１９によって、それぞれ接続されている。また、有機性廃液導入路２には有機性廃液導入ポンプ３７が設置されている。
【００８９】
また、固液分離槽１７とリン回収槽２４が、分離液排出路２０によって接続されており、リン回収槽２４はリン回収後液導入路２６を介して酸生成槽３３に接続されている。分離液排出路２０には凝集剤導入路２３が接続され、凝集剤導入路２３の他端は凝集剤保持槽２１へと接続されている。さらに、凝集剤導入路２３には凝集剤導入ポンプ２２が設置されている。また、リン回収槽２４にはリン回収路２５が接続されている。
【００９０】
さらに、酸生成槽３３の後段には、消化汚泥排出路３を介して固液分離槽４が設けられ、固液分離槽４には濃縮汚泥排出路５および処理水排出路８が接続されている。濃縮汚泥排出路５は汚泥廃棄路６と汚泥返送路７に分岐し、汚泥返送路７は酸生成槽３３に接続されている。また、処理水排出路８はメタン生成槽１３に接続されている。
【００９１】
メタン生成槽１３の後段には、消化汚泥排出路１４を介し固液分離槽１５が設けられ、固液分離槽１５には濃縮汚泥排出路２７および処理水排出路１６が接続されている。濃縮汚泥排出路２７は汚泥廃棄路３４と汚泥返送路３５に分岐し、汚泥返送路３５はメタン生成槽１３に接続されている。また、メタン生成槽１３には消化ガス排出路３６が接続されている。
【００９２】
つぎに本実施の形態の処理装置の動作について説明する。
【００９３】
有機性廃液導入ポンプ３７を動作させ、下水処理場の初沈汚泥と余剰汚泥を混合した有機汚泥を、有機性廃液として有機性廃液導入路２から超音波破砕処理槽９に導入する。導入した有機汚泥を、超音波破砕処理槽９にて超音波破砕機３０によって処理し、汚泥中の固形物質を分散させる。分散処理後の有機汚泥を分散廃液排出路１０を介してオゾン処理槽１１に送り、オゾン発生器３１で発生させたオゾンガスをオゾンガス注入路３２を通してオゾン処理槽１１に注入して、有機汚泥のオゾン処理を行なう。すなわち、分散処理後の有機汚泥にオゾンによる改質処理を加える。
【００９４】
このオゾン処理した有機汚泥を、処理液排出路１８を通して固液分離槽１７へと送り、固液分離槽１７で固形物と溶液に分ける。固形物を濃縮液導入路１９から酸生成槽３３に導入し、処理した有機汚泥を微生物によって溶解する。一方、リンを多く含む溶液を、分離液排出路２０を通してリン回収槽２４に送る。この際、凝集剤導入ポンプ２２を動作させ、凝集剤保持槽２１に保持した炭酸カルシウム溶液を、凝集剤導入路２３を通して分離液排出路２０へと供給し、分離液排出路２０を通るリン含有処理水に、炭酸カルシウム溶液を導入する。リン回収槽２４では析出したリン酸カルシウムを分離し、リン回収路２５から引き抜くとともに、リンを含まない溶液をリン回収後液導入路２６を通して酸生成槽３３に導入する。
【００９５】
酸生成槽３３で微生物によって有機汚泥を溶解した後、酸生成槽３３内の汚泥を消化汚泥排出路３から排出し、固液分離槽４で固形物と溶液に分け、溶液を処理水排出路８を介してメタン生成槽１３へ導入し、固形物を濃縮汚泥排出路５から排出する。また、濃縮汚泥排出路５中の固形物を汚泥返送路７を介して酸生成槽３３に返送するとともに、一部を汚泥廃棄路６から系外に排出する。
【００９６】
メタン生成槽１３で微生物によって溶液中の有機物をメタンに変換した後、メタン生成槽１３内の汚泥を消化汚泥排出路１４から排出し、固液分離槽１５で固形物と溶液に分ける。溶液を処理水排出路１６から、固形物を濃縮汚泥排出路２７からそれぞれ排出する。また、濃縮汚泥排出路２７中の固形物を汚泥返送路３５を介してメタン生成槽１３に返送するとともに、一部を汚泥廃棄路３４から系外に排出する。また、メタン生成槽１３で発生する消化ガスを、消化ガス排出路３６によって排出する。
【００９７】
このように、有機汚泥にオゾンを反応させると、オゾンの強い酸化作用によって有機汚泥の固形物中の繊維質や細胞壁などの難溶解性物質を改質し、酸生成内の汚泥によって溶解されやすい易溶解性物質へと変換することができる。また、オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理単独の場合にくらべ、注入したオゾンと固形物との接触効率が大幅に高くなり、効率的に難溶解性物質の溶解性を向上することができる。このように、超音波処理とオゾン処理との併用によって難溶解性物質を改質した有機汚泥を酸生成槽に導入して微生物処理を行なうと、超音波処理単独やオゾン処理単独の場合、およびこれらの処理の単純な和とくらべ、酸生成槽での有機汚泥の溶解量およびメタン生成槽でのメタンへの変換量を大幅に増大することができる。また、これに対応して、処分すべき汚泥の発生量も大幅に低減できる。
【００９８】
同時に、オゾンの強い酸化作用によって細胞壁の分解が進むため、有機汚泥の固形物中に含有されるリンを固形物外の溶液中へ高い効率で溶出させることができる。オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理のみを行なう場合にくらべ、注入したオゾンによる細胞壁の分解がより進み、より効率的にリンの溶出量を増大することができる。さらに、この処理後の汚泥を固液分離することで、溶液中のリンを凝集剤を用いて固形状のリンにすることができ、再利用可能なリンとして回収することができる。
【００９９】
したがって、酸生成槽へ導入する有機汚泥を超音波処理で分散させた後にオゾン処理で改質することによって、エネルギー、リン同時回収型のより効率的な有機汚泥の処理が可能となる。
【０１００】
また、本実施の形態のように、嫌気性消化を前段の酸生成槽と後段のメタン生成槽とに分けて行なう場合において、酸生成槽に導入する有機汚泥に対して分散および改質の処理を行なって溶解性を向上させることで、後段のメタン生成槽として従来の流動床式や固定床式のメタン生成槽だけでなく、高負荷嫌気性処理に用いられるＵＡＳＢ（上向流嫌気性汚泥ブランケット）型のメタン生成槽を用いることができ、高速なメタン生成が可能になる。
【０１０１】
なお、本実施の形態では、酸生成槽へ導入する有機汚泥の全てを超音波処理およびオゾン処理したが、導入する有機汚泥の一部に超音波処理およびオゾン処理を行ない、残りは処理を行なわずに酸生成槽へ導入するようにしてもよい。
【０１０２】
実施の形態３
本発明のほかの実施の形態における有機性廃液の処理装置およびそれを用いた有機性廃液の処理方法について説明する。
【０１０３】
図１５は本実施の形態の有機性廃液の処理装置について、その構成の概略と処理の流れを示した図である。
【０１０４】
図１５に示すように、嫌気性消化槽１には有機性廃液導入路２が接続されている。嫌気性消化槽１には消化汚泥引抜き路４７が接続され、消化汚泥引抜き路４７のもう一端は超音波破砕処理槽９およびオゾン処理槽１１に接続されている。超音波破砕処理槽９内には超音波破砕器３０が設置されており、オゾン処理槽１１には、オゾンガス注入路３２を介してオゾン発生器３１が接続されている。超音波破砕処理槽９とオゾン処理槽１１は分散廃液排出路１０によって、オゾン処理槽１１と固液分離槽１７は処理液排出路１８によって、固液分離槽１７と嫌気性消化槽１は濃縮液導入路１９によって、それぞれ接続されている。また、有機性廃液導入路２には有機性廃液導入ポンプ３７が、消化汚泥引抜き路４７には消化汚泥引抜きポンプ３８が設置されている。
【０１０５】
また、固液分離槽１７とリン回収槽２４が、分離液排出路２０によって接続されており、リン回収槽２４はリン回収後液導入路２６を介して嫌気性消化槽１に接続されている。分離液排出路２０には凝集剤導入路２３が接続され、凝集剤導入路２３の他端は凝集剤保持槽２１へと接続されている。さらに、凝集剤導入路２３には凝集剤導入ポンプ２２が設置されている。また、リン回収槽２４にはリン回収路２５が接続されている。
【０１０６】
また、嫌気性消化槽１には消化汚泥排出路３を介して固液分離槽４が接続され、固液分離槽４には濃縮汚泥排出路５および処理水排出路８が接続されている。濃縮汚泥排出路５は汚泥廃棄路６と汚泥返送路７に分岐し、汚泥返送路７は嫌気性消化槽１に接続されている。また、嫌気性消化槽１には消化ガス排出路３６が接続されている。
【０１０７】
つぎに本実施の形態の処理装置の動作について説明する。
【０１０８】
有機性廃液導入ポンプ３７を動作させ、下水処理場の初沈汚泥と余剰汚泥を混合した有機汚泥を、有機性廃液として有機性廃液導入路２から嫌気性消化槽１に導入する。嫌気性消化槽１で微生物によって有機汚泥を消化した後、嫌気性消化槽１内の汚泥を消化汚泥排出路３から排出し、固液分離槽４で固形物と溶液に分け、溶液を処理水排出路８から、固形物を濃縮汚泥排出路５からそれぞれ排出する。また、濃縮汚泥排出路５中の固形物を汚泥返送路７を介して嫌気性消化槽１に返送するとともに、一部を汚泥廃棄路６から系外に排出する。また、嫌気性消化槽１で発生する消化ガスを消化ガス排出路３６によって排出する。
【０１０９】
この嫌気性消化の過程において、消化汚泥引抜きポンプ３８を動作させ、嫌気性消化槽１の消化汚泥を消化汚泥引抜き路４７を通して超音波破砕処理槽９に導入する。導入した消化汚泥を超音波破砕機３０によって処理し、消化汚泥中の固形物を分散させる。分散処理後の消化汚泥を分散廃液排出路１０を介してオゾン処理槽１１に送り、オゾン発生器３１で発生させたオゾンガスをオゾンガス注入路３２を通してオゾン処理槽１１に注入し、消化汚泥のオゾン処理を行なう。すなわち、分散処理後の消化汚泥にオゾンによる改質処理を加える。
【０１１０】
このオゾン処理後の消化汚泥を、処理液排出路１８を通して固液分離槽１７に送り、固液分離槽１７で固形物と溶液に分ける。固形物を濃縮液導入路１９から嫌気性消化槽１に導入し、オゾン処理した消化汚泥を微生物によって分解する。一方、リンを多く含む溶液を、分離液排出路２０を通してリン回収槽２４に送る。この際、凝集剤導入ポンプ２２を動作させ、凝集剤保持槽２１に保持した炭酸カルシウム溶液を凝集剤導入路２３を介して分離液排出路２０に導入し、分離液排出路２０を通るリン含有処理水に炭酸カルシウム溶液を混合させる。リン回収槽２４では、析出したリン酸カルシウムを分離しリン回収路２５から引き抜くとともに、リンを含まない溶液をリン回収後液導入路２６を通して嫌気性消化槽１に導入する。
【０１１１】
このように、消化汚泥にオゾンを反応させると、オゾンの強い酸化作用によって消化汚泥の固形物中の繊維質や細胞壁などの難溶解性物質を改質し、消化槽内の汚泥によって溶解されやすい易溶解性物質へと変換することができる。また、オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理単独の場合にくらべ、注入したオゾンと固形物との接触効率が大幅に高くなり、効率的に難溶解性物質の溶解性を向上することができる。このように超音波処理とオゾン処理とを併用して難溶解性物質を改質した消化汚泥を嫌気性消化槽に導入して生物処理すると、超音波処理単独やオゾン処理単独の場合、およびこれらの処理の単純な和とくらべ、汚泥の溶解量およびメタンへの変換量を大幅に増大することができる。また、これに対応して、処分すべき汚泥の発生量も大幅に低減できる。
【０１１２】
同時に、オゾンの強い酸化作用によって細胞壁の分解が進むため、消化汚泥の固形物中に含有されるリンを固形物外の溶液中へ高い効率で溶出させることができる。オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理のみを行なう場合にくらべ、注入したオゾンによる細胞壁の分解がより進み、より効率的にリンの溶出量を増大することができる。さらに、この処理後の汚泥を固液分離することで、溶液中のリンを凝集剤を用いて固形状のリンにすることができ、再利用可能なリンとして回収することができる。
【０１１３】
したがって、嫌気性消化槽の消化汚泥中を超音波処理で分散させた後にオゾン処理で改質することによって、エネルギー、リン同時回収型のより効率的な消化汚泥の処理が可能となる。
【０１１４】
また、嫌気性消化槽の消化汚泥中には、生物によって溶解し難い難溶解性物質が多く蓄積している。したがって、本実施の形態のように、嫌気性消化槽から消化汚泥の一部を引き抜き、引き抜いた消化汚泥中の固形物を処理して易溶解性物質へ変換することによって、よりいっそう効果的にエネルギー、リン回収を進めることが可能となる。
【０１１５】
実施の形態４
本発明のまた別の実施の形態における有機性廃液の処理装置およびそれを用いた有機性廃液の処理方法について説明する。
【０１１６】
図１６は、本実施の形態の有機性廃液の処理装置について、その構成の概略と処理の流れを示した図であり、嫌気性消化を酸生成槽とメタン生成槽の２つの槽で行なう場合に本発明を適用した例を示している。
【０１１７】
図１６に示すように、酸生成槽３３に有機性廃液導入路２が接続されている。酸生成槽３３には消化汚泥引抜き路４７が接続され、消化汚泥引抜き路４７の後段には超音波破砕処理槽９およびオゾン処理槽１１が設けられている。超音波破砕処理槽９内には超音波破砕器３０が設置されており、オゾン処理槽１１には、オゾンガス注入路３２を介してオゾン発生器３１が接続されている。超音波破砕処理槽９とオゾン処理槽１１は分散廃液排出路１０によって、オゾン処理槽１１と固液分離槽１７は処理液排出路１８によって、固液分離槽１７と酸生成槽３３は濃縮液導入路１９によって、それぞれ接続されている。また、有機性廃液導入路２には有機性廃液導入ポンプ３７が、消化汚泥引抜き路４７には消化汚泥引抜きポンプ３８が設置されている。
【０１１８】
また、固液分離槽１７とリン回収槽２４が、分離液排出路２０によって接続されており、リン回収槽２４はリン回収後液導入路２６を介して酸生成槽３３に接続されている。分離液排出路２０には凝集剤導入路２３が接続され、凝集剤導入路２３の他端は凝集剤保持槽２１へと接続されている。さらに、凝集剤導入路２３には凝集剤導入ポンプ２２が設置されている。また、リン回収槽２４にはリン回収路２５が接続されている。
【０１１９】
さらに、酸生成槽３３の後段には消化汚泥排出路３を介して固液分離槽４が設けられ、固液分離槽４には濃縮汚泥排出路５および処理水排出路８が接続している。濃縮汚泥排出路５は汚泥廃棄路６と汚泥返送路７に分岐し、汚泥返送路７は酸生成槽３３に接続されている。一方、処理水排出路８はメタン生成槽１３に接続されている。
【０１２０】
メタン生成槽１３の後段には、消化汚泥排出路１４を介し固液分離槽１５が設けられ、固液分離槽１５には濃縮汚泥排出路２７および処理水排出路１６が接続されている。濃縮汚泥排出路２７は汚泥廃棄路３４と汚泥返送路３５に分岐し、汚泥返送路３５はメタン生成槽１３に接続されている。また、メタン生成槽１３には消化ガス排出路３６が接続されている。
【０１２１】
つぎに本実施の形態の処理装置の動作について説明する。
【０１２２】
有機性廃液導入ポンプ３７を動作させ、下水処理場の初沈汚泥と余剰汚泥を混合した有機汚泥を、有機性廃液として有機性廃液導入路２から酸生成槽３３に導入する。酸生成槽３３で微生物によって有機汚泥を溶解した後、酸生成槽３３内の汚泥を消化汚泥排出路３から排出し、固液分離槽４で固形物と溶液に分け、溶液は処理水排出路８を介してメタン生成槽１３へ導入し、固形物を濃縮汚泥排出路５から排出する。濃縮汚泥排出路５中の固形物を汚泥返送路７を介して酸生成槽３３に返送するとともに、一部を汚泥廃棄路６から系外に排出する。
【０１２３】
メタン生成槽１３で微生物によって溶液中の有機物をメタンに変換した後、メタン生成槽１３内の汚泥を消化汚泥排出路１４から排出し、固液分離槽１５で固形物と溶液に分ける。溶液は処理水排出路１６から、固形物は濃縮汚泥排出路２７からそれぞれ排出する。また、濃縮汚泥排出路２７中の固形物を汚泥返送路３５を介してメタン生成槽１３に返送するとともに、一部を汚泥廃棄路３４から系外に排出する。また、メタン生成槽１３で発生する消化ガスを、消化ガス排出路３６によって排出する。
【０１２４】
この嫌気性消化の過程において、消化汚泥引抜きポンプ３８を動作させ、酸生成槽３３の消化汚泥を消化汚泥引抜き路４７を通して超音波破砕処理槽９に導入し、超音波破砕機３０によって処理して消化汚泥中の固形物を分散させる。分散処理後の消化汚泥を分散廃液排出路１０を介してオゾン処理槽１１に導入し、同時にオゾン発生器３１で発生させたオゾンガスをオゾンガス注入路３２を通してオゾン処理槽１１に注入し、消化汚泥のオゾン処理を行なう。すなわち、分散処理後の消化汚泥にオゾンによる改質処理を加える。
【０１２５】
このオゾン処理後の消化汚泥を、処理液排出路１８を通して固液分離槽１７に送り、固液分離槽１７で固形物と溶液に分ける。固形物を濃縮液導入路１９から酸生成槽３３に導入し、オゾン処理した消化汚泥を微生物によって溶解する。一方、リンを多く含む溶液を、分離液排出路２０を通してリン回収槽２４に送る。この際、凝集剤導入ポンプ２２を動作させ、凝集剤保持槽２１に保持した炭酸カルシウム溶液を凝集剤導入路２３を介して分離液排出路２０に導入し、分離液排出路２０を通るリン含有処理水に炭酸カルシウム溶液を混合させる。リン回収槽２４では、析出したリン酸カルシウムを分離しリン回収路２５から引き抜くとともに、リンを含まない溶液をリン回収後液導入路２６を通して酸生成槽３３に導入する。
【０１２６】
このように、酸生成槽の消化汚泥にオゾンを反応させると、オゾンの強い酸化作用によって消化汚泥の固形物中の繊維質や細胞壁などの難溶解性物質を改質し、酸生成槽内の汚泥によって溶解されやすい易溶解性物質へと変換することができる。また、オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理単独の場合にくらべ、注入したオゾンと固形物との接触効率が大幅に高くなり、効率的に難溶解性物質の溶解性を向上することができる。このように、超音波処理とオゾン処理とを併用して難溶解性物質を改質した消化汚泥を酸生成槽に導入して生物処理することにより、超音波処理単独やオゾン処理単独の場合、およびこれらの処理の単純な和とくらべ、酸生成槽での汚泥の溶解量およびメタン生成槽でのメタンへの変換量を大幅に増大することができる。
【０１２７】
同時に、オゾンの強い酸化作用によって細胞壁の分解が進むため、消化汚泥の固形物中に含有されるリンを固形物外の溶液中へ高い効率で溶出させることができる。オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理のみを行なう場合にくらべ、注入したオゾンによる細胞壁の分解がより進み、より効率的にリンの溶出量を増大することができる。さらに、この処理後の汚泥を固液分離することで、溶液中のリンを凝集剤を用いて固形状のリンにすることができ、再利用可能なリンとして回収することができる。
【０１２８】
したがって、酸生成槽の消化汚泥を超音波処理で分散させた後にオゾン処理で改質することによって、エネルギー、リン同時回収型のより効率的な有機汚泥の処理が可能となる。
【０１２９】
また、酸生成槽の消化汚泥中には、生物によって溶解し難い難溶解性物質が多く蓄積している。したがって、本実施の形態のように、酸生成槽から消化汚泥の一部を引き抜き、引き抜いた消化汚泥中の固形物質を処理して易溶解性物質へ変換することによって、より効果的にエネルギー、リン回収を進めることが可能となる。
【０１３０】
また、本実施の形態のように、嫌気性消化を前段の酸生成槽と後段のメタン生成槽とに分けて行なう場合において、酸生成槽の消化汚泥に超音波処理で分散させた後にオゾン処理で改質して溶解性を向上させることで、後段のメタン生成槽として従来の流動床式や固定床式のメタン生成槽だけでなく、高負荷嫌気性処理に用いられるＵＡＳＢ（上向流嫌気性汚泥ブランケット）型のメタン生成槽を用いることができ、高速なメタン生成が可能になる。
【０１３１】
実施の形態５
本発明のほかの実施の形態における有機性廃液の処理装置およびそれを用いた有機性廃液の処理について説明する。
【０１３２】
図１７は本実施の形態の有機性廃液の処理装置について、構成の概略と処理の流れを示した図である。
【０１３３】
図１７に示すように、嫌気性消化槽１に有機性廃液導入路２が接続されている。嫌気性消化槽１には消化汚泥排出路３を介して固液分離槽４が接続され、固液分離槽４には濃縮汚泥排出路５および処理水排出路８が接続されている。濃縮汚泥排出路５は汚泥廃棄路６と汚泥返送路７に分岐し、汚泥返送路７の後段には、超音波破砕処理槽９およびオゾン処理槽１１が設けられている。超音波破砕処理槽９内には超音波破砕器３０が設置されており、オゾン処理槽１１にはオゾンガス注入路３２を介してオゾン発生器３１が接続されている。超音波破砕処理槽９とオゾン処理槽１１は分散廃液排出路１０によって、オゾン処理槽１１と固液分離槽１７は処理液排出路１８によって、固液分離槽１７と嫌気性消化槽１は濃縮液導入路１９によって、それぞれ接続されている。また、嫌気性消化槽１には消化ガス排出路３６が接続されている。また、有機性廃液導入路２には有機性廃液導入ポンプ３７が、汚泥返送路７には汚泥返送ポンプ４６が設置されている。
【０１３４】
また、固液分離槽１７とリン回収槽２４が、分離液排出路２０によって接続されており、リン回収槽２４はリン回収後液導入路２６を介して嫌気性消化槽１に接続されている。分離液排出路２０には凝集剤導入路２３が接続され、凝集剤導入路２３の他端は凝集剤保持槽２１へと接続されている。さらに、凝集剤導入路２３には凝集剤導入ポンプ２２が設置されている。また、リン回収槽２４にはリン回収路２５が接続されている。
【０１３５】
つぎに本実施の形態の処理装置の動作について説明する。
【０１３６】
有機性廃液導入ポンプ３７を動作させ、下水処理場の初沈汚泥と余剰汚泥を混合した有機汚泥を、有機性廃液として有機性廃液導入路２から嫌気性消化槽１に導入する。嫌気性消化槽１で微生物によって有機汚泥を消化した後、嫌気性消化槽１内の汚泥を消化汚泥排出路３から排出し、固液分離槽４で固形物と溶液に分ける。溶液は処理水排出路８から、固形物は濃縮汚泥排出路５からそれぞれ排出する。また、嫌気性消化槽１で発生する消化ガスは、消化ガス排出路３６によって排出する。
【０１３７】
この嫌気性消化の過程において、濃縮汚泥排出路５中の濃縮汚泥の一部を汚泥廃棄路６から系外に排出するとともに、汚泥返送ポンプ４６を動作させ濃縮汚泥排出路５中の濃縮汚泥の一部を汚泥返送路７を介して超音波破砕処理槽９に導入し、超音波破砕機３０によって処理して濃縮汚泥中の固形物を分散させる。分散処理後の濃縮汚泥を分散廃液排出路１０を介してオゾン処理槽１１に送り、オゾン発生器３１で発生させたオゾンガスをオゾンガス注入路３２を通してオゾン処理槽１１に注入し、濃縮汚泥のオゾン処理を行なう。すなわち、分散処理後の濃縮汚泥にオゾンによる改質処理を加える。
【０１３８】
このオゾン処理後の濃縮汚泥を、オゾン処理液排出路１８を通して固液分離槽１７に送り、固液分離槽１７で固形物と溶液に分ける。固形物を処理廃液導入路１９から嫌気性消化槽１に導入し、オゾン処理した濃縮汚泥を微生物によって分解する。一方、リンを多く含む溶液を、リン含有処理水排出路２０を通ってリン回収槽２４に送る。この際、凝集剤導入ポンプ２２を動作させ、リン含有処理水排出路２０を通るリン含有処理水に凝集剤保持槽２１に保持した炭酸カルシウム溶液を供給し、混合させる。リン回収槽２４で析出したリン酸カルシウムを分離し、リン回収路２５から引き抜くとともに、リンを含まない溶液をリン回収後処理水導入路２６を通して嫌気性消化槽１に導入する。
【０１３９】
このように嫌気性消化槽の消化汚泥を濃縮した濃縮汚泥に対しオゾン処理を行なうことで、オゾンの強い酸化作用によって有機汚泥の固形物中の繊維質や細胞壁などの難溶解性物質を改質し、消化槽内の汚泥によって溶解されやすい易溶解性物質へと変換することができる。また、オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理単独の場合にくらべ、注入したオゾンと固形物との接触効率が大幅に高くなり、効率的に難溶解性物質の溶解性を向上することができる。このように、超音波処理とオゾン処理とを併用して難溶解性物質を改質した濃縮汚泥を嫌気性消化槽に導入して生物処理することにより、超音波処理単独やオゾン処理単独の場合、およびこれらの処理の単純な和とくらべ、汚泥の溶解量およびメタンへの変換量を大幅に増大することができる。
【０１４０】
同時に、オゾンの強い酸化作用によって細胞壁の分解が進むため、濃縮汚泥の固形物中に含有されるリンを固形物外の溶液中へ高い効率で溶出させることができる。オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理のみを行なう場合にくらべ、注入したオゾンによる細胞壁の分解がより進み、より効率的にリンの溶出量を増大することができる。さらに、この処理後の汚泥を固液分離することで、溶液中のリンを凝集剤を用いて固形状のリンにすることができ、再利用可能なリンとして回収することができる。
【０１４１】
したがって、嫌気性消化槽の消化汚泥を濃縮した濃縮汚泥を超音波処理で分散させた後にオゾン処理で改質することによって、エネルギー、リン同時回収型のより効率的な濃縮汚泥の処理が可能となる。
【０１４２】
また、嫌気性消化槽の消化汚泥中には生物によって溶解し難い難溶解性物質が多く蓄積している。したがって、本実施の形態のように、嫌気性消化槽内の汚泥を濃縮し、濃縮した消化汚泥中の固形物を処理して易溶解性物質へ変換することによって、より効果的にエネルギー、リン回収を進めることが可能となる。
【０１４３】
なお、本実施の形態では、嫌気性消化槽へと返送する消化汚泥の全てを超音波処理およびオゾン処理したが、返送する消化汚泥の一部に超音波処理およびオゾン処理を行ない、残りの部分については処理を行なわずに嫌気性消化槽へと返送するようにしてもよい。
【０１４４】
実施の形態６
本発明のまた別の実施の形態における有機性廃液の処理装置およびそれを用いた有機性廃液の処理方法について説明する。
【０１４５】
図１８は、本実施の形態の有機性廃液の処理装置について、その構成の概略と処理の流れを示した図であり、嫌気性消化を酸生成槽とメタン生成槽の２つの槽で行なう場合に本発明を適用した例を示している。
【０１４６】
図１８に示すように、酸生成槽３３に有機性廃液導入路２が接続されている。酸生成槽３３の後段には消化汚泥排出路３を介して固液分離槽４が設けられ、固液分離槽４には濃縮汚泥排出路５および処理水排出路８が接続されている。濃縮汚泥排出路５は汚泥廃棄路６と汚泥返送路７に分岐し、汚泥返送路７の後段には、超音波破砕処理槽９およびオゾン処理槽１１が設けられている。超音波破砕処理槽９内には超音波破砕器３０が設置されており、オゾン処理槽１１にはオゾンガス注入路３２を介してオゾン発生器３１が接続されている。超音波破砕処理槽９とオゾン処理槽１１は分散廃液排出路１０によって、オゾン処理槽１１と固液分離槽１７は処理液排出路１８によって、固液分離槽１７と酸生成槽３３は濃縮液導入路１９によって、それぞれ接続されている。一方、処理水排出路８はメタン生成槽１３に接続されている。また、有機性廃液導入路２には有機性廃液導入ポンプ３７が、汚泥返送路７には汚泥返送ポンプ４６が設置されている。
【０１４７】
また、固液分離槽１７とリン回収槽２４が、分離液排出路２０によって接続されており、リン回収槽２４はリン回収後液導入路２６を介して酸生成槽３３に接続されている。分離液排出路２０には凝集剤導入路２３が接続され、凝集剤導入路２３の他端は凝集剤保持槽２１へと接続されている。さらに、凝集剤導入路２３には凝集剤導入ポンプ２２が設置されている。また、リン回収槽２４にはリン回収路２５が接続されている。
【０１４８】
メタン生成槽１３の後段には消化汚泥排出路１４を介し固液分離槽１５が設けられており、固液分離槽１５には濃縮汚泥排出路２７および処理水排出路１６が接続されている。濃縮汚泥排出路２７は汚泥廃棄路３４と汚泥返送路３５に分岐し、汚泥返送路３５はメタン生成槽１３に接続されている。また、メタン生成槽１３には消化ガス排出路３６が接続されている。
【０１４９】
つぎに本実施の形態の処理装置の動作について説明する。
【０１５０】
有機性廃液導入ポンプ３７を動作させ、下水処理場の初沈汚泥と余剰汚泥を混合した有機汚泥を、有機性廃液として有機性廃液導入路２から酸生成槽３３に導入する。酸生成槽３３で微生物によって有機汚泥を溶解した後、酸生成槽３３内の汚泥を消化汚泥排出路３から排出し、固液分離槽４で固形物と溶液に分ける。溶液は処理水排出路８を通ってメタン生成槽１３へ導入し、固形物は濃縮汚泥排出路５から排出する。
【０１５１】
メタン生成槽１３にて微生物によって溶液をメタンに変換した後、メタン生成槽１３内の汚泥を消化汚泥排出路１４から排出し、固液分離槽１５で固形物と溶液に分ける。溶液を処理水排出路１６から、固形物を濃縮汚泥排出路２７からそれぞれ排出する。また、濃縮汚泥排出路２７中の固形物を汚泥返送路３５を介してメタン生成槽１３に返送するとともに、一部を汚泥廃棄路３４から系外に排出する。また、メタン生成槽１３で発生する消化ガスは、消化ガス排出路３６によって排出する。
【０１５２】
この嫌気性消化の過程において、濃縮汚泥排出路５中の濃縮汚泥の一部を汚泥廃棄路６から系外に排出するとともに、汚泥返送ポンプ４６を動作させ濃縮汚泥排出路５中の濃縮汚泥の一部を汚泥返送路７を介して超音波破砕処理槽９に導入し、超音波破砕機３０によって処理して濃縮汚泥中の固形物を分散させる。分散処理後の濃縮汚泥を分散廃液排出路１０を介してオゾン処理槽１１に送り、、同時にオゾン発生器３１で発生させたオゾンガスをオゾンガス注入路３２を通してオゾン処理槽１１に注入し、濃縮汚泥のオゾン処理を行なう。すなわち、分散処理後の濃縮汚泥にオゾンによる改質処理を加える。
【０１５３】
このオゾン処理後の濃縮汚泥を、オゾン処理液排出路１８を通して固液分離槽１７に送り、固液分離槽１７で固形物と溶液に分ける。固形物を処理廃液導入路１９から酸生成槽３３に導入し、オゾン処理した濃縮汚泥を微生物によって分解する。一方、リンを多く含む溶液を、リン含有処理水排出路２０を通ってリン回収槽２４に送られる。この際、凝集剤導入ポンプ２２を動作させ、リン含有処理水排出路２０を通るリン含有処理水に凝集剤保持槽２１に保持した炭酸カルシウム溶液を供給し、混合させる。リン回収槽２４で析出したリン酸カルシウムを分離し、リン回収路２５から引き抜くとともに、リンを含まない溶液をリン回収後処理水導入路２６を通して酸生成槽３３に導入する。
【０１５４】
このように、濃縮した消化汚泥にオゾンを反応させると、オゾンの強い酸化作用によって濃縮汚泥の固形物中の繊維質や細胞壁などの難溶解性物質を改質し、酸生成槽内の汚泥によって溶解されやすい易溶解性物質へと変換することができる。また、オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理単独の場合にくらべ、注入したオゾンと固形物との接触効率が大幅に高くなり、効率的に難溶解性物質の溶解性を向上することができる。このように、超音波処理とオゾン処理とを併用して難溶解性物質を改質した消化汚泥を酸生成槽に導入して生物処理することにより、超音波処理単独やオゾン処理単独の場合、およびこれらの処理の単純な和とくらべ、酸生成槽での汚泥の溶解量およびメタン生成槽でのメタンへの変換量を大幅に増大することができる。
【０１５５】
同時に、オゾンの強い酸化作用によって細胞壁の分解が進むため、濃縮汚泥の固形物中に含有されるリンを固形物外の溶液中へ高い効率で溶出させることができる。オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理のみを行なう場合にくらべ、注入したオゾンによる細胞壁の分解がより進み、より効率的にリンの溶出量を増大することができる。さらに、この処理後の汚泥を固液分離することで、溶液中のリンを凝集剤を用いて固形状のリンにすることができ、再利用可能なリンとして回収することができる。
【０１５６】
したがって、酸生成槽の消化汚泥を濃縮した濃縮汚泥を超音波処理で分散させた後にオゾン処理で改質することによって、エネルギー、リン同時回収型のより効率的な濃縮汚泥の処理が可能となる。
【０１５７】
また、本実施の形態のように、嫌気性消化を前段の酸生成槽と後段のメタン生成槽とに分けて行なう場合において、濃縮した酸生成槽の濃縮汚泥にオゾン処理を行なって溶解性を促進することで、後段のメタン生成槽として従来の流動床式や固定床式のメタン生成槽だけでなく、高負荷嫌気性処理に用いられるＵＡＳＢ（上向流嫌気性汚泥ブランケット）型のメタン生成槽を用いることができ、高速なメタン生成が可能になる。
【０１５８】
また、酸生成を行なう槽の消化汚泥中には、生物によって溶解し難い難溶解性物質が多く蓄積している。したがって、本実施の形態のように、濃縮した消化汚泥中の固形物を処理して易溶解性物質へ変換することによって、より効果的にエネルギー、リン回収を進めることが可能となる。
【０１５９】
なお、本実施の形態では、酸生成槽へと返送する濃縮汚泥を全て超音波処理およびオゾン処理したが、返送する消化汚泥の一部に超音波処理およびオゾン処理を行ない、残りの部分については処理を行なわずに酸生成槽に返送してもよい。
【０１６０】
実施の形態７
本発明のまた別の実施の形態における有機性廃液の処理装置およびそれを用いた有機性廃液の処理方法について説明する。
【０１６１】
図１９は、本実施の形態の有機性廃液の処理装置について、その構成の概略と処理の流れを示した図である。
【０１６２】
図１９に示す本実施の形態の処理装置は、図１３に示した実施の形態１の処理装置において、嫌気性消化槽１に消化汚泥引抜き路４７が接続され、この消化汚泥引抜き路４７は超音波破砕槽９に接続されている。また、消化汚泥引抜き路４７には消化汚泥引抜きポンプ３８が設置されている。本実施の形態の処理装置は、消化汚泥引抜き路４７、消化汚泥引抜きポンプ３８を備える点を除き、図１３に示した実施の形態１の処理装置と同様の構成である。
【０１６３】
つぎに本実施の形態の処理装置の動作について説明する。
【０１６４】
実施の形態１と同様、有機性廃液として下水処理場の有機汚泥を導入し、超音波破砕処理槽９にて超音波処理を行なうが、このとき本実施の形態においては、嫌気性消化槽１内の消化汚泥を消化汚泥引抜き路４７を通して超音波破砕槽９に導入する。すなわち、流入する有機汚泥と嫌気性消化槽１の消化汚泥とを混合し、混合汚泥に対し超音波破砕処理槽９で超音波破砕処理を行ない、その後オゾン処理槽１１にてオゾン処理を行なう。その後の動作は実施の形態１と同様である。
【０１６５】
このように、有機汚泥と消化汚泥との混合汚泥にオゾンを反応させると、オゾンの強い酸化作用によって混合汚泥の固形物中の繊維質や細胞壁などの難溶解性物質を改質し、消化槽内の汚泥によって溶解されやすい易溶解性物質へと変換することができる。また、オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理単独の場合とくらべ、注入したオゾンと固形物との接触効率が大幅に高くなり、効率的に難溶解性物質の溶解性を向上することができる。このように、超音波処理とオゾン処理とを併用して難溶解性物質を改質した混合汚泥を嫌気性消化槽に導入して生物処理すると、超音波処理単独やオゾン処理単独の場合、およびこれらの処理の単純な和とくらべ、汚泥の溶解量およびメタンへの変換量を大幅に増大することができる。
【０１６６】
同時に、オゾンの強い酸化作用によって細胞壁の分解が進むため、混合汚泥の固形物中に含有されるリンを固形物外の溶液中へ高い効率で溶出させることができる。オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理のみを行なう場合にくらべ、注入したオゾンによる細胞壁の分解がより進み、より効率的にリンの溶出量を増大することができる。さらに、この処理後の汚泥を固液分離することで、溶液中のリンを凝集剤を用いて固形状のリンにすることができ、再利用可能なリンとして回収することができる。したがって、エネルギー、リン同時回収型の混合汚泥の処理が可能となる。
【０１６７】
また、流入する有機性廃液の固形物中に難溶解性物質が多く含まれるような場合には、本実施の形態のように、難溶解性物質を多く含んだ有機性廃液と難溶解性物質が多く蓄積されている消化汚泥を混合し、これら難溶解性物質を多く含んだ混合汚泥中の固形物質を超音波処理で分散させオゾン処理で改質することにより、効果的に難溶解性物質の溶解性増大を促進することができ、流入する有機性廃液にのみ処理を加える場合や嫌気性消化槽の消化汚泥にのみ処理を加える場合にくらべ、有機性廃液からのエネルギー、リン回収量をより大幅に増大できるとともに、処分すべき汚泥量をより大幅に低減することができる。
【０１６８】
実施の形態８
本発明のさらに別の実施の形態における有機性廃液の処理装置およびそれを用いた有機性廃液の処理方法について説明する。
【０１６９】
図２０は、本実施の形態の有機性廃液の処理装置について、その構成の概略と処理の流れを示した図である。
【０１７０】
図２０に示す本実施の形態の処理装置は、図１４に示した実施の形態２の処理装置において、酸生成槽３３に消化汚泥引抜き路４７が接続され、この消化汚泥引抜き路４７は超音波破砕処理槽９に接続されている。また、消化汚泥引抜き路４７には消化汚泥引抜きポンプ３８が設置されている。本実施の形態の処理装置は、消化汚泥引抜き路４７、消化汚泥引抜きポンプ３８を備える点を除き、図１４に示した実施の形態２の処理装置と同様の構成である。
【０１７１】
つぎに本実施の形態の処理装置の動作について説明する。
【０１７２】
実施の形態２と同様、有機性廃液として下水処理場の有機汚泥を導入し、超音波破砕処理槽９にて超音波処理を行なうが、このとき本実施の形態においては、酸生成槽３３内の消化汚泥を消化汚泥引抜き路４７を通して超音波破砕槽９に導入する。すなわち、流入する有機汚泥と酸生成槽３３の消化汚泥とを混合し、混合汚泥に対し超音波破砕処理槽９で超音波破砕処理を行ない、その後オゾン処理槽１１にてオゾン処理を行なう。その後の動作は実施の形態２と同様である。
【０１７３】
このように、有機汚泥と酸生成槽の汚泥との混合汚泥にオゾンを反応させると、オゾンの強い酸化作用によって混合汚泥の固形物中の繊維質や細胞壁などの難溶解性物質を改質し、酸生成槽内の汚泥によって溶解されやすい易溶解性物質へと変換することができる。また、オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理単独の場合とくらべ、注入したオゾンと固形物との接触効率が大幅に高くなり、効率的に難溶解性物質の溶解性を向上することができる。このように、超音波処理とオゾン処理とを併用して難溶解性物質を改質した混合汚泥を酸生成槽に導入して生物処理すると、超音波処理単独やオゾン処理単独の場合、およびこれらの処理の単純な和とくらべ、酸生成槽での汚泥の溶解量およびメタン生成槽でのメタンへの変換量を大幅に増大することができる。
【０１７４】
同時に、オゾンの強い酸化作用によって細胞壁の分解が進むため、混合汚泥の固形物中に含有されるリンを固形物外の溶液中へ高い効率で溶出させることができる。オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理のみを行なう場合にくらべ、注入したオゾンによる細胞壁の分解がより進み、より効率的にリンの溶出量を増大することができる。さらに、この処理後の汚泥を固液分離することで、溶液中のリンを凝集剤を用いて固形状のリンにすることができ、再利用可能なリンとして回収することができる。したがって、エネルギー、リン同時回収型の混合汚泥の処理が可能となる。
【０１７５】
また、本実施の形態のように、嫌気性消化を前段の酸生成槽と後段のメタン生成槽とに分けて行なう場合において、酸生成槽に導入する有機汚泥や酸生成槽の消化汚泥のオゾン処理を行なって溶解性を促進することで、後段のメタン生成槽として従来の流動床式や固定床式のメタン生成槽だけでなく、高負荷嫌気性処理に用いられるＵＡＳＢ（上向流嫌気性汚泥ブランケット）型のメタン生成槽を用いることができ、高速なメタン生成が可能になる。
【０１７６】
また、流入する有機性廃液の固形物中に難溶解性物質が多く含まれるような場合には、本実施の形態のように、難溶解性物質を多く含んだ有機性廃液と難溶解性物質が多く蓄積されている酸生成槽の消化汚泥を混合し、これら難溶解性物質を多く含んだ混合汚泥中の固形物質を超音波処理で分散させオゾン処理で改質することにより、効果的に難溶解性物質の溶解性増大を促進することができ、流入する有機性廃液にのみ処理を加える場合や酸生成槽の消化汚泥にのみ処理を加える場合にくらべ、有機性廃液からのエネルギー回収量をより大幅に増大できるとともに、処分すべき汚泥量をより大幅に低減することができる。
【０１７７】
実施の形態９
本発明の別の実施の形態における有機性廃液の処理装置およびそれを用いた有機性廃液の処理方法について説明する。
【０１７８】
図２１は、本実施の形態の有機性廃液の処理装置について、その構成の概略と処理の流れを示した図である。
【０１７９】
図２１に示す本実施の形態の処理装置は、図１３に示した実施の形態１の処理装置において、汚泥返送路７が超音波破砕槽９に接続されている。また、汚泥返送路７には汚泥返送ポンプ４６が設置されている。本実施の形態の処理装置は、汚泥返送路７がオゾン処理槽１１に接続され、汚泥返送ポンプ４６が設置されている点を除き、図１３に示した実施の形態１の処理装置と同様の構成である。
【０１８０】
つぎに本実施の形態の処理装置の動作について説明する。
【０１８１】
実施の形態１と同様、有機性廃液として下水処理場の有機汚泥を導入し、超音波破砕槽９にて超音波処理を行なうが、このとき本実施の形態においては、固液分離槽４で濃縮した濃縮汚泥を汚泥返送路７を通して超音波破砕槽９に導入する。すなわち、流入する有機汚泥と固液分離後の濃縮汚泥とを混合し、混合汚泥に対し超音波破砕処理槽９で超音波破砕処理を行ない、その後オゾン処理槽１１にてオゾン処理を行なう。その後の動作は、前記実施の形態１と同様である。
【０１８２】
このように、有機汚泥と濃縮汚泥との混合汚泥にオゾンを反応させると、オゾンの強い酸化作用によって混合汚泥の固形物中の繊維質や細胞壁などの難溶解性物質を改質し、消化槽内の汚泥によって溶解されやすい易溶解性物質へと変換することができる。また、オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理単独の場合にくらべ、注入したオゾンと固形物との接触効率が大幅に高くなり、効率的に難溶解性物質の溶解性を向上することができる。このように、超音波処理とオゾン処理とを併用して難溶解性物質を改質した有機汚泥を嫌気性消化槽に導入して生物処理すると、超音波処理単独やオゾン処理単独の場合、およびこれらの処理の単純な和とくらべ、汚泥の溶解量およびメタンへの変換量を大幅に増大することができる。
【０１８３】
同時に、オゾンの強い酸化作用によって細胞壁の分解が進むため、混合汚泥の固形物中に含有されるリンを固形物外の溶液中へ高い効率で溶出させることができる。オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理のみを行なう場合にくらべ、注入したオゾンによる細胞壁の分解がより進み、より効率的にリンの溶出量を増大することができる。さらに、この処理後の汚泥を固液分離することで、溶液中のリンを凝集剤を用いて固形状のリンにすることができ、再利用可能なリンとして回収することができる。したがって、エネルギー、リン同時回収型の有機汚泥の処理が可能となる。
【０１８４】
また、流入する有機性廃液の固形物中に難溶解性物質が多く含まれるような場合には、本実施の形態のように、難溶解性物質を多く含んだ有機性廃液と難溶解性物質が多く蓄積されている消化汚泥を濃縮した汚泥を混合し、これら難溶解性物質を多く含んだ混合汚泥中の固形物質を超音波処理で分散させオゾン処理で改質することにより、効果的に難溶解性物質の溶解性増大を促進することができ、流入する有機性廃液にのみ処理を加える場合や嫌気性消化槽からの濃縮汚泥にのみ処理を加える場合にくらべ、有機性廃液からのエネルギー回収量をより大幅に増大できるとともに、処分すべき汚泥量をより大幅に低減することができる。
【０１８５】
実施の形態１０
本発明のまた別の実施の形態における有機性廃液の処理装置およびそれを用いた有機性廃液の処理方法について説明する。
【０１８６】
図２２は、本実施の形態の有機性廃液の処理装置について、その構成の概略と処理の流れを示した図である。
【０１８７】
図２２に示す本実施の形態の処理装置は、図１４に示した実施の形態２の処理装置において、汚泥返送路７が超音波破砕槽９に接続されている。また、汚泥返送路７には汚泥返送ポンプ４６が設置されている。本実施の形態の処理装置は、汚泥返送路７が超音波破砕槽９に接続され、汚泥返送ポンプ４６が設置されている点を除き、図１４に示した実施の形態２の処理装置と同様の構成である。
【０１８８】
つぎに本実施の形態の処理装置の動作について説明する。
【０１８９】
前記実施の形態２と同様、有機性廃液として下水処理場の有機汚泥を導入し、、超音波破砕槽９にて超音波処理を行なうが、このとき本実施の形態においては、酸生成槽３３の後段の固液分離槽４で濃縮した濃縮汚泥を、汚泥返送路７を通して超音波破砕槽９に導入する。すなわち、流入する有機汚泥と固液分離後の濃縮汚泥とを混合し、混合汚泥に対し超音波破砕処理槽９で超音波破砕処理を行ない、その後オゾン処理槽１１にてオゾン処理を行なう。その後の動作は、前記実施の形態２と同様である。
【０１９０】
このように、有機汚泥と濃縮した酸生成槽汚泥との混合汚泥にオゾンを反応させると、オゾンの強い酸化作用によって混合汚泥の固形物中の繊維質や細胞壁などの難溶解性物質を改質し、酸生成槽内の汚泥によって溶解されやすい易溶解性物質へと変換することができる。また、オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理単独の場合にくらべ、注入したオゾンと固形物との接触効率が大幅に高くなり、効率的に難溶解性物質の溶解性を向上することができる。このように、超音波処理とオゾン処理とを併用して難溶解性物質を改質した混合汚泥を酸生成槽に導入して生物処理すると、超音波処理単独やオゾン処理単独の場合、およびこれらの処理の単純な和とくらべ、酸生成槽での汚泥の溶解量およびメタン生成槽でのメタンへの変換量を大幅に増大することができる。
【０１９１】
同時に、オゾンの強い酸化作用によって細胞壁の分解が進むため、混合汚泥の固形物中に含有されるリンを固形物外の溶液中へ高い効率で溶出させることができる。オゾン処理前に超音波破砕による分散処理を行なうことにより、オゾン処理のみを行なう場合にくらべ、注入したオゾンによる細胞壁の分解がより進み、より効率的にリンの溶出量を増大することができる。さらに、この処理後の汚泥を固液分離することで、溶液中のリンを凝集剤を用いて固形状のリンにすることができ、再利用可能なリンとして回収することができる。したがって、エネルギー、リン同時回収型の有機汚泥の処理が可能となる。
【０１９２】
また、本実施の形態のように、嫌気性消化を前段の酸生成槽と後段のメタン生成槽とに分けて行なう場合において、酸生成槽の汚泥に分散および改質の処理を行ない溶解性を促進することで、後段のメタン生成槽として従来の流動床式や固定床式のメタン生成槽だけでなく、高負荷嫌気性処理に用いられるＵＡＳＢ（上向流嫌気性汚泥ブランケット）型のメタン生成槽を用いることができ、高速なメタン生成が可能になる。
【０１９３】
また、流入する有機性廃液の固形物中に難溶解性物質が多く含まれるような場合には、本実施の形態のように、難溶解性物質を多く含んだ有機性廃液と難溶解性物質が多く蓄積されている酸生成槽の消化汚泥を混合し、これら難溶解性物質を多く含んだ混合汚泥中の固形物質を超音波処理で分散させオゾン処理で改質することにより、難溶解性物質の溶解性増大を促進することができ、流入する有機性廃液にのみ処理を加える場合や酸生成槽からの濃縮汚泥にのみ処理を加える場合にくらべ、有機性廃液からのエネルギー回収量をより大幅に増大できるとともに、処分すべき汚泥量をより大幅に低減することができる。
【０１９４】
実施の形態１１
本発明のまた別の実施の形態における有機性廃液の処理装置およびそれを用いた有機性廃液の処理方法について説明する。
【０１９５】
図２３は、本実施の形態の有機性廃液の処理装置について、その構成の概略と処理の流れを示した図である。
【０１９６】
図２３に示す本実施の形態の処理装置は、図１５に示した実施の形態３の処理装置において、嫌気性消化槽１にはＯＲＰ計４９が設置され、信号線５１を介してコントローラ５２に接続されている。コントローラ５２は、超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８に、それぞれ信号線２８、信号線５３、信号線３９を介して接続されている。本実施の形態の処理装置は、ＯＲＰ計とコントローラおよび信号線を除き、図１５に示した前記実施の形態３の処理装置と同様の構成である。
【０１９７】
つぎに本実施の形態の処理装置の動作について説明する。
【０１９８】
実施の形態３と同様に、有機性廃液を嫌気性消化槽１に導入して微生物による消化を行なうとともに、嫌気性消化槽１から消化汚泥を引き抜き、超音波処理およびオゾン処理を行なう。このとき、本実施の形態においては、嫌気性消化槽１の嫌気度をＯＲＰ計４９で測定し、その測定結果を信号線５１を通してコントローラ５２に送る。コントローラ５２では送られてきた測定結果とあらかじめ設定されたＯＲＰの値との比較を行なう。
【０１９９】
測定値があらかじめ設定した範囲内である場合、嫌気性消化槽１の運転状態は良好であると判断し、少なくとも超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８のうちの１つについて、消化汚泥の処理を拡張するように処理条件を変更する。消化汚泥の処理の拡張は、超音波破砕機３０の出力を増加させることにより実現される。また、オゾン発生器３１でのオゾン発生量を増やし、オゾン注入量を増すことによって実現される。さらに、消化汚泥引抜きポンプ３８の流量を増し処理される汚泥の量を増やすことによって実現される。もちろん、これらのうちのいくつか、またはすべてを組み合わせてもよい。
【０２００】
変更された処理条件は、超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８に信号線２８、信号線５３または信号線３９を通して伝えられる。変更後の処理条件を受けた超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８は、その条件にしたがって拡張した消化汚泥の処理を行なう。
【０２０１】
一方、測定値があらかじめ設定した範囲から上回って外れている場合は、嫌気性消化槽１の運転状態が不良であると判断し、少なくとも超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８のうちの１つについて、消化汚泥の処理を縮小するように処理条件を変更する。消化汚泥の処理の縮小は、超音波破砕機３０の出力を低減させることにより実現される。また、オゾン発生器３１でのオゾン発生量を減らし、オゾン注入量を低減することによって実現される。さらに、消化汚泥引抜きポンプ３８の流量を減らし、処理される汚泥の量を低減することによって実現される。もちろん、これらのうちのいくつか、またはすべてを組み合わせてもよい。
【０２０２】
変更された処理条件は、超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８に、信号線２８、信号線５３または信号線３９を通して伝えられる。変更後の処理条件を受けた超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８は、その条件にしたがって縮小した消化汚泥の処理を行なう。
【０２０３】
このように嫌気性消化槽のＯＲＰを計測することによって、分散処理および改質処理が嫌気性消化槽の運転状態におよぼす影響を常時かつ的確に把握することができる。さらに、ＯＲＰの測定結果にもとづき固形物の分散処理および分散処理後の有機物の改質処理を制御することにより、嫌気性消化槽の運転状態を安定に維持することができる。したがって、計測制御を行わない場合にくらべ、消化汚泥中の固形物の溶解性をより安定に増大できる。なお、ここで安定とは、長期間にわたって性能（固形物の溶解）を維持できることを意味する。
【０２０４】
この安定な溶解性増大によって、消化汚泥中の有機物のメタンへの変換率をより安定に向上できるとともに、処分すべき汚泥の発生量も同様により安定に低減することが可能となる。
【０２０５】
なお、本実施の形態では嫌気性消化槽１の運転状態の指標としてＯＲＰを測定したが、溶存酸素濃度など嫌気性消化槽の嫌気度の指標であればこれに限るものではない。また、嫌気度に限らず、嫌気性消化槽の消化汚泥濃度、ｐＨ、消化汚泥の微生物活性に関する指標を計測し、制御にもちいても、同様の効果が得られる。消化汚泥の微生物活性は、たとえば、メタン発酵微生物の補酵素（Ｆ４２０）を蛍光光度計によって測定することにより計測することができる。
【０２０６】
また、本実施の形態では嫌気性消化槽の消化汚泥を分散および改質処理する場合を示したが、実施の形態１のように流入する有機性廃液を分散および改質処理する場合、実施の形態５のように固液分離後の濃縮汚泥を分散および改質処理する場合、実施の形態７のように有機性廃液と消化汚泥の混合汚泥を分散および改質処理する場合、実施の形態９のように有機性廃液と濃縮汚泥の混合汚泥を分散および改質処理する場合においても、同様の計測、制御を行なうことで同様の効果が得られる。
【０２０７】
実施の形態１２
本発明のさらに別の実施の形態における有機性廃液の処理装置、およびそれを用いた有機性廃液の処理方法について説明する。
【０２０８】
図２４は、本実施の形態の有機性廃液の処理装置について、その構成の概略と処理の流れを示した図である。
【０２０９】
図２４に示す本実施の形態の処理装置は、図１６に示した実施の形態４の処理装置において、酸生成槽３３にはＯＲＰ計４９が設置され、信号線５１を介してコントローラ５２に接続されている。コントローラ５２は、超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８に、それぞれ信号線２８、信号線５３および信号線３９を介して接続されている。本実施の形態の処理装置は、ＯＲＰ計とコントローラおよび信号線を除き、図１５に示した前記実施の形態４の処理装置と同様の構成である。
【０２１０】
つぎに本実施の形態の処理装置の動作について説明する。
【０２１１】
実施の形態４と同様に、有機性廃液を酸生成槽３３に導入し微生物によって有機汚泥の溶解を行なうとともに、酸生成槽３３の消化汚泥を引き抜き、超音波処理およびオゾン処理を行なう。このとき、本実施の形態においては、酸生成槽３３の嫌気度をＯＲＰ計４９で測定し、その測定結果を信号線５１を通してコントローラ５２に送る。コントローラ５２では、送られてきた測定結果とあらかじめ設定されたＯＲＰの値との比較を行なう。
【０２１２】
測定値があらかじめ設定した値の範囲内である場合、酸生成槽３３の運転状態が良好であると判断し、少なくとも超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８のうちの１つについて、消化汚泥の処理を拡張するように処理条件を変更する。変更された処理条件は、超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８に、信号線２８、信号線５３または信号線３９を通して伝えられる。変更後の処理条件を受けた超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８は、その条件にしたがって拡張した消化汚泥の処理を行なう。
【０２１３】
一方、測定値があらかじめ設定した範囲を上回って外れている場合は、酸生成槽３３の運転状態が不良であると判断し、少なくとも超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８のうちの１つについて、消化汚泥の処理を縮小するように処理条件を変更する。変更された処理条件は、超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８に、信号線２８、信号線５３または信号線３９を通して伝えられる。変更後の処理条件を受けた超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８は、その条件にしたがって縮小した消化汚泥の処理を行なう。
【０２１４】
このように酸生成槽のＯＲＰを計測することによって、分散処理および改質処理が酸生成槽の運転状態におよぼす影響を常時かつ的確に把握することができる。さらに、ＯＲＰの測定結果にもとづき固形物の分散処理および分散処理後の有機物の改質処理を制御することにより、酸生成槽の運転状態を安定に維持することができる。したがって、計測制御を行わない場合にくらべ、酸生成槽の消化汚泥中の固形物の溶解性をより安定に増大できる。
【０２１５】
この安定な溶解性増大によって、酸生成槽の消化汚泥中の有機物のメタン生成槽でのメタンへの変換率をより安定に向上できるとともに、処分すべき汚泥の発生量も同様により安定に低減することが可能となる。
【０２１６】
また、本実施の形態では酸生成槽３３の運転状態の指標としてＯＲＰを用いたが、溶存酸素濃度など酸生成槽の嫌気度の指標であればこれに限るものではない。また、嫌気度に限らず、酸生成槽の消化汚泥濃度、嫌気度、消化汚泥の微生物活性に関する指標を計測し、制御しても、同様の効果が得られる。
【０２１７】
また、本実施の形態では酸生成槽の消化汚泥を分散および改質処理する場合を示したが、実施の形態２のように流入する有機性廃液を分散および改質処理する場合、実施の形態６のように固液分離後の濃縮汚泥を分散および改質処理する場合、実施の形態８のように有機性廃液と酸生成槽の消化汚泥の混合汚泥を分散および改質処理する場合、実施の形態１０のように有機性廃液と酸生成槽からの濃縮汚泥の混合汚泥を分散および改質処理する場合においても、同様の計測、制御を行なうことで同様の効果が得られる。
【０２１８】
実施の形態１３
本発明のまた別の実施の形態における有機性廃液の処理装置、およびそれを用いた有機性廃液の処理方法について説明する。
【０２１９】
図２５は、本実施の形態の有機性廃液の処理装置について、その構成の概略と処理の流れを示した図である。
【０２２０】
図２５に示す本実施の形態の処理装置は、図１５に示した実施の形態３の処理装置において、有機性廃液導入路２にはＭＬＳＳ計４５が設置され、信号線４０を介してコントローラ５２に接続されている。コントローラ５２は、超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８に、それぞれ信号線２８、信号線５３および信号線３９を介して接続されている。本実施の形態の処理装置は、ＭＬＳＳ計とコントローラおよび信号線を除き図１５に示した前記実施の形態３の処理装置と同様の構成である。
【０２２１】
つぎに本実施の形態の処理装置の動作について説明する。
【０２２２】
実施の形態３と同様に、有機性廃液を嫌気性消化槽１に導入して微生物による消化を行なうとともに、嫌気性消化槽１から消化汚泥を引き抜き、超音波処理およびオゾン処理を行なう。このとき、本実施の形態においては、有機性廃液導入路２を通る廃液の固形物の濃度をＭＬＳＳ計４５で測定し、その測定結果を信号線４０を通してコントローラ５２に送る。コントローラ５２では送られてきた測定結果とあらかじめ設定されたＭＬＳＳ濃度の値との比較を行なう。
【０２２３】
測定値があらかじめ設定した範囲内である場合、嫌気性消化槽１の流入負荷が適切で運転状態は良好に維持できると判断し、少なくとも超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８のうちの１つについて、消化汚泥の処理を拡張するように処理条件を変更する。変更された処理条件は、超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８に、信号線２８、信号線５３または信号線３９を通して伝えられる。変更後の処理条件を受けた超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８は、その条件にしたがって拡張した消化汚泥の処理を行なう。
【０２２４】
一方、測定値があらかじめ設定した範囲から上回って外れている場合は、嫌気性消化槽１の流入負荷が極端に高い、あるいは極端に低く運転状態が良好に維持できなくなると判断し、少なくとも超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８のうちの１つについて、消化汚泥の処理を縮小するように処理条件を変更する。変更された処理条件は、超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８に、それぞれ信号線２８、信号線５３または信号線３９を通して伝えられる。変更後の処理条件を受けた超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８は、その条件にしたがって縮小した消化汚泥の処理を行なう。
【０２２５】
このように流入する有機性廃液の固形物のＭＬＳＳ濃度を計測することによって、嫌気性消化槽の運転状態に影響をおよぼす流入負荷を常時かつ的確に把握することができる。さらに、ＭＬＳＳ濃度の測定結果にもとづき消化汚泥の分散処理および改質処理を制御することにより、嫌気性消化槽の運転状態を安定に維持しながら分散および改質処理を行なうことができる。したがって、計測制御を行わない場合にくらべ、消化汚泥中の固形物の溶解性をより安定に増大できる。
【０２２６】
この安定な溶解性増大によって、消化汚泥中の有機物のメタンへの変換率をより安定に向上できるとともに、処分すべき汚泥の発生量も同様により安定に低減することが可能となる。加えて、消化汚泥からのリン溶出を安定に確保できるため、リン回収量を安定に得ることが可能となる。
【０２２７】
なお、本実施の形態では流入する有機性廃液の固形物濃度の指標としてＭＬＳＳ濃度を測定したが、濁度など固形物濃度の指標であればこれに限るものではない。また、本実施の形態では流入する有機性廃液の指標として固形物濃度を用いたが、これに限るものではなく、ｐＨや嫌気度などの有機性廃液に関する指標を計測し、制御に用いても、同様の効果が得られる。
【０２２８】
また、本実施の形態では嫌気性消化槽の消化汚泥を分散および改質処理する場合を示したが、実施の形態１のように流入する有機性廃液を分散および改質処理する場合、実施の形態５のように固液分離後の濃縮汚泥を分散および改質処理する場合、実施の形態７のように有機性廃液と消化汚泥の混合汚泥を分散および改質処理する場合、実施の形態９のように有機性廃液と濃縮汚泥の混合汚泥を分散および改質処理する場合においても、同様の計測、制御を行なうことで同様の効果が得られる。
【０２２９】
実施の形態１４
本発明のまた別の実施の形態における有機性廃液の処理装置、およびそれを用いた有機性廃液の処理方法について説明する。
【０２３０】
図２６は本実施の形態の有機性廃液の処理装置について、その構成の概略と処理の流れを示した図である。
【０２３１】
図２６に示す本実施の形態の処理装置は、図１６に示した実施の形態４の処理装置において、有機性廃液導入路２にＭＬＳＳ計４５が設置され、信号線４０を介してコントローラ５２に接続されている。コントローラ５２は、超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８に、それぞれ信号線２８、信号線５３および信号線３９を介して接続されている。本実施の形態の処理装置は、ＭＬＳＳ計とコントローラおよび信号線を除き、図１６に示した前記実施の形態４の処理装置と同様の構成である。
【０２３２】
つぎに本実施の形態の処理装置の動作について説明する。
【０２３３】
実施の形態４と同様に、有機性廃液を酸生成槽３３に導入し微生物によって有機汚泥の溶解を行なうとともに、酸生成槽３３の消化汚泥を引き抜き、超音波処理およびオゾン処理を行なう。このとき、本実施の形態においては、有機性廃液導入路２を通る廃液の固形物の濃度をＭＬＳＳ計４５で測定し、その測定結果を信号線４０を通してコントローラ５２に送る。コントローラ５２では、送られてきた結果とあらかじめ設定されたＭＬＳＳ濃度の値との比較を行なう。
【０２３４】
測定値があらかじめ設定した範囲内である場合、酸生成槽３３の流入負荷が適切で運転状態は良好に維持できると判断し、少なくとも超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８のうちの１つについて、消化汚泥の処理を拡張するように処理条件を変更する。変更された処理条件は、超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８に、信号線２８、信号線５３または信号線３９を通して伝えられる。変更後の処理条件を受けた超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８は、その条件にしたがって拡張した消化汚泥の処理を行なう。
【０２３５】
一方、測定値があらかじめ設定した範囲を外れている場合は、酸生成槽３３の流入負荷が極端に高い、あるいは極端に低く運転状態が良好に維持できなくなると判断し、少なくとも超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８のうちの１つについて、消化汚泥の処理を縮小するように処理条件を変更する。変更された処理条件は、超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８に、信号線２８、信号線５３または信号線３９を通して伝えられる。変更後の処理条件を受けた超音波破砕機３０、オゾン発生器３１、消化汚泥引抜きポンプ３８は、その条件にしたがって縮小した消化汚泥の処理を行なう。
【０２３６】
このように流入廃液の固形物の濃度を計測することによって、酸生成槽の運転状態に影響をおよぼす流入負荷を常時かつ的確に把握することができる。さらに、測定した固形物の濃度にもとづいて消化汚泥の分散処理および改質処理を制御することにより、酸生成槽の運転状態を安定に維持しながら分散処理および改質処理を行なうことができる。したがって、計測制御を行わない場合に比べ、消化汚泥中の固形物の溶解性をより安定に増大できる。
【０２３７】
この安定な溶解性増大によって、酸生成槽の消化汚泥中の有機物のメタン生成槽でのメタンへの変換率をより安定に向上できるとともに、処分すべき汚泥の発生量も同様により安定に低減することが可能となる。加えて、消化汚泥からのリン溶出を安定に確保できるため、リン回収量を安定に得ることが可能となる。
【０２３８】
なお、本実施の形態では流入する有機性廃液の固形物濃度の指標としてＭＬＳＳ濃度を測定したが、濁度など固形物濃度の指標であればこれに限るものではない。また、固形物濃度に限らず、ｐＨや嫌気度などの有機性廃液に関する指標を計測し、制御にもちいても、同様の効果が得られる。
【０２３９】
また、本実施の形態では酸生成槽の消化汚泥を分散および改質処理する場合を示したが、実施の形態２のように流入する有機性廃液を分散および改質処理する場合、実施の形態６のように固液分離後の濃縮汚泥を分散および改質処理する場合、実施の形態８のように有機性廃液と酸生成槽の消化汚泥の混合汚泥を分散および改質処理する場合、実施の形態１０のように有機性廃液と酸生成槽からの濃縮汚泥の混合汚泥を分散および改質処理する場合においても、同様の計測、制御を行なうことで同様の効果が得られる。
【０２４０】
実施の形態１５
本発明のほかの実施の形態における有機性廃液の処理装置、およびそれを用いた有機性廃液の処理方法について説明する。
【０２４１】
図２７は、本実施の形態の有機性廃液の処理装置について、その構成の概略と処理の流れを示した図である。
【０２４２】
図２７に示す本実施の形態の処理装置は、図１５に示した実施の形態３の処理装置において、超音波破砕処理槽９にはＭＬＳＳ濃度計４１が、オゾン処理槽１１にはＯＲＰ計４２が設置され、それぞれ信号線４３および信号線４４を介してコントローラ５２に接続されている。コントローラ５２は、超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８に、それぞれ信号線２８、信号線５３および信号線３９を介して接続されている。本実施の形態の処理装置は、ＭＬＳＳ計、ＯＲＰ計、コントローラおよび信号線を除き、図１５に示した前記実施の形態３の処理装置と同様の構成である。
【０２４３】
つぎに本実施の形態の処理装置の動作について説明する。
【０２４４】
実施の形態３と同様に、有機性廃液を嫌気性消化槽１に導入して微生物による消化を行なうとともに、嫌気性消化槽１から消化汚泥を引き抜き、超音波処理およびオゾン処理を行なう。このとき、本実施の形態においては、超音波破砕処理槽９の固形物濃度をＭＬＳＳ濃度計４１で、またオゾン処理槽１１の嫌気度をＯＲＰ計４２で測定し、これら測定結果をそれぞれ信号線４３、信号線４４を通してコントローラ５２に送る。コントローラ５２では、送られてきた結果とあらかじめ設定されたＭＬＳＳ濃度およびＯＲＰの値との比較を行なう。
【０２４５】
ＭＬＳＳ、ＯＲＰの測定値がともにあらかじめ設定した範囲内である場合は、超音波破砕処理槽９およびオゾン処理槽１１での処理が適切で処理状態は良好に維持されていると判断し、消化汚泥の処理を維持するような処理条件を設定し、その処理条件を超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８の少なくとも１つに、信号線２８、信号線５３または信号線３９を通して伝える。処理条件を受けた超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８は、その条件にしたがって維持に向けた消化汚泥の処理を行なう。すなわち、コントローラ５２が、超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８に対し、現状の処理条件で運転を継続するよう指示する。
【０２４６】
一方、ＭＬＳＳ測定値があらかじめ設定した範囲から上回って外れている、またはＯＲＰ測定値値があらかじめ設定した範囲から下回って外れている場合は、超音波破砕処理槽９またはオゾン処理槽１１での処理が不充分であると判断し、少なくとも超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８のうちの１つについて、消化汚泥の処理を拡張するように処理条件を変更する。変更された条件は、超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８に、信号線２８、信号線５３または信号線３９を通して伝えられる。変更後の処理条件を受けた超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８は、その条件にしたがって拡張した消化汚泥の処理を行なう。
【０２４７】
このように超音波破砕処理槽９の固形物濃度およびオゾン処理槽１１の嫌気度の指標を計測することによって、各槽での処理の状態を常時かつ的確に把握することができる。さらに、これら測定結果にもとづいて消化汚泥の分散処理および改質処理を制御することにより、各処理槽での処理状態を安定に保ちながら分散および改質処理を行なうことができる。したがって、計測制御を行わない場合に比べ、消化汚泥中の固形物の溶解性をより安定に増大できる。
【０２４８】
この安定な溶解性増大によって、消化汚泥中の有機物のメタンへの変換率をより安定に向上できるとともに、処分すべき汚泥の発生量も同様により安定に低減することが可能となる。加えて、消化汚泥からのリン溶出を安定に確保できるため、リン回収量を安定に得ることが可能となる。
【０２４９】
なお、本実施の形態では超音波破砕処理槽の固形物濃度として消化汚泥のＭＬＳＳ濃度を測定したが、濁度など固形物濃度の指標であればこれに限るものではない。また、固形物濃度に限らず、超音波破砕処理槽のｐＨ、嫌気度、消化汚泥の微生物活性など処理された消化汚泥に関する指標を計測し、制御しても、同様の効果が得られる。
【０２５０】
また、本実施の形態ではオゾン処理槽の嫌気度の指標としてＯＲＰを用いたが、溶存酸素濃度など嫌気度の指標であればこれに限るものではない。また、嫌気度に限らず、オゾン処理槽のｐＨ、消化汚泥濃度、消化汚泥の微生物活性など処理された消化汚泥に関する指標を計測し、制御しても、同様の効果が得られる。
【０２５１】
また、本実施の形態では超音波破砕処理槽とオゾン処理槽の両方の消化汚泥について同時に計測制御を行なう例を示したが、超音波破砕処理槽とオゾン処理槽のどちらか一方について計測制御を行なってもよい。
【０２５２】
また、本実施の形態では、嫌気性消化槽の消化汚泥を分散および改質処理する場合を示したが、実施の形態１のように流入する有機性廃液を分散および改質処理する場合、実施の形態５のように固液分離後の濃縮汚泥を分散および改質処理する場合、実施の形態７のように有機性廃液と消化汚泥の混合汚泥を分散および改質処理する場合、実施の形態９のように有機性廃液と濃縮汚泥の混合汚泥を分散および改質処理する場合においても、同様の計測、制御を行なうことで同様の効果が得られる。
【０２５３】
実施の形態１６
本発明の別の実施の形態における有機性廃液の処理装置、およびそれを用いた有機性廃液の処理方法について説明する。
【０２５４】
図２８は、本実施の形態の有機性廃液の処理装置について、その構成の概略と処理の流れを示した図である。
【０２５５】
図２８に示す本実施の形態の処理装置は、図１６に示した実施の形態４の処理装置において、超音波破砕処理槽９にはＭＬＳＳ濃度計４１が、オゾン処理槽１１にはＯＲＰ計４２が設置され、それぞれ信号線４３、信号線４４を介してコントローラ５２に接続されている。コントローラ５２は超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８に、それぞれ信号線２８、信号線５３および信号線３９を介して接続されている。本実施の形態の処理装置は、ＭＬＳＳ計、ＯＲＰ計、コントローラおよび信号線を除き、図１６に示した前記実施の形態４の処理装置と同様の構成である。
【０２５６】
つぎに本実施の形態の処理装置の動作について説明する。
【０２５７】
実施の形態４と同様に、有機性廃液を酸生成槽３３に導入し微生物によって有機汚泥の溶解を行なうとともに、酸生成槽３３の消化汚泥を引き抜き、超音波処理およびオゾン処理を行なう。このとき、本実施の形態においては、超音波破砕処理槽９の固形物濃度をＭＬＳＳ濃度計４１で、またオゾン処理槽１１の嫌気度をＯＲＰ計４２で測定し、これらの測定結果をそれぞれ信号線４３、信号線４４を通してコントローラ５２に送る。コントローラ５２では、送られてきた測定結果とあらかじめ設定されたＭＬＳＳ濃度およびＯＲＰの値との比較を行なう。
【０２５８】
ＭＬＳＳ、ＯＲＰの測定値がともにあらかじめ設定した範囲内である場合は、超音波破砕処理槽９およびオゾン処理槽１１での処理が適切で処理状態は良好に維持されていると判断し、消化汚泥の処理を維持するような条件を設定し、その条件を超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８の少なくとも１つに、信号線２８、信号線５３または信号線３９を通して伝える。処理条件を受けた超音波破砕機３０、オゾン発生器３１、消化汚泥引抜きポンプ３８では、その条件にしたがって維持に向けた消化汚泥の処理を行なう。すなわち、コントローラ５２が、超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８に対し、現状の処理条件で運転を継続するよう指示する。
【０２５９】
一方、ＭＬＳＳ測定値があらかじめ設定した範囲から上回って外れている、またはＯＲＰ測定値があらかじめ設定した範囲から下回って外れている場合は、超音波破砕処理槽９またはオゾン処理槽１１での処理が不充分であると判断し、少なくとも超音波破砕機３０、オゾン発生器３１および消化汚泥引抜きポンプ３８のうちの１つについて、消化汚泥の処理を拡張するように処理条件を変更する。変更された処理条件は、超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８に、信号線２８、信号線５３または信号線３９を通して伝えられる。変更後の処理条件を受けた超音波破砕機３０、オゾン発生器３１または消化汚泥引抜きポンプ３８は、その条件にしたがって拡張した消化汚泥の処理を行なう。
【０２６０】
このように、超音波破砕処理槽９の固形物濃度およびオゾン処理槽１１の嫌気度の指標を計測することによって、各槽での処理の状態を常時かつ的確に把握することができる。さらに、これら測定結果にもとづいて消化汚泥の分散処理および改質処理を制御することにより、各処理槽での処理状態を常に適切な状態に保ちながら、安定に分散および改質処理を行なうことができる。したがって、計測制御を行わない場合に比べ、消化汚泥中の固形物の溶解性をより安定に増大できる。
【０２６１】
この安定な溶解性増大によって、酸生成槽の消化汚泥中の有機物のメタン生成槽でのメタンへの変換率をより安定に向上できるとともに、処分すべき汚泥の発生量も同様により安定に低減することが可能となる。加えて、消化汚泥からのリン溶出を安定に確保できるため、リン回収量を安定に得ることが可能となる。
【０２６２】
なお、本実施の形態では超音波破砕処理槽の固形物濃度として消化汚泥のＭＬＳＳ濃度を測定したが、濁度など固形物濃度の指標であればこれに限るものではない。また、固形物濃度に限らず、超音波破砕処理槽のｐＨ、嫌気度、消化汚泥の微生物活性など処理された消化汚泥に関する指標を計測し、制御しても、同様の効果が得られる。
【０２６３】
また、本実施の形態ではオゾン処理槽の嫌気度の指標としてＯＲＰを用いたが、溶存酸素濃度など嫌気度の指標であればこれに限るものではない。また、嫌気度に限らず、オゾン処理槽のｐＨ、消化汚泥濃度、消化汚泥の微生物活性など処理された消化汚泥に関する指標を計測し、制御しても、同様の効果が得られる。
【０２６４】
また、本実施の形態では超音波破砕処理槽とオゾン処理槽の両方の消化汚泥について同時に計測制御を行なう例を示したが、超音波破砕処理槽とオゾン処理槽のどちらか一方について計測制御を行なってもよい。
【０２６５】
また、本実施の形態では、酸生成槽の消化汚泥を分散および改質処理する場合を示したが、実施の形態２のように流入する有機性廃液を分散および改質処理する場合、実施の形態６のように固液分離後の濃縮汚泥を分散および改質処理する場合、実施の形態８のように有機性廃液と消化汚泥の混合汚泥を分散および改質処理する場合、実施の形態１０のように有機性廃液と濃縮汚泥の混合汚泥を分散および改質処理する場合においても、同様の計測、制御を行なうことで同様の効果が得られる。
【０２６６】
実施の形態１７
本発明のまた別の実施の形態における有機性廃液の処理装置、およびそれを用いた有機性廃液の処理方法について説明する。
【０２６７】
図２９は、本実施の形態の有機性廃液の処理装置について、その構成の概略と処理の流れを示した図である。
【０２６８】
図２９に示す本実施の形態の処理装置は、図１３に示した実施の形態１の処理装置において、分離液排出路２０にリン酸濃度計４８が設置され、信号線５４を介してコントローラ５２に接続されている。コントローラ５２は超音波破砕機３０およびオゾン発生器３１に、それぞれ信号線２８および信号線５３を介して接続されている。本実施の形態の処理装置は、リン酸濃度計とコントローラおよび信号線を除き図５に示した前記実施の形態１３の処理装置と同様の構成である。
【０２６９】
つぎに本実施の形態の処理装置の動作について説明する。
【０２７０】
実施の形態１と同様に、有機汚泥のオゾン処理を行ない、固液分離槽１７で固形物と溶液に分け、固形物を嫌気性消化槽１に導入し、消化を行なう。一方、リンを多く含む溶液をリン回収槽２４に送り、炭酸カルシウム溶液を導入し、析出したリン酸カルシウムをリン回収路２５から引き抜く。このとき、本実施の形態においては、分離液排出路２０を通るリンを多く含む溶液のリン酸濃度をリン酸濃度計４８で測定し、その測定結果を信号線５４を通してコントローラ５２に送る。コントローラ５２では送られてきた測定結果とあらかじめ設定されたリン酸濃度の値との比較を行なう。
【０２７１】
測定値があらかじめ設定した範囲内である場合、有機汚泥からのリン溶出が良好で、有機汚泥からのリン回収が良好に維持されていると判断し、流入する有機汚泥のオゾン処理を維持するような条件を設定し、その条件を超音波破砕機３０およびオゾン発生器３１の少なくとも１つに、信号線２８または信号線５３を通して伝える。処理条件を受けた超音波破砕機３０、オゾン発生器３１では、その条件にしたがって維持に向けた消化汚泥の処理を行なう。すなわち、コントローラ５２が、超音波破砕機３０およびオゾン発生器３１に対し、現状の処理条件で運転を継続するよう指示する。
【０２７２】
一方、測定値があらかじめ設定した範囲から下回って外れている場合は、有機汚泥からのリン溶出が低くリン回収が不充分と判断し、少なくとも超音波破砕機３０およびオゾン発生器３１のうちの１つについて、消化汚泥の処理を拡張するように処理条件を変更する。変更された処理条件は、超音波破砕機３０またはオゾン発生器３１に、信号線２８または信号線５３を通して伝えられる。変更後の処理条件を受けた超音波破砕機３０またはオゾン発生器３１は、その条件にしたがって拡張した消化汚泥の処理を行なう。
【０２７３】
このようにオゾン処理、固液分離後の溶液のリン酸濃度を計測し、この測定結果にもとづき有機汚泥の分散処理および改質処理を制御することにより、有機汚泥からのリン溶出を安定に確保できる。したがって、計測制御を行わない場合にくらべ、有機汚泥からのリン回収量をより安定に維持できる。
【０２７４】
なお、本実施の形態ではオゾン処理、固液分離後の溶液のリンの指標としてリン酸濃度を測定したが、全リン濃度などリンの指標であればこれに限るものではない。
【０２７５】
また、本実施の形態では、嫌気性消化槽の消化汚泥を分散および改質処理する場合を示したが、実施の形態１のように流入する有機性廃液を分散および改質処理する場合、実施の形態５のように固液分離後の濃縮汚泥を分散および改質処理する場合、実施の形態７のように有機性廃液と消化汚泥の混合汚泥を分散および改質処理する場合、実施の形態９のように有機性廃液と濃縮汚泥の混合汚泥を分散および改質処理する場合においても、同様の計測、制御を行なうことで同様の効果が得られる。
【０２７６】
実施の形態１８
本発明のまた別の実施の形態における有機性廃液の処理装置、およびそれを用いた有機性廃液の処理方法について説明する。
【０２７７】
図３０は、本実施の形態の有機性廃液の処理装置について、その構成の概略と処理の流れを示した図である。
【０２７８】
図３０に示す本実施の形態の処理装置は、図１４に示した実施の形態２の処理装置において、分離液排出路２０にリン酸濃度計４８が設置され、信号線５４を介してコントローラ５２に接続されている。コントローラ５２は、超音波破砕機３０およびオゾン発生器３１に、それぞれ信号線２８および信号線５３を介して接続されている。本実施の形態の処理装置は、リン酸濃度計とコントローラおよび信号線を除き図１４に示した前記実施の形態２の処理装置と同様の構成である。
【０２７９】
つぎに本実施の形態の処理装置の動作について説明する。
【０２８０】
実施の形態２と同様に、有機汚泥のオゾン処理を行ない、固液分離槽１７で固形物と溶液に分け、固形物を酸生成槽３３に導入し、溶解を行なう。一方、リンを多く含む溶液をリン回収槽２４に送り、炭酸カルシウム溶液を導入し、析出したリン酸カルシウムをリン回収路２５から引き抜く。このとき、本実施の形態においては、分離液排出路２０を通るリンを多く含む溶液のリン酸濃度をリン酸濃度計４８で測定し、その測定結果を信号線５４を通してコントローラ５２に送る。コントローラ５２では送られてきた測定結果とあらかじめ設定されたリン酸濃度の値との比較を行なう。
【０２８１】
測定値があらかじめ設定した範囲内である場合、有機汚泥からのリン溶出が良好で、有機汚泥からのリン回収が良好に維持されていると判断し、流入する有機汚泥のオゾン処理を維持するような条件を設定し、その条件を超音波破砕機３０およびオゾン発生器３１の少なくとも１つに、信号線２８または信号線５３を通して伝える。処理条件を受けた超音波破砕機３０、オゾン発生器３１では、その条件にしたがって維持に向けた消化汚泥の処理を行なう。すなわち、コントローラ５２が、超音波破砕機３０およびオゾン発生器３１に対し、現状の処理条件で運転を継続するよう指示する。
【０２８２】
一方、測定値があらかじめ設定した範囲から下回って外れている場合は、有機汚泥からのリン溶出が低くリン回収が不充分と判断し、少なくとも超音波破砕機３０およびオゾン発生器３１のうちの１つについて、消化汚泥の処理を拡張するように処理条件を変更する。変更された処理条件は、超音波破砕機３０またはオゾン発生器３１に、信号線２８または信号線５３を通して伝えられる。変更後の処理条件を受けた超音波破砕機３０またはオゾン発生器３１は、その条件にしたがって拡張した消化汚泥の処理を行なう。
【０２８３】
このようにオゾン処理、固液分離後の溶液のリン酸濃度を計測し、この測定結果にもとづき有機汚泥のオゾン処理を制御することにより、有機汚泥からのリン溶出を安定に確保できる。したがって、計測制御を行わない場合にくらべ、有機汚泥からのリン回収量をより安定に維持できる。
【０２８４】
なお、本実施の形態ではオゾン処理、固液分離後の溶液のリンの指標としてリン酸濃度を測定したが、全リン濃度などリンの指標であればこれに限るものではない。
【０２８５】
また、本実施の形態では、酸生成槽の消化汚泥を分散および改質処理する場合を示したが、実施の形態２のように流入する有機性廃液を分散および改質処理する場合、実施の形態６のように固液分離後の濃縮汚泥を分散および改質処理する場合、実施の形態８のように有機性廃液と消化汚泥の混合汚泥を分散および改質処理する場合、実施の形態１０のように有機性廃液と濃縮汚泥の混合汚泥を分散および改質処理する場合においても、同様の計測、制御を行なうことで同様の効果が得られる。
【０２８６】
実施の形態１９
本発明のまた別の実施の形態における有機性廃液の処理装置、およびそれを用いた有機性廃液の処理方法について説明する。
【０２８７】
図３１は、本実施の形態の有機性廃液の処理装置について、その構成の概略と処理の流れを示した図である。
【０２８８】
図３１に示す本実施の形態の処理装置は、図１３に示した実施の形態１の処理装置において、分離液排出路２０にリン酸濃度計４８が設置され、信号線５４を介してコントローラ５２に接続されている。コントローラ５２は、凝集剤導入ポンプ２２に信号線５５を介して接続されている。本実施の形態の処理装置は、リン酸濃度計とコントローラおよび信号線を除き図１３に示した前記実施の形態１の処理装置と同様の構成である。
【０２８９】
つぎに本実施の形態の処理装置の動作について説明する。
【０２９０】
実施の形態１と同様に、有機汚泥のオゾン処理を行ない、固液分離槽１７で固形物と溶液に分け、固形物を嫌気性消化槽１に導入し、消化を行なう。一方、リンを多く含む溶液をリン回収槽２４に送り、炭酸カルシウム溶液を導入し、析出したリン酸カルシウムをリン回収路２５から引き抜く。このとき、本実施の形態においては、分離液排出路２０を通るリンを多く含む溶液のリン酸濃度をリン酸濃度計４８で測定し、その測定結果を信号線５４を通してコントローラ５２に送る。コントローラ５２では送られてきた測定結果から溶液中のリンを析出させるのに必要な炭酸カルシウムの量を計算し、この量が確保できるよう信号線５５を通して凝集剤導入ポンプ２２の流量を変更する。
【０２９１】
このようにオゾン処理、固液分離後の溶液のリン酸濃度を計測し、この測定結果にもとづき凝集剤の添加量を制御することにより、溶液中のリンを溶液中に残存させずほぼ全量をリン酸カルシウムとして回収できるとともに、凝集剤の過剰投与を避けることができる。したがって、計測制御を行わない場合にくらべ、有機汚泥からのリン回収量をより効率的かつ確実に得られる。
【０２９２】
なお、本実施の形態ではオゾン処理、固液分離後の溶液のリンの指標としてリン酸濃度を測定したが、全リン濃度などリンの指標であればこれに限るものではない。
【０２９３】
また、本実施の形態では流入する有機汚泥をオゾン処理する場合を示したが、実施の形態３のように嫌気性消化槽の消化汚泥をオゾン処理する場合、実施の形態５のように固液分離後の濃縮汚泥をオゾン処理する場合、実施の形態７のように有機汚泥と消化汚泥の混合汚泥をオゾン処理する場合、実施の形態９のように有機汚泥と濃縮汚泥の混合汚泥をオゾン処理する場合においても、同様の計測、制御を行なうことで同様の効果が得られる。
【０２９４】
実施の形態２０
本発明のまた別の実施の形態における有機性廃液の処理装置、およびそれを用いた有機性廃液の処理方法について説明する。
【０２９５】
図３２は、本実施の形態の有機性廃液の処理装置について、その構成の概略と処理の流れを示した図である。
【０２９６】
図３２に示す本実施の形態の処理装置は、図１４に示した実施の形態２の処理装置において、分離液排出路２０にリン酸濃度計４８が設置され、信号線５４を介してコントローラ５２に接続されている。コントローラ５２は、凝集剤導入ポンプ２２に信号線５５を介して接続されている。本実施の形態の処理装置は、リン酸濃度計とコントローラおよび信号線を除き図１４に示した前記実施の形態２の処理装置と同様の構成である。
【０２９７】
つぎに本実施の形態の処理装置の動作について説明する。
【０２９８】
実施の形態２と同様に、有機汚泥のオゾン処理を行ない、固液分離槽１７で固形物と溶液に分け、固形物を酸生成槽３３に導入し、溶解を行なう。一方、リンを多く含む溶液をリン回収槽２４に送り、炭酸カルシウム溶液を導入し、析出したリン酸カルシウムをリン回収路２５から引き抜く。このとき、本実施の形態においては、分離液排出路２０を通るリンを多く含む溶液のリン酸濃度をリン酸濃度計４８で測定し、その測定結果を信号線５４を通してコントローラ５２に送る。コントローラ５２では送られてきた測定結果から溶液中のリンを析出させるのに必要な炭酸カルシウムの量を計算し、この量が確保できるよう信号線５５を通して凝集剤導入ポンプ２２の流量を変更する。
【０２９９】
このようにオゾン処理、固液分離後の溶液のリン酸濃度を計測し、この測定結果にもとづき凝集剤の添加量を制御することにより、溶液中のリンを溶液中に残存させずほぼ全量をリン酸カルシウムとして回収できるとともに、凝集剤の過剰投与を避けることができる。したがって、計測制御を行わない場合にくらべ、有機汚泥からのリン回収量をより効率的かつ確実に得られる。
【０３００】
なお、本実施の形態ではオゾン処理、固液分離後の溶液のリンの指標としてリン酸濃度を測定したが、全リン濃度などリンの指標であればこれに限るものではない。
【０３０１】
また、本実施の形態では流入する有機汚泥をオゾン処理する場合を示したが、実施の形態４のように酸生成槽の消化汚泥をオゾン処理する場合、実施の形態６のように固液分離後の濃縮汚泥をオゾン処理する場合、実施の形態８のように有機汚泥と消化汚泥の混合汚泥をオゾン処理する場合、実施の形態１０のように有機汚泥と濃縮汚泥の混合汚泥をオゾン処理する場合においても、同様の計測、制御を行なうことで同様の効果が得られる。
【０３０２】
実施の形態２１
前記実施の形態１から２０においては、有機汚泥、消化汚泥および濃縮汚泥を分散処理する方法として超音波処理を、分散後のこれら汚泥を改質処理する方法としてオゾン処理を示したが、これに限るものではない。分散処理方法としては、ホモジナイズ、ミル破砕、高圧噴射による衝突、ローラー、ヒューズプレス、加圧、減圧、ワーリングブレンダ−を用いることができる。また、改質処理方法としては酸添加、アルカリ添加、界面活性剤添加、過酸化水素添加、紫外線照射、加熱、高電圧パルス、熱プラズマ、超臨界水や亜臨界水利用などの水熱反応処理を用いても同等かそれ以上の効果が得られる。
【０３０３】
実施の形態２２
前記実施の形態１から２０においては溶出したリン回収に凝集剤として炭酸カルシウムを用いたが、これに限るものではなく、炭酸水素カルシウムなどほかのカルシウムを含む物質でも同等の効果が得られ、ＰＡＣ（ポリ塩化アルミニウム）などの一般的な凝集剤を用いてもよい。また、前記実施の形態では溶出したリンの回収方法として凝集剤を用いたが、これに限るものではなく、晶析法などの別のリン固形化方法を用いることもできる。
【０３０４】
また、これら実施の形態においては、リン回収後の液をリン回収後処理水導入路２６を用いて嫌気性消化槽に戻したが、これに限るものではなく、リン回収後の液を嫌気性消化槽に戻さず、別途処理を行なってもかまわない。
【０３０５】
実施の形態２３
前記実験、および実施の形態においては有機性廃液として下水処理場の初沈汚泥と余剰汚泥を混合した有機汚泥を用いたが、これに限るものではなく、下水処理場の初沈汚泥、余剰汚泥、生ごみ、食品残渣、畜産糞尿、し尿、工場廃液、またはこれらの混合物など有機物濃度が高い汚泥、廃棄物、廃液に対して同等またはそれ以上の効果が得られる。
【０３０６】
【発明の効果】
本発明の有機性廃液の処理方法および装置によれば、有機性廃液中の固形物に対し、分散処理と分散後の有機物の改質処理とを組み合わせた処理を行なうことによって、分散処理または改質処理の単独処理にくらべ、流入廃液中の固形物の溶解性を増大できるという効果がある。この溶解性増大によって、流入廃液中の有機物のメタンへの変換率をよりいっそう向上できるとともに、処分すべき汚泥の発生量もよりいっそう低減することが可能となり、同時に固形物中に含有されるリンを固形物外に高い効率で溶出できるという効果がある。
【０３０７】
この溶解性増大によって、流入廃液中の有機物のメタンへの変換率を向上できるとともに、処分すべき汚泥の発生量を低減できる。同時に、リンの固形物外への高効率溶出によって、有限資源であるリンを効率よく回収することが可能となる。
【０３０８】
また、本発明によれば、嫌気性消化を行なう槽の消化汚泥に対し、分散処理と分散後の有機物の改質処理とを組み合わせた処理を行なうことによって、あるいは嫌気性消化を行なう槽の消化汚泥を固液分離し、固液分離後の消化汚泥中の固形物に対し、分散処理と分散後の有機物の改質処理とを組み合わせた処理を行なうことによって、分散処理または改質処理の単独処理にくらべ、嫌気性消化において溶解されずに残存する固形物の溶解性を増大でき、同時に固形物中に含有されるリンを固形物外に高い効率で溶出できるという効果がある。
【０３０９】
とくに、嫌気性消化を行なう槽の消化汚泥、およびその固液分離後の固形物中には、生物によって溶解し難い難溶解性物質が多く蓄積されているため、これら消化汚泥に対し、あるいはこれら消化汚泥を固液分離した後の固形物に対し、分散処理と改質処理との組合せ処理を行なうことによって、難溶解性物質の溶解性増大を促進できる。
【０３１０】
この溶解性増大によって、流入廃液中の有機物のメタンへの変換率を向上できるとともに、処分すべき汚泥の発生量をよりいっそう低減できる。同時に、リンの固形物外への高効率溶出によって、有限資源であるリンをより効率よく回収することが可能となる。
【０３１１】
また、本発明によれば、嫌気性消化を行なう槽の消化汚泥と流入廃液とを混合し、あるいは、嫌気性消化を行なう槽の消化汚泥を固液分離し、分離後の消化汚泥と流入廃液とを混合し、これら混合液中の固形物に対し、分散処理と分散後の有機物の改質処理とを組み合わせた処理を行なうことによって、分散処理または改質処理の単独処理に比べ、嫌気性消化において溶解されずに残存する固形物の溶解性を増大でき、同時に固形物中に含有されるリンを固形物外に高い効率で溶出できるという効果がある。
【０３１２】
とくに、流入する流入廃液の固形物中に難溶解性物質が多く含まれるような場合、難溶解性物質が多く存在する嫌気性消化を行なう槽の消化汚泥、またはその固液分離後の消化汚泥と混合して、これらを同時に処理することによって難溶解性物質の溶解性増大をさらに促進できる。
【０３１３】
この溶解性増大によって、流入廃液中の有機物のメタンへの変換率を向上できるとともに、処分すべき汚泥の発生量をよりいっそう低減できる。同時に、リンの固形物外への高効率溶出によって、有限資源であるリンをより効率よく回収することが可能となる。
【図面の簡単な説明】
【図１】 本発明の有機性廃液処理方法について、経過時間とＶＳＳ濃度の関係を示した図である。
【図２】 本発明の有機性廃液処理方法について、経過時間と消化ガス発生量の関係を示した図である。
【図３】 本発明の有機性廃液処理方法について、溶出リン濃度を示した図である。
【図４】 本発明の有機性廃液処理方法について、滞留時間とＶＳＳ低減率の関係を示した図である。
【図５】 本発明の有機性廃液処理方法について、消化ガス発生率を示した図である。
【図６】 本発明の有機性廃液処理方法について、リン回収率を示した図である。
【図７】 本発明の有機性廃液処理方法について、滞留時間とＶＳＳ低減率の関係を示した図である。
【図８】 本発明の有機性廃液処理方法について、消化ガス発生率を示した図である。
【図９】 本発明の有機性廃液処理方法について、リン回収率を示した図である。
【図１０】 本発明の有機性廃液処理方法について、滞留時間とＶＳＳ低減率の関係を示した図である。
【図１１】 本発明の有機性廃液処理方法について、消化ガス発生率を示した図である。
【図１２】 本発明の有機性廃液処理方法について、リン回収率を示した図である。
【図１３】 本発明の一実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図１４】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図１５】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図１６】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図１７】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図１８】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図１９】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図２０】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図２１】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図２２】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図２３】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図２４】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図２５】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図２６】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図２７】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図２８】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図２９】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図３０】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図３１】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【図３２】 本発明の別の実施の形態の有機性廃液処理装置について、その構成および処理の流れを示した図である。
【符号の説明】
１ 嫌気性消化槽、２ 有機性廃液導入路、３ 消化汚泥排出路、４ 固液分離槽、５ 濃縮汚泥排出路、６ 汚泥廃棄路、７ 汚泥返送路、８ 処理水排出路、９超音波破砕処理槽、１１ オゾン処理槽、１３ メタン生成槽、１４ 消化汚泥排出路、１５ 固液分離槽、１６ 処理水排出路、１７ 固液分離槽、 １８ 処理液排出路、１９ 濃縮液導入路、２０ 分離液排出路、２１ 凝集剤保持槽、２２ 凝集剤導入ポンプ、 ２３ 凝集剤導入路、２４ リン回収槽、２５ リン回収路、２６ リン回収後液導入路、２７ 濃縮汚泥排出路、２８ 信号線、３０超音波破砕器、３１ オゾン発生器、３２ オゾンガス注入路、 ３３ 酸生成槽、３４ 汚泥廃棄路、３５ 汚泥返送路、３６ 消化ガス排出路、３７ 有機性廃液導入ポンプ、３８ 消化汚泥引抜きポンプ、３９ 信号線、４０ 信号線、４１ ＭＬＳＳ計、４２ ＯＲＰ計、４３ 信号線、４４ 信号線、４５ ＭＬＳＳ計、４６ 汚泥返送ポンプ、４７ 消化汚泥引抜き路、 ４８ リン酸濃度計、４９ ＯＲＰ計、５２ コントローラ、５１ 信号線、 ５３ 信号線、５４ 信号線、５５ 信号線、１０２ 膜分離装置、１０３ 改質槽、１０４ 被処理液路、 １０５ 返送汚泥路、１１１ 連絡路、１１７ 濃縮液取出路、１２３ 改質汚泥路。[0001]
BACKGROUND OF THE INVENTION
The present invention relates to an organic waste liquid processing method and processing apparatus.
[0002]
[Prior art]
This is called anaerobic digestion using anaerobic microorganisms for the treatment of slurry-like high-concentration organic waste liquids such as waste liquids from manufacturing processes such as food, organic sludge discharged from sewage wastewater treatment processes, and human waste. Processing methods are widely implemented. In this anaerobic digestion, the organic matter in the waste liquid is converted into methane gas by the action of microorganisms through the process of solids dissolution, organic acid production, and methane production. Since this methane gas can be used as a fuel or a power generation raw material, it is attracting attention as an energy production type processing method.
[0003]
However, in this anaerobic digestion, the action of microorganisms from dissolution of solids to organic acid production and methane production is slow, and it takes a long time to process, so that the digester that performs anaerobic digestion, in particular, an anaerobic digestion is enlarged. There are drawbacks.
[0004]
Further, the inflow waste liquid to be treated often contains solids that are hardly dissolved by anaerobic microorganisms, such as fibers derived from paper and wood, and cell walls of microorganisms, that is, hardly soluble substances. Since this hardly soluble substance remains undissolved even in the process of solids dissolution and organic acid generation, it is extracted from the digestion tank as undecomposed sludge without being converted to methane gas, and is then incinerated or other methods to save energy. To be disposed of. In the current anaerobic digestion, about 50% of the solids in the influent waste liquid cannot be dissolved and are discarded and, as a result, the energy recovery as methane gas is only about 50%. Therefore, in order to increase the energy recovery rate from organic matter in the influent wastewater and reduce the amount of sludge to be disposed of, dissolve the hardly soluble substances present in the influent wastewater and digested sludge, and promote the conversion to methane gas This is a problem.
[0005]
The dissolution of these hardly soluble substances involves modifying the hardly soluble substance into a readily soluble substance, that is, modifying it to a substance that is soluble for microorganisms in an anaerobic digestion tank, and dissolving them by microorganisms. An effective and efficient method for reforming easily soluble substances and reformers are important.
[0006]
In recent years, it has become clear that there is a limit to the number of phosphorus mining years, and the reuse of phosphorus resources is regarded as important. Organic waste liquid, especially organic sludge generated in the sewage wastewater treatment process, may contain a relatively high concentration of phosphorus. A method for eluting, recovering, and reusing phosphorus from this organic sludge. The equipment has become important.
[0007]
As a method for increasing the solubility of solid matter in anaerobic digestion and improving the conversion to methane gas, Patent Document 1 describes that digested sludge extracted from an anaerobic digester is modified by ozone treatment or high-pressure pulse discharge treatment. A treatment method for returning the treated sludge to the anaerobic digester is described. In such a treatment method, waste liquid to be treated is introduced from the liquid passage to be treated, and digestion is performed in an anaerobic digester. The sludge in the anaerobic digester is transported to the membrane separator through the communication path and separated into concentrated sludge and treatment liquid. The sludge separated by the membrane separator is returned to the anaerobic digestion tank by the return sludge path, but part of it is sent to the reforming tank through the concentrate extraction path, and after performing ozone treatment here, It is returned to the anaerobic digester via the modified sludge path.
[0008]
An example of an attempt to elute and recover phosphorus from organic sludge generated in a wastewater treatment process is disclosed in Non-Patent Document 1, for example. Here, the result which eluted the phosphorus component in activated sludge in a liquid phase by heat-processing the activated sludge of a sewage treatment plant at 70-90 degreeC for a maximum of 120 minutes is disclosed.
[0009]
[Patent Document 1]
JP-A-9-206785 (page 2-3, FIG. 1)
[Non-Patent Document 1]
Hisao Otake, 4 others, “Repair of contaminated environment using bioremediation technology, biotechnology for recycling and recycling of phosphorus resources”, Journal of Environmental Science, Environmental Science Society, 1999, Vol. 12, No. 4, p. 433-441
[0010]
[Problems to be solved by the invention]
In the prior art using ozone of Patent Document 1, the sludge is treated with ozone only to improve the sludge solubility. In this ozone treatment, the effect of eluting phosphorus contained in the sludge into the liquid phase. Is not shown at all. On the other hand, in the conventional technology related to phosphorus recovery from sewage sludge in Non-Patent Document 1, the phosphorus component in the sludge is eluted in the liquid phase by heat treatment, but this heat treatment is performed only for phosphorus elution. No effect other than phosphorus elution by heat treatment of sludge is shown. Therefore, no processing method and processing apparatus for simultaneously recovering energy and phosphorus from sludge have been disclosed so far, and there is no method or apparatus for realizing it.
[0011]
In addition, the sludge in the anaerobic digestion tank has a high concentration of various microorganisms and organic polymers to form a sludge floc. However, in the conventional technology using ozone, since the ozone treatment is directly performed on the solid matter in the digested sludge, the ozone cannot permeate into the sludge floc, and the ozone is in contact with the surface of the sludge solid matter. Will only react. As a result, with such ozone treatment alone, modification of a hardly soluble substance, that is, conversion to a readily soluble substance becomes insufficient, and the effect of increasing the solubility of sludge solids and improving the conversion efficiency to methane gas is sufficient. There was a problem that could not be obtained.
[0012]
Further, in the prior art, it is possible to disperse solid matter by ozone treatment, and to react ozone with a hardly decomposable substance inside the solid matter, but when trying to disperse solid matter only with ozone, As a result, the amount of ozone consumption increases, and a large amount of ozone is required to achieve the modification of a hardly soluble substance, that is, the conversion to a readily soluble substance, resulting in an inefficient treatment and high operating costs. There was a problem that.
[0013]
In the present invention, when treating organic waste liquid from the production process or organic sludge generated by sewage wastewater treatment by anaerobic digestion, the solubility of solids contained in the organic waste liquid, organic sludge or anaerobic digested sludge is reduced. In addition to increasing the conversion rate to methane gas and reducing the amount of sludge to be disposed of, at the same time, phosphorus that is concerned about depletion is eluted from organic waste liquid, organic sludge or anaerobic digested sludge, It is an object of the present invention to provide an energy / phosphorus simultaneous recovery type processing method and processing apparatus that can be recovered as a resource. Furthermore, the present invention solves the problem of low efficiency in a single process, and by combining two or more processes, it is possible to process organic waste liquid that can achieve simultaneous energy and phosphorus recovery with less energy and cost. It is an object to provide a method and a processing apparatus.
[0014]
[Means for Solving the Problems]
In order to achieve the said objective, the detailed examination with respect to the solubility by a living body was performed about the inflowing organic waste liquid and the solid substance in digested sludge. As a result, in order to improve the solubility of organisms, first, the solids in the organic waste liquid and digested sludge are dispersed by mechanical treatment, and then the dispersed fibers and cell walls are hardly dissolved. When chemical substances are modified to low molecular weight, which is easy to dissolve microorganisms by chemical treatment, not only can very high sludge solubility and conversion efficiency to methane gas be achieved, but also phosphorus in the sludge can be achieved. It was found that the elution efficiency of can be increased.
[0015]
That is, the present invention is an organic waste liquid treatment method for performing anaerobic digestion to achieve the above object,
At least one of the inflowing organic waste liquid, the digested sludge extracted from the anaerobic digestion process, and the solid sludge after solid-liquid separation of the digested sludge, or the organic sludge, digested sludge or concentrated sludge A dispersion treatment step of dispersing at least a part of solids in the mixture of
A modification treatment step for modifying the organic matter in the organic waste liquid, digested sludge or concentrated sludge after the dispersion treatment, or a mixture of the organic sludge, digested sludge or concentrated sludge;
A separation step of separating the organic waste liquid after the reforming treatment, digested sludge or concentrated sludge, or a mixture of the organic sludge, digested sludge or concentrated sludge into a solution and a solid;
The step of anaerobically digesting the solid after the separation step
A method including:
[0016]
Further, the present invention is an organic waste liquid treatment apparatus comprising an apparatus for performing anaerobic digestion to achieve the above object,
At least one of the inflowing organic waste liquid, the digested sludge extracted from the anaerobic digester, and the solid sludge after solid-liquid separation of the digested sludge, or the organic sludge, digested sludge or concentrated A dispersion treatment device for dispersing at least a part of the solid in the sludge mixture;
A reforming treatment device for reforming organic matter in at least one of organic waste liquid, digested sludge and concentrated sludge after treatment by the dispersion treatment device, or a mixture of the organic sludge, digested sludge or concentrated sludge;
A separator for separating the organic waste liquid, digested sludge or concentrated sludge, or a mixture of the organic sludge, digested sludge or concentrated sludge, which has been treated in the reforming apparatus, into a solution and a solid;
Introducing device for introducing solid matter after being treated in the separation device into the anaerobic digestion device
It is an apparatus provided with.
[0017]
DETAILED DESCRIPTION OF THE INVENTION
An experiment was conducted to confirm the effect of the organic waste liquid treatment method of the present invention.
[0018]
Experiment 1
The organic sludge mixed with primary sludge and excess sludge from a sewage treatment plant was subjected to ultrasonic treatment as a mechanical dispersion treatment and then subjected to ozone treatment as a chemical modification treatment. In the ultrasonic treatment, the oscillation output is 1.0 kW and the treatment time is 15 minutes. In the ozone treatment, the ozone injection rate is 0.05 g-O. _Three / G-SS. An anaerobic digested sludge having a VSS concentration of about 17,000 mg / L was introduced into a culture bottle having an effective volume of 3.0 L for 1.0 L, and the pH was adjusted to near neutral and the VSS concentration was adjusted to about 17,000 mg / L. The treated sludge (1.0 L was mixed. 2.0 L of the mixed sludge prepared in this way was kept in an anaerobic state at 50 ° C. and digested.
[0019]
For comparison, only the ultrasonic treatment and the ozone treatment were performed on the same organic sludge. In the ultrasonic treatment, the oscillation output is 1.0 kW and the treatment time is 15 minutes. In the ozone treatment, the ozone injection rate is 0.05 g-O. _Three / G-SS. 1.0 L of anaerobic digested sludge having a VSS concentration of about 17,000 mg / L was introduced into a culture bottle having an effective volume of 3.0 L, and the pH was adjusted to near neutral and the VSS concentration was adjusted to about 17,000 mg / L. 1.0 L of each treated sludge was mixed. The thus prepared 2.0 L of mixed sludge having a VSS concentration of about 17,000 mg / L was kept in an anaerobic state at 50 ° C. and digested.
[0020]
Furthermore, as a control experiment, only anaerobic digested sludge having a VSS concentration of about 17,000 mg / L was put into a 2.0 L culture bottle without adding ultrasonically treated or ozone treated sludge, and similarly at 50 ° C. Digestion was performed while maintaining an anaerobic state.
[0021]
FIG. 1 shows the daily change of the VSS concentration in this experiment, and FIG. 2 shows the generation amount (integrated value) of digestion gas. In FIG. 1 and FIG. 2, the data when untreated is the curve L1, the data when only the ultrasonic treatment is performed is the curve L2, and the data when only the ozone treatment is performed is the curve L3, the ultrasonic treatment and the ozone treatment. The data when the combined processing is performed is represented by a curve L4.
[0022]
As shown in FIG. 1, by performing ultrasonic treatment or ozone treatment, the solid matter in the sludge is dissolved and the reduction in the VSS concentration is promoted. However, in the combined treatment in which the ozone treatment is performed after the ultrasonic treatment, Compared to sonication alone or ozone treatment alone, dissolution of solids in the sludge is further promoted, and the effect of reducing the VSS concentration is significantly increased.
[0023]
For example, the decrease in VSS concentration in 15 days is about 2,400 mg / L in the case of only ozone treatment, and about 2,100 mg / L in the case of only ultrasonic treatment, whereas ultrasonic treatment and ozone treatment are performed. In the treatment method of the present invention using both of the above and the like, it was about 6,000 mg / L, and a large reduction in VSS concentration that could not be obtained by a simple sum of the case of ultrasonic treatment alone and the case of ozone treatment alone was obtained.
[0024]
In addition, as shown in FIG. 2, the digestion gas generation amount (integrated value) when ultrasonic treatment and ozone treatment are used in combination is larger than the gas generation amount in the case of ultrasonic treatment alone or ozone treatment alone. Of course, it was bigger than their sum.
[0025]
Further, the sludge immediately after each treatment was centrifuged, and the phosphorus concentration in the supernatant was measured. The results are shown in FIG. In the case of untreated, almost no phosphorus was detected, but in the case of only ozone treatment and only sonication, both were about 20 mg / L, whereas the treatment of the present invention using ultrasonic treatment and ozone treatment in combination. In the method, it was about 55 mg / L, and a large phosphorus elution concentration that cannot be obtained by a simple sum of the case of only ultrasonic treatment and the case of only ozone treatment was obtained. When the calcium carbonate solution is mixed with the supernatant from which phosphorus is eluted in this way and stirred, the phosphorus in the solution can be precipitated as calcium phosphate, and solid-liquid separation such as centrifugation and membrane separation can be performed to obtain a solid form. It was recovered as phosphorus.
[0026]
From these results, the treatment method of the present invention, in which ozone treatment is further performed after ultrasonic treatment, not only has a large effect of promoting the dissolution of organic solids in organic sludge and the generation of digestion gas, but at the same time organic It was found that the effect of eluting phosphorus in sludge was great.
[0027]
In the ultrasonic treatment, it is preferable that the oscillation output is 0.1 to 3.0 kW and the treatment is performed for about 5 to 25 minutes. When the oscillation output is smaller than 0.1 kW, the organic matter in the organic sludge cannot be sufficiently decomposed, the conversion efficiency to methane gas cannot be improved, and the phosphorus in the organic sludge cannot be eluted. When the oscillation output is larger than 3.0 kW, high conversion efficiency to methane gas and phosphorus elution amount can be ensured, but the efficiency is not increased and the cost is increased. Moreover, when processing time is shorter than 5 minutes, the organic substance in organic sludge cannot fully be decomposed | disassembled, but it cannot not only improve the conversion efficiency to methane gas, but also cannot elute phosphorus in organic sludge. When the treatment time is longer than 25 minutes, high conversion efficiency to methane gas and phosphorus elution amount can be secured, but the efficiency is not increased and the cost is increased.
[0028]
The ozone injection rate in the ozone treatment is 0.01 to 0.10 g-O. _Three / G-SS is preferred, especially 0.03-0.07 g-O. _Three About / g-SS is preferable. Ozone injection rate is 0.01g-O _Three If it is less than / g-SS, the organic matter in the organic sludge cannot be sufficiently decomposed and the conversion efficiency to methane gas cannot be improved, and the phosphorus in the organic sludge cannot be eluted. On the other hand, the ozone injection rate is 0.10 g-O. _Three If it exceeds / g-SS, high conversion efficiency to methane gas and phosphorus elution amount can be ensured, but the efficiency is not increased and the cost is increased.
[0029]
Experiment 2
In the experiment 1, sludge was not added to the culture bottle or extracted from the culture bottle during the experiment. However, in an actual sludge treatment plant, sludge is continuously charged and extracted. Therefore, a continuous treatment experiment was conducted in which organic sludge mixed with primary sludge and surplus sludge in a sewage treatment plant was continuously added for digestion.
[0030]
Five culture bottles having an effective volume of 5.0 L were prepared, and 4.0 L of anaerobic digested sludge having a VSS concentration of about 17,000 mg / L was added thereto, and anaerobic digestion was performed at 50 ° C.
[0031]
Also, the organic sludge that has been subjected to the same ultrasonic dispersion treatment and ozone modification treatment as in Experiment 1 is allowed to stand for 30 minutes, and separated into a solution that does not contain the upper solids and a solution that contains more of the lower solids. did. A solution containing a large amount of solid matter after separation (VSS concentration of 30,000 mg / L) is once per day in five culture bottles for anaerobic digestion, 0.8 L, 0.4 L, and 0.26 L, respectively. , 0.2L, and 0.13L each. In order to keep the amount of sludge in the culture bottle constant, immediately before the treated organic sludge was introduced, the same amount of sludge was drawn out from the culture bottle. By the experiment operation of the charging and withdrawal, the residence time of the organic sludge in each culture bottle becomes 5, 10, 15, 20, and 30 days, respectively.
[0032]
On the other hand, a calcium carbonate solution was mixed with a solution containing no solid matter after separation of the treated sludge, and then stirred to precipitate phosphorus in the solution as calcium phosphate. Further, this was separated into a solid and a solution by centrifugation, and the separated solid was recovered as solid phosphorus.
[0033]
For comparison, the same experiment was performed on organic sludge that was subjected only to ultrasonic treatment, organic sludge that was subjected only to ozone treatment, and organic sludge that was not subjected to any treatment under exactly the same conditions.
[0034]
For these four types of sonication and ozone treatment, sonication only, ozone treatment only, and no treatment, a continuous experiment in which anaerobic digestion was carried out while performing a predetermined amount of injection and extraction was continued for 3 months. From the total VSS amount in the treated sludge and the total amount of VSS remaining undissolved, the proportion of solids digested by anaerobic digestion, that is, the VSS reduction rate was determined. In addition, the ratio of the total amount of digested gas generated to the total VSS amount of organic sludge charged into the culture bottle during this continuous experiment, that is, the digestive gas generation rate was determined. Furthermore, the ratio of the total amount of recovered phosphorus to the total amount of SS of organic sludge charged into the culture bottle during this continuous experiment, that is, the phosphorus recovery rate was determined.
[0035]
FIG. 4 shows the relationship between the residence time of the input organic sludge in the culture bottle and the VSS reduction rate. In FIG. 4, the data when untreated is the curve L1, the data when only the ultrasonic treatment is performed is the curve L2, the data when only the ozone treatment is performed is the curve L3, and the combined processing of the ultrasonic treatment and the ozone treatment is performed. The data in the case of performing is represented by a curve L4.
[0036]
As can be seen from FIG. 4, when untreated organic sludge was added, the solids were hardly reduced at a residence time of 10 days, and finally the VSS reduction rate was about 40% after a residence time of 30 days. In addition, when ultrasonic treatment or ozone treatment is added to the input organic sludge, the VSS reduction rate increases compared to the case where untreated organic sludge is added, and the VSS reduction rate at a residence time of 30 days is around 50%. It was. On the other hand, when the combined treatment in which the ozone treatment is further performed after the ultrasonic treatment is added to the organic sludge to be added, VSS reduction occurs actively even at a residence time of 5 days, and is about 80% high at a residence time of 20 days. A VSS reduction rate was obtained.
[0037]
Moreover, as shown in FIG. 5, the digestion gas generation rate during this experiment period is about 0.3 L / g-VSS for untreated, only about 0.4 L / g- for both ultrasonic treatment and ozone treatment alone. In contrast to VSS, in the case of combined treatment in which ozone treatment was performed after ultrasonic treatment, a high digestive gas generation rate of about 0.75 L / g-VSS was obtained.
[0038]
Furthermore, as shown in FIG. 6, the phosphorus recovery rate during this experimental period was almost zero when untreated, only sonication, and 5-7 mg-P / g-SS only with ozone treatment, In the case of combined treatment in which ozone treatment was performed after ultrasonic treatment, a high phosphorus recovery rate of about 30 mg-P / g-TS was obtained.
[0039]
From the results of this experiment, it is possible to digest organic sludge in a shorter time by using ultrasonic treatment and ozone treatment in combination with ultrasonic treatment alone or ozone treatment alone. It has been found that not only the generation rate of digestion gas that can be used as energy can be further increased, but also phosphorus in the organic sludge can be recovered at a higher yield.
[0040]
Experiment 3
In Experiment 2, the organic sludge is subjected to ultrasonic treatment, ozone treatment, or combined treatment of ultrasonic treatment and ozone treatment, and separated into a solution containing a lot of solids and a solution containing no solids, and the former is cultured. It was put into a bottle and phosphorus was recovered from the latter.
[0041]
In this experiment, ultrasonic treatment, ozone treatment, or combined treatment of ultrasonic treatment and ozone treatment is added to the digested sludge in the culture bottle. That is, while putting organic sludge into the culture bottle, a part of the digested sludge in the culture bottle was extracted, and the extracted digested sludge was subjected to ultrasonic treatment, ozone treatment, or combined treatment of ultrasonic treatment and ozone treatment. Thereafter, the solution is separated into a solid-rich solution and a solid-free solution, and the solid-rich solution is returned to the culture bottle. On the other hand, phosphorus is recovered from the solution containing no solid matter.
[0042]
As in Experiment 2, five culture bottles with an effective volume of 5.0 L were prepared, and 4.0 L of anaerobic digested sludge with a VSS concentration of about 17,000 mg / L was added to each, and anaerobic digestion was performed at 50 ° C. It was. In five culture bottles, organic sludge whose VSS concentration is adjusted to 17,000 mg / L is once a day, 0.8 L, 0.4 L, 0.26 L, 0.2 L, and 0.13 L respectively. I put it in. Moreover, in order to make the amount of sludge in the culture bottle constant, immediately before the organic sludge was introduced, the same amount of digested sludge as the amount to be introduced was extracted from the culture bottle. Due to the experimental operation of charging and withdrawal, the residence time of the organic sludge in each culture bottle is 5 days, 10 days, 15 days, 20 days, and 30 days, respectively.
[0043]
In this continuous digestion experiment, once a day, the same amount of digested sludge as the amount of the input organic sludge is withdrawn from the culture bottle, and each treatment of Experiment 1, that is, only ultrasonic treatment, only ozone treatment, or ultrasonic After the combined treatment of the treatment and the ozone treatment, the treated digested sludge was centrifuged and separated into a solution containing no solid matter and a solution containing a lot of solid matter. In order to keep the amount of sludge in the culture bottle constant, the solution containing a large amount of solid matter after separation was mixed with water degassed with oxygen to obtain the same amount as the amount withdrawn, and then returned to the culture bottle.
[0044]
On the other hand, a calcium carbonate solution was mixed with a solution containing no solid matter after centrifugation, and then stirred to precipitate phosphorus in the solution as calcium phosphate. Further, this was separated into a solid and a solution by centrifugation, and the separated solid was recovered as solid phosphorus.
[0045]
In addition, as a control experiment, the extracted digested sludge was centrifuged without any treatment, and a solution containing a large amount of solid matter after centrifugation was returned to the culture bottle and phosphorus was recovered from the solution containing no solid matter. It was.
[0046]
Such a continuous experiment was continued for 3 months, and the VSS reduction rate, digestion gas generation rate, and phosphorus recovery rate were obtained as in Experiment 2.
[0047]
In FIG. 7, the residence time of the input organic sludge in the culture bottle (the digested sludge of the same amount as that of the input organic sludge is extracted and treated, so it can also be said that the treated digested sludge stays in the culture bottle) And the VSS reduction rate. In FIG. 7, the data when unprocessed is the curve L1, the data when only the ultrasonic treatment is performed is the curve L2, the data when only the ozone treatment is performed is the curve L3, and the combined processing of the ultrasonic treatment and the ozone treatment is performed. The data in the case of performing is represented by a curve L4.
[0048]
As can be seen from FIG. 7, in the case of untreated, the organic solid matter was hardly reduced when the residence time was 10 days, and the VSS reduction rate was finally about 40% after the residence time of 30 days. In the case of ultrasonic treatment and ozone treatment, the VSS reduction rate increased compared to the case of no treatment, and the VSS reduction rate at a residence time of 30 days was around 60%. On the other hand, in the combined treatment in which ozone treatment is further performed after ultrasonic treatment, VSS reduction occurred actively even at a residence time of 5 days, and a high VSS reduction rate of 85% or more was obtained at a residence time of 20 days.
[0049]
Further, as shown in FIG. 8, the digestion gas generation rate during the experiment period is about 0.3 L / g-VSS when untreated, only about 0.5 L / g- when only ultrasonic treatment and ozone treatment are performed. In contrast to VSS, in the case of combined treatment in which ozone treatment was performed after ultrasonic treatment, a very high digestive gas generation rate of about 0.9 L / g-VSS was obtained.
[0050]
Furthermore, as shown in FIG. 9, the phosphorus recovery rate during this experimental period was almost zero when untreated, only about ultrasonic treatment, and about 7 mg-P / g-SS only with ozone treatment. In the case of combined treatment in which ozone treatment was performed after ultrasonic treatment, a high phosphorus recovery rate of about 33 mg-P / g-SS was obtained.
[0051]
Based on the results of this experiment, digestion of organic sludge was shortened compared to the case of ultrasonic treatment alone or ozone treatment alone by performing combined treatment of ultrasonic treatment with digested sludge drawn from the culture bottle, ie digester, and ozone treatment. It can be carried out in a time and VSS reduction rate can be increased, and it has been found that not only the generation of digestion gas that can be used as energy can be further increased, but also phosphorus in organic sludge can be recovered at a higher yield.
[0052]
By the way, in this experiment, no treatment was applied to the input organic sludge, and sonication and ozone treatment were added to the digested sludge extracted from the culture bottle, but the input organic sludge and the digested sludge extracted from the culture bottle were removed. The mixed sludge may be mixed and subjected to ultrasonic treatment or ozone treatment, or ultrasonic treatment, ozone treatment and centrifugation.
[0053]
Once a day, 0.8L, 0.4L, 0.26L, 0.2L, 0 so that the residence time of the organic sludge in the culture bottle is 5, 10, 15, 20, and 30 days. In this experiment in which 13 L of organic sludge is introduced, the same amount of digested sludge is extracted from the culture bottle and mixed with half of the organic sludge to be added, and this mixed sludge is subjected to ultrasonic treatment, ozone treatment, or ultrafiltration. When an experiment for adding sonication and ozone treatment was performed, results similar to those shown in FIGS. 7 to 9 were obtained. From this result, even if organic sludge and digested sludge are mixed and processed, the effects of reducing VSS, increasing digestion gas generation rate, and increasing phosphorus recovery rate are the same as when processing digested sludge. It turns out that it is obtained.
[0054]
Experiment 4
In Experiment 3, the digested sludge in the culture bottle was pulled out, and the extracted digested sludge was subjected to ultrasonic treatment, ozone treatment, or combined treatment of ultrasonic treatment and ozone treatment. On the other hand, in this experiment, the extracted digested sludge is separated into a solid and a solution, and ultrasonic treatment, ozone treatment, or combined treatment of ultrasonic treatment and ozone treatment is added to the concentrated digested sludge.
[0055]
As in Experiments 2 and 3, prepare 5 culture bottles with an effective volume of 5.0 L, and add 4.0 L of anaerobic digested sludge with a VSS concentration of about 17,000 mg / L to anaerobic at 50 ° C. Digestion was performed. In 5 culture bottles, organic sludge with VSS concentration adjusted to 17,000 mg / L is added once a day, 0.8L, 0.4L, 0.26L, 0.2L, 0.13L. did. Also, immediately before adding the organic sludge, extract the same amount of digested sludge as the input organic sludge from the culture bottle, leave it for 30 minutes to concentrate the solid, and add the solid rich solution and the solid Separated into free solution.
[0056]
Each treatment of Experiment 1, that is, ultrasonic treatment or ozone treatment, or combined treatment of ultrasonic treatment and ozone treatment was performed on the solution containing a large amount of solid matter. The conditions for each treatment were the same as in Experiment 1. Thereafter, the treated digested sludge was further centrifuged to separate it into a solution containing no solid matter and a solution containing a lot of solid matter. The solution containing a large amount of solid matter after centrifugation was returned to the culture bottle.
[0057]
In order to keep the amount of sludge in the culture bottle constant, the same amount of digested sludge was extracted from the culture bottle just before returning the solution containing a large amount of separated solids, and then returned.
[0058]
On the other hand, a calcium carbonate solution was mixed with a solution containing no solid matter after centrifugation, and then stirred to precipitate phosphorus in the solution as calcium phosphate. This was further separated into a solid and a solution by centrifugation, and the separated solid was recovered as solid phosphorus.
[0059]
In addition, as a control experiment, a solution containing a large amount of solid matter left for 30 minutes after extraction was centrifuged without any treatment, and the solution containing a large amount of solid matter after centrifugation was returned to the culture bottle to obtain a solution containing no solid matter. An experiment was also conducted to recover phosphorus from slag.
[0060]
Such a continuous experiment was continued for 3 months, and the VSS reduction rate, digestion gas generation rate, and phosphorus recovery rate were obtained as in Experiments 2 and 3.
[0061]
FIG. 10 shows the relationship between the residence time of the input organic sludge in the culture bottle and the VSS reduction rate. In FIG. 10, the data when untreated is the curve L1, the data when only the ultrasonic treatment is performed is the curve L2, the data when only the ozone treatment is performed is the curve L3, and the combined processing of the ultrasonic treatment and the ozone treatment is performed. The data in the case of performing is represented by a curve L4.
[0062]
As can be seen from FIG. 10, in the case of untreated, the organic solid matter was hardly reduced at the residence time of 10 days, and the VSS reduction rate was finally about 40% after the residence time of 30 days. In the case of ultrasonic treatment and ozone treatment, the VSS reduction rate increased compared to the case of no treatment, and the VSS reduction rate at a residence time of 30 days was around 60%. On the other hand, in the case of combined treatment in which ozone treatment is further performed after ultrasonic treatment, VSS reduction occurs actively even at a residence time of 5 days, and a very high VSS reduction rate of about 85% is obtained at a residence time of 20 days. It was.
[0063]
In addition, as shown in FIG. 11, the digestion gas generation rate during this experiment period is about 0.3 L / g-VSS when untreated, only 0.4 to 0.5 L / g when only ultrasonic treatment is performed, and only ozone treatment is performed. In contrast to -VSS, in the case of combined treatment in which ozone treatment was performed after ultrasonic treatment, a very high digestive gas generation rate of about 0.9 L / g-VSS was obtained.
[0064]
Furthermore, as shown in FIG. 12, the phosphorus recovery rate during this experimental period was almost zero when untreated, only sonication, and 7-9 mg-P / g-SS only with ozone treatment, In the case of combined treatment in which ozone treatment was performed after ultrasonic treatment, a high phosphorus recovery rate of about 30 mg-P / g-SS was obtained.
[0065]
From the results of this experiment, digested sludge extracted from the culture bottle, that is, digester, was concentrated and combined with ultrasonic treatment and ozone treatment, so that organic sludge was used compared to ultrasonic treatment alone or ozone treatment alone. Digestion can be performed in a shorter time, and the reduction rate of VSS can be increased, which not only increases the generation of digestion gas that can be used as energy, but also recovers phosphorus in organic sludge at a higher yield. I knew it was possible.
[0066]
Experiment 5
In the experiment 1, as a mechanical dispersion process, in addition to the ultrasonic process, a process of homogenizing, mill crushing, and jetting at a high pressure to collide with a processing tank wall was performed. In addition to ozone treatment, treatment with acid and treatment with alkali were carried out as chemical modification treatment. As the acid, sulfuric acid or hydrochloric acid was used, and the pH was adjusted to 2 to 4 and held for 5 to 30 minutes. On the other hand, in the alkali treatment, sodium hydroxide or potassium hydroxide was used and the pH was adjusted to 9 to 13 and held for 5 to 30 minutes. Furthermore, a combined treatment of these mechanical dispersion treatment and chemical modification treatment was also performed. Similar to Experiment 1, these treated sludges were mixed with digested sludges, digested in a digestive anaerobic state at 50 ° C., and changes in VSS concentration over time were examined.
[0067]
Further, the sludge immediately after each treatment was centrifuged, and the phosphorus concentration in the supernatant was measured.
[0068]
For each treatment and combinations thereof, Table 1 shows the reduction rate of VSS concentration over 15 days, and Table 2 shows the phosphorus elution concentration.
[0069]
[Table 1]

[0070]
[Table 2]

[0071]
From Table 1, the effect of reducing the VSS concentration when the mechanical dispersion treatment and the chemical modification treatment are used in combination is somewhat different depending on the combination of the mechanical treatment and the chemical treatment used together. However, when any of the treatments is combined, the reduction rate of the VSS concentration is larger than that of the mechanical treatment alone or the chemical treatment alone, and it is compared with the sum of the reduction rates of the VSS concentration in these single treatments. However, the reduction rate of the VSS concentration becomes larger. Therefore, the combination treatment in which the modification treatment is performed by a chemical method after the dispersion treatment by a mechanical method is not limited to the combination treatment in which the ozone treatment is performed after the ultrasonic treatment, and is extremely effective for improving the sludge solubility. I found out.
[0072]
Furthermore, from Table 2, the effect of phosphorus elution when the mechanical dispersion treatment and the chemical modification treatment are used in combination is somewhat different depending on the combination of the mechanical treatment and the chemical treatment used together. However, in the case of combining any of the treatments, the phosphorus elution concentration is higher than that of the mechanical treatment alone or the chemical treatment alone, and it is also compared with the sum of the reduction rates of the VSS concentration in these single treatments. The phosphorus elution concentration becomes larger. Therefore, the combination treatment in which the modification treatment is performed by the chemical method after the dispersion treatment by the mechanical method is not limited to the combination treatment in which the ozone treatment is performed after the ultrasonic treatment, but is also extremely effective for phosphorus elution. I understood it.
[0073]
Embodiment 1
Next, an organic waste liquid treatment apparatus according to the present invention and an organic waste liquid treatment method using the same will be described.
[0074]
FIG. 13 is a diagram showing a schematic configuration and a processing flow of an organic waste liquid processing apparatus according to an embodiment of the present invention.
[0075]
As shown in FIG. 13, an ultrasonic crushing treatment tank 9, an ozone treatment tank 11, and a solid-liquid separation tank 17 are provided between the anaerobic digestion tank 1 and the organic waste liquid introduction path 2. An ultrasonic crusher 30 is installed in the ultrasonic crushing treatment tank 9, and an ozone generator 31 is connected to the ozone treatment tank 11 through an ozone gas injection path 32. The ultrasonic crushing treatment tank 9 and the ozone treatment tank 11 are concentrated by the dispersed waste liquid discharge passage 10, the ozone treatment tank 11 and the solid-liquid separation tank 17 are treated by the treatment liquid discharge passage 18, and the solid-liquid separation tank 17 and the anaerobic digestion tank 1 are concentrated. The liquid introduction paths 19 are connected to each other. An organic waste liquid introduction pump 37 is installed in the organic waste liquid introduction path 2.
[0076]
Further, the solid-liquid separation tank 17 and the phosphorus recovery tank 24 are connected by a separation liquid discharge path 20, and the phosphorus recovery tank 24 is connected to the anaerobic digestion tank 1 through a phosphorus recovery post-liquid introduction path 26. . A flocculant introduction path 23 is connected to the separation liquid discharge path 20, and the other end of the flocculant introduction path 23 is connected to a flocculant holding tank 21. Further, a flocculant introduction pump 22 is installed in the flocculant introduction path 23. A phosphorus recovery path 25 is connected to the phosphorus recovery tank 24.
[0077]
Further, the anaerobic digestion tank 1 is connected to the solid / liquid separation tank 4 via the digested sludge discharge path 3, and the concentrated sludge discharge path 5 and the treated water discharge path 8 are connected to the solid / liquid separation tank 4. The concentrated sludge discharge path 5 branches into a sludge disposal path 6 and a sludge return path 7, and the sludge return path 7 is connected to the anaerobic digester 1. In addition, a digestion gas discharge path 36 is connected to the anaerobic digestion tank 1.
[0078]
Next, the operation of the processing apparatus of this embodiment will be described.
[0079]
The organic waste liquid introduction pump 37 is operated to introduce the organic sludge mixed with the first settling sludge and the excess sludge from the sewage treatment plant into the ultrasonic crushing treatment tank 9 from the organic waste liquid introduction path 2 as an organic waste liquid. The introduced organic sludge is processed by the ultrasonic crusher 30 in the ultrasonic crushing treatment tank 9 to disperse the solid substance in the sludge. The organic sludge after the dispersion treatment is sent to the ozone treatment tank 11 through the dispersion waste liquid discharge path 10, and the ozone gas generated by the ozone generator 31 is injected into the ozone treatment tank 11 through the ozone gas injection path 32, so that ozone of the organic sludge is obtained. Perform processing. That is, reforming treatment with ozone is added to the organic sludge after the dispersion treatment.
[0080]
This ozone-treated organic sludge is sent to the solid-liquid separation tank 17 through the treatment liquid discharge passage 18 and is separated into solid and solution in the solid-liquid separation tank 17. A solid substance is introduced into the anaerobic digester 1 from the concentrated liquid introduction channel 19 and the treated organic sludge is decomposed by microorganisms. On the other hand, a solution containing a large amount of phosphorus is sent to the phosphorus recovery tank 24 through the separation liquid discharge passage 20. At this time, the flocculant introduction pump 22 is operated to supply the calcium carbonate solution held in the flocculant holding tank 21 to the separation liquid discharge path 20 through the flocculant introduction path 23, and contain phosphorus containing the separation liquid discharge path 20. A calcium carbonate solution is introduced into the treated water. In the phosphorus recovery tank 24, the precipitated calcium phosphate is separated and extracted from the phosphorus recovery path 25, and a solution containing no phosphorus is introduced into the anaerobic digester 1 through the phosphorus recovery post-liquid introduction path 26.
[0081]
After digesting organic sludge with microorganisms in the anaerobic digestion tank 1, the sludge in the anaerobic digestion tank 1 is discharged from the digested sludge discharge passage 3, and separated into solids and solutions in the solid-liquid separation tank 4, and the solution is processed. From the water discharge path 8, solids are discharged from the concentrated sludge discharge path 5, respectively. In addition, the solid matter in the concentrated sludge discharge path 5 is returned to the anaerobic digester 1 via the sludge return path 7, and a part is discharged out of the system from the sludge disposal path 6. In addition, the digestion gas generated in the anaerobic digester 1 is discharged through the digestion gas discharge path 36.
[0082]
When ozone is reacted with organic sludge, the highly oxidative action of ozone modifies poorly soluble substances such as fibers and cell walls in the solid matter of organic sludge and is easily dissolved by sludge in the digestion tank. Can be converted to In addition, by performing dispersion treatment by ultrasonic crushing before ozone treatment, the contact efficiency between the injected ozone and solid matter is significantly higher than when only ozone treatment is carried out, and it is possible to efficiently dissolve hardly soluble substances. Solubility can be improved. In this way, when organic sludge modified with a poorly soluble substance by combined use of ultrasonic treatment and ozone treatment is introduced into an anaerobic digestion tank and subjected to microbial treatment, ultrasonic treatment alone or ozone treatment alone, Compared with the simple sum of these treatments, the amount of sludge dissolved and converted to methane can be greatly increased. Correspondingly, the amount of sludge to be disposed of can be greatly reduced.
[0083]
At the same time, decomposition of the cell wall proceeds by the strong oxidizing action of ozone, so that phosphorus contained in the solid matter of the organic sludge can be eluted with high efficiency into the solution outside the solid matter. By performing the dispersion treatment by ultrasonic crushing before the ozone treatment, the cell wall is further decomposed by the injected ozone, and the phosphorus elution amount can be increased more efficiently than when only the ozone treatment is performed. Furthermore, by solid-liquid separation of the sludge after the treatment, the phosphorus in the solution can be converted into solid phosphorus using a flocculant and can be recovered as reusable phosphorus.
[0084]
Therefore, the organic sludge introduced into the anaerobic digester is dispersed by ultrasonic treatment and then modified by ozone treatment, whereby energy and phosphorus simultaneous recovery type organic sludge can be processed more efficiently.
[0085]
In this embodiment, all of the organic sludge to be introduced into the anaerobic digestion tank has been subjected to ultrasonic treatment and ozone treatment. However, ultrasonic treatment and ozone treatment are performed on a part of the introduced organic sludge, and the rest are treated. You may make it introduce | transduce into an anaerobic digester without performing.
[0086]
Embodiment 2
An organic waste liquid processing apparatus and an organic waste liquid processing method using the same according to another embodiment of the present invention will be described.
[0087]
FIG. 14 is a diagram showing the outline of the configuration and the flow of processing of the organic waste liquid processing apparatus of the present embodiment, and the case where anaerobic digestion is performed in two tanks, an acid generation tank and a methane generation tank. Shows an example to which the present invention is applied.
[0088]
As shown in FIG. 14, an ultrasonic crushing treatment tank 9, an ozone treatment tank 11, and a solid-liquid separation tank 17 are provided between the acid generation tank 33 and the organic waste liquid introduction path 2. An ultrasonic crusher 30 is installed in the ultrasonic crushing treatment tank 9, and an ozone generator 31 is connected to the ozone treatment tank 11 through an ozone gas injection path 32. The ultrasonic crushing treatment tank 9 and the ozone treatment tank 11 are provided with the dispersion waste liquid discharge path 10, the ozone treatment tank 11 and the solid-liquid separation tank 17 are provided with the treatment liquid discharge path 18, and the solid-liquid separation tank 17 and the acid generation tank 33 are concentrated liquid. Each is connected by an introduction path 19. An organic waste liquid introduction pump 37 is installed in the organic waste liquid introduction path 2.
[0089]
Further, the solid-liquid separation tank 17 and the phosphorus recovery tank 24 are connected by a separation liquid discharge path 20, and the phosphorus recovery tank 24 is connected to the acid generation tank 33 via a phosphorus recovery post-liquid introduction path 26. A flocculant introduction path 23 is connected to the separation liquid discharge path 20, and the other end of the flocculant introduction path 23 is connected to a flocculant holding tank 21. Further, a flocculant introduction pump 22 is installed in the flocculant introduction path 23. A phosphorus recovery path 25 is connected to the phosphorus recovery tank 24.
[0090]
Further, a solid-liquid separation tank 4 is provided downstream of the acid generation tank 33 via the digested sludge discharge path 3, and the concentrated sludge discharge path 5 and the treated water discharge path 8 are connected to the solid-liquid separation tank 4. Yes. The concentrated sludge discharge path 5 branches into a sludge disposal path 6 and a sludge return path 7, and the sludge return path 7 is connected to an acid generation tank 33. Further, the treated water discharge path 8 is connected to the methane generation tank 13.
[0091]
A solid-liquid separation tank 15 is provided downstream of the methane generation tank 13 via a digested sludge discharge path 14, and a concentrated sludge discharge path 27 and a treated water discharge path 16 are connected to the solid-liquid separation tank 15. The concentrated sludge discharge path 27 branches into a sludge disposal path 34 and a sludge return path 35, and the sludge return path 35 is connected to the methane generation tank 13. In addition, a digestion gas discharge path 36 is connected to the methane generation tank 13.
[0092]
Next, the operation of the processing apparatus of this embodiment will be described.
[0093]
The organic waste liquid introduction pump 37 is operated to introduce the organic sludge mixed with the first settling sludge and the excess sludge from the sewage treatment plant into the ultrasonic crushing treatment tank 9 from the organic waste liquid introduction path 2 as an organic waste liquid. The introduced organic sludge is processed by the ultrasonic crusher 30 in the ultrasonic crushing treatment tank 9 to disperse the solid substance in the sludge. The organic sludge after the dispersion treatment is sent to the ozone treatment tank 11 through the dispersion waste liquid discharge path 10, and the ozone gas generated by the ozone generator 31 is injected into the ozone treatment tank 11 through the ozone gas injection path 32, so that ozone of the organic sludge is obtained. Perform processing. That is, reforming treatment with ozone is added to the organic sludge after the dispersion treatment.
[0094]
This ozone-treated organic sludge is sent to the solid-liquid separation tank 17 through the treatment liquid discharge passage 18 and is separated into solid and solution in the solid-liquid separation tank 17. A solid substance is introduced into the acid generation tank 33 from the concentrated liquid introduction path 19, and the treated organic sludge is dissolved by microorganisms. On the other hand, a solution containing a large amount of phosphorus is sent to the phosphorus recovery tank 24 through the separation liquid discharge path 20. At this time, the flocculant introduction pump 22 is operated to supply the calcium carbonate solution held in the flocculant holding tank 21 to the separation liquid discharge path 20 through the flocculant introduction path 23, and contain phosphorus containing the separation liquid discharge path 20. A calcium carbonate solution is introduced into the treated water. In the phosphorus recovery tank 24, the precipitated calcium phosphate is separated and pulled out from the phosphorus recovery path 25, and a solution containing no phosphorus is introduced into the acid generation tank 33 through the liquid recovery path 26 after phosphorus recovery.
[0095]
After organic sludge is dissolved by microorganisms in the acid generation tank 33, the sludge in the acid generation tank 33 is discharged from the digested sludge discharge path 3, and is separated into solids and solutions in the solid-liquid separation tank 4, and the solution is discharged into the treated water discharge path. 8 is introduced into the methane generation tank 13 and the solid matter is discharged from the concentrated sludge discharge passage 5. In addition, the solid matter in the concentrated sludge discharge path 5 is returned to the acid generation tank 33 via the sludge return path 7, and a part is discharged out of the system from the sludge disposal path 6.
[0096]
After the organic matter in the solution is converted into methane by the microorganisms in the methane generation tank 13, the sludge in the methane generation tank 13 is discharged from the digested sludge discharge path 14, and is separated into a solid and a solution in the solid-liquid separation tank 15. The solution is discharged from the treated water discharge path 16, and the solid is discharged from the concentrated sludge discharge path 27. In addition, the solid matter in the concentrated sludge discharge path 27 is returned to the methane generation tank 13 through the sludge return path 35 and a part thereof is discharged from the sludge disposal path 34 to the outside of the system. Further, the digestion gas generated in the methane generation tank 13 is discharged through the digestion gas discharge path 36.
[0097]
In this way, when ozone is reacted with organic sludge, it is easily dissolved by sludge in the acid generation by modifying hardly soluble substances such as fibers and cell walls in the solid matter of organic sludge by the strong oxidizing action of ozone. It can be converted into a readily soluble substance. In addition, by performing dispersion treatment by ultrasonic crushing before ozone treatment, the contact efficiency between the injected ozone and solid matter is significantly higher than in the case of ozone treatment alone, and dissolution of hardly soluble substances efficiently. Can be improved. As described above, when organic sludge having a poorly soluble substance modified by a combination of ultrasonic treatment and ozone treatment is introduced into an acid generation tank to perform microbial treatment, ultrasonic treatment alone or ozone treatment alone, and Compared with the simple sum of these treatments, the amount of organic sludge dissolved in the acid generator and the amount of methane converted in the methane generator can be greatly increased. Correspondingly, the amount of sludge to be disposed of can be greatly reduced.
[0098]
At the same time, decomposition of the cell wall proceeds by the strong oxidizing action of ozone, so that phosphorus contained in the solid matter of the organic sludge can be eluted with high efficiency into the solution outside the solid matter. By performing the dispersion treatment by ultrasonic crushing before the ozone treatment, the cell wall is further decomposed by the injected ozone, and the phosphorus elution amount can be increased more efficiently than when only the ozone treatment is performed. Furthermore, by solid-liquid separation of the sludge after the treatment, the phosphorus in the solution can be converted into solid phosphorus using a flocculant and can be recovered as reusable phosphorus.
[0099]
Therefore, the organic sludge introduced into the acid generation tank is dispersed by ultrasonic treatment and then modified by ozone treatment, so that energy and phosphorus simultaneous recovery type organic sludge can be processed more efficiently.
[0100]
In addition, as in the present embodiment, when anaerobic digestion is performed separately in a first acid generation tank and a second methane generation tank, dispersion and reforming treatment are performed on the organic sludge introduced into the acid generation tank. By improving the solubility, the UASB (upflow anaerobic sludge used for high-load anaerobic treatment is used as well as the conventional fluidized bed type and fixed bed type methane generating tanks as the latter methane generating tank. A blanket type methane production tank can be used, and high-speed methane production becomes possible.
[0101]
In this embodiment, all of the organic sludge to be introduced into the acid generation tank has been subjected to ultrasonic treatment and ozone treatment. However, ultrasonic treatment and ozone treatment are performed on a part of the organic sludge to be introduced, and the rest are treated. Instead, it may be introduced into the acid generation tank.
[0102]
Embodiment 3
An organic waste liquid processing apparatus and an organic waste liquid processing method using the same according to another embodiment of the present invention will be described.
[0103]
FIG. 15 is a diagram showing an outline of the configuration and processing flow of the organic waste liquid processing apparatus of the present embodiment.
[0104]
As shown in FIG. 15, an organic waste liquid introduction path 2 is connected to the anaerobic digester 1. A digested sludge extraction passage 47 is connected to the anaerobic digestion tank 1, and the other end of the digested sludge extraction passage 47 is connected to the ultrasonic crushing treatment tank 9 and the ozone treatment tank 11. An ultrasonic crusher 30 is installed in the ultrasonic crushing treatment tank 9, and an ozone generator 31 is connected to the ozone treatment tank 11 through an ozone gas injection path 32. The ultrasonic crushing treatment tank 9 and the ozone treatment tank 11 are concentrated by the dispersed waste liquid discharge passage 10, the ozone treatment tank 11 and the solid-liquid separation tank 17 are treated by the treatment liquid discharge passage 18, and the solid-liquid separation tank 17 and the anaerobic digestion tank 1 are concentrated. The liquid introduction paths 19 are connected to each other. An organic waste liquid introduction pump 37 is installed in the organic waste liquid introduction path 2, and a digested sludge extraction pump 38 is installed in the digested sludge extraction path 47.
[0105]
Further, the solid-liquid separation tank 17 and the phosphorus recovery tank 24 are connected by a separation liquid discharge path 20, and the phosphorus recovery tank 24 is connected to the anaerobic digestion tank 1 through a phosphorus recovery post-liquid introduction path 26. . A flocculant introduction path 23 is connected to the separation liquid discharge path 20, and the other end of the flocculant introduction path 23 is connected to a flocculant holding tank 21. Further, a flocculant introduction pump 22 is installed in the flocculant introduction path 23. A phosphorus recovery path 25 is connected to the phosphorus recovery tank 24.
[0106]
In addition, a solid-liquid separation tank 4 is connected to the anaerobic digestion tank 1 through a digested sludge discharge path 3, and a concentrated sludge discharge path 5 and a treated water discharge path 8 are connected to the solid-liquid separation tank 4. The concentrated sludge discharge path 5 branches into a sludge disposal path 6 and a sludge return path 7, and the sludge return path 7 is connected to the anaerobic digester 1. In addition, a digestion gas discharge path 36 is connected to the anaerobic digestion tank 1.
[0107]
Next, the operation of the processing apparatus of this embodiment will be described.
[0108]
The organic waste liquid introduction pump 37 is operated to introduce the organic sludge mixed with the first settling sludge and the excess sludge from the sewage treatment plant into the anaerobic digester 1 from the organic waste liquid introduction path 2 as an organic waste liquid. After digesting organic sludge with microorganisms in the anaerobic digestion tank 1, the sludge in the anaerobic digestion tank 1 is discharged from the digested sludge discharge passage 3 and separated into solids and solutions in the solid-liquid separation tank 4, and the solution is treated with treated water. From the discharge path 8, solids are discharged from the concentrated sludge discharge path 5, respectively. In addition, the solid matter in the concentrated sludge discharge path 5 is returned to the anaerobic digester 1 through the sludge return path 7 and a part is discharged out of the system from the sludge disposal path 6. Further, the digestion gas generated in the anaerobic digestion tank 1 is discharged through the digestion gas discharge path 36.
[0109]
In the process of anaerobic digestion, the digested sludge extraction pump 38 is operated to introduce the digested sludge from the anaerobic digester 1 into the ultrasonic crushing tank 9 through the digested sludge extraction path 47. The introduced digested sludge is processed by the ultrasonic crusher 30 to disperse the solid matter in the digested sludge. The digested sludge after the dispersion treatment is sent to the ozone treatment tank 11 through the dispersion waste liquid discharge path 10, and the ozone gas generated by the ozone generator 31 is injected into the ozone treatment tank 11 through the ozone gas injection path 32, and the digested sludge is treated with ozone. To do. That is, reforming treatment with ozone is added to the digested sludge after the dispersion treatment.
[0110]
The digested sludge after the ozone treatment is sent to the solid / liquid separation tank 17 through the treatment liquid discharge passage 18 and is separated into a solid and a solution in the solid / liquid separation tank 17. A solid substance is introduced into the anaerobic digestion tank 1 from the concentrated liquid introduction path 19, and the digested sludge treated with ozone is decomposed by microorganisms. On the other hand, a solution containing a large amount of phosphorus is sent to the phosphorus recovery tank 24 through the separation liquid discharge path 20. At this time, the flocculant introduction pump 22 is operated, the calcium carbonate solution held in the flocculant holding tank 21 is introduced into the separation liquid discharge path 20 via the flocculant introduction path 23, and phosphorus containing is passed through the separation liquid discharge path 20. The calcium carbonate solution is mixed with the treated water. In the phosphorus recovery tank 24, the precipitated calcium phosphate is separated and extracted from the phosphorus recovery path 25, and a solution containing no phosphorus is introduced into the anaerobic digester 1 through the phosphorus recovery post-liquid introduction path 26.
[0111]
In this way, when ozone is reacted with digested sludge, it is easily dissolved by sludge in the digestion tank, which modifies poorly soluble substances such as fibers and cell walls in the solid matter of digested sludge by the strong oxidizing action of ozone. It can be converted into a readily soluble substance. In addition, by performing dispersion treatment by ultrasonic crushing before ozone treatment, the contact efficiency between the injected ozone and solid matter is significantly higher than in the case of ozone treatment alone, and dissolution of hardly soluble substances efficiently. Can be improved. In this way, when digested sludge modified with a poorly soluble substance using ultrasonic treatment and ozone treatment in combination is introduced into an anaerobic digester and biologically treated, ultrasonic treatment alone or ozone treatment alone, and these Compared to the simple sum of the treatment, the amount of sludge dissolved and the amount converted to methane can be greatly increased. Correspondingly, the amount of sludge to be disposed of can be greatly reduced.
[0112]
At the same time, decomposition of the cell wall proceeds due to the strong oxidizing action of ozone, so that phosphorus contained in the solid matter of the digested sludge can be eluted with high efficiency into the solution outside the solid matter. By performing the dispersion treatment by ultrasonic crushing before the ozone treatment, the cell wall is further decomposed by the injected ozone, and the phosphorus elution amount can be increased more efficiently than when only the ozone treatment is performed. Furthermore, by solid-liquid separation of the sludge after the treatment, the phosphorus in the solution can be converted into solid phosphorus using a flocculant and can be recovered as reusable phosphorus.
[0113]
Therefore, by dispersing the digested sludge in the anaerobic digestion tank by ultrasonic treatment and then modifying it by ozone treatment, it becomes possible to more efficiently treat the energy and phosphorus simultaneous recovery type digested sludge.
[0114]
Further, in the digested sludge of the anaerobic digester, a large amount of hardly soluble substances that are difficult to dissolve by living organisms are accumulated. Therefore, as in the present embodiment, a part of the digested sludge is extracted from the anaerobic digester, and the solid matter in the extracted digested sludge is processed and converted into an easily soluble substance, thereby further effectively. Energy and phosphorus recovery can be promoted.
[0115]
Embodiment 4
An organic waste liquid treatment apparatus and an organic waste liquid treatment method using the same according to another embodiment of the present invention will be described.
[0116]
FIG. 16 is a diagram showing an outline of the configuration and the flow of processing of the organic waste liquid processing apparatus of the present embodiment, in the case where anaerobic digestion is performed in two tanks, an acid generation tank and a methane generation tank. Shows an example to which the present invention is applied.
[0117]
As shown in FIG. 16, the organic waste liquid introduction path 2 is connected to the acid generation tank 33. A digested sludge extraction passage 47 is connected to the acid generation tank 33, and an ultrasonic crushing treatment tank 9 and an ozone treatment tank 11 are provided downstream of the digested sludge extraction passage 47. An ultrasonic crusher 30 is installed in the ultrasonic crushing treatment tank 9, and an ozone generator 31 is connected to the ozone treatment tank 11 through an ozone gas injection path 32. The ultrasonic crushing treatment tank 9 and the ozone treatment tank 11 are provided with the dispersion waste liquid discharge path 10, the ozone treatment tank 11 and the solid-liquid separation tank 17 are provided with the treatment liquid discharge path 18, and the solid-liquid separation tank 17 and the acid generation tank 33 are concentrated liquid. Each is connected by an introduction path 19. An organic waste liquid introduction pump 37 is installed in the organic waste liquid introduction path 2, and a digested sludge extraction pump 38 is installed in the digested sludge extraction path 47.
[0118]
Further, the solid-liquid separation tank 17 and the phosphorus recovery tank 24 are connected by a separation liquid discharge path 20, and the phosphorus recovery tank 24 is connected to the acid generation tank 33 via a phosphorus recovery post-liquid introduction path 26. A flocculant introduction path 23 is connected to the separation liquid discharge path 20, and the other end of the flocculant introduction path 23 is connected to a flocculant holding tank 21. Further, a flocculant introduction pump 22 is installed in the flocculant introduction path 23. A phosphorus recovery path 25 is connected to the phosphorus recovery tank 24.
[0119]
Further, a solid-liquid separation tank 4 is provided downstream of the acid generation tank 33 via the digested sludge discharge path 3, and the concentrated sludge discharge path 5 and the treated water discharge path 8 are connected to the solid-liquid separation tank 4. . The concentrated sludge discharge path 5 branches into a sludge disposal path 6 and a sludge return path 7, and the sludge return path 7 is connected to an acid generation tank 33. On the other hand, the treated water discharge path 8 is connected to the methane generation tank 13.
[0120]
A solid-liquid separation tank 15 is provided downstream of the methane generation tank 13 via a digested sludge discharge path 14, and a concentrated sludge discharge path 27 and a treated water discharge path 16 are connected to the solid-liquid separation tank 15. The concentrated sludge discharge path 27 branches into a sludge disposal path 34 and a sludge return path 35, and the sludge return path 35 is connected to the methane generation tank 13. In addition, a digestion gas discharge path 36 is connected to the methane generation tank 13.
[0121]
Next, the operation of the processing apparatus of this embodiment will be described.
[0122]
The organic waste liquid introduction pump 37 is operated to introduce organic sludge, which is a mixture of primary sludge and excess sludge from the sewage treatment plant, into the acid generation tank 33 from the organic waste liquid introduction path 2 as an organic waste liquid. After the organic sludge is dissolved by microorganisms in the acid generation tank 33, the sludge in the acid generation tank 33 is discharged from the digested sludge discharge passage 3, and is separated into solids and solutions in the solid-liquid separation tank 4, and the solution is treated water discharge passage. 8 is introduced into the methane generation tank 13 and the solid matter is discharged from the concentrated sludge discharge passage 5. The solid matter in the concentrated sludge discharge path 5 is returned to the acid generation tank 33 via the sludge return path 7 and a part is discharged out of the system from the sludge disposal path 6.
[0123]
After the organic matter in the solution is converted into methane by the microorganisms in the methane generation tank 13, the sludge in the methane generation tank 13 is discharged from the digested sludge discharge path 14, and is separated into a solid and a solution in the solid-liquid separation tank 15. The solution is discharged from the treated water discharge path 16, and the solid matter is discharged from the concentrated sludge discharge path 27. In addition, the solid matter in the concentrated sludge discharge path 27 is returned to the methane generation tank 13 through the sludge return path 35 and a part thereof is discharged from the sludge disposal path 34 to the outside of the system. Further, the digestion gas generated in the methane generation tank 13 is discharged through the digestion gas discharge path 36.
[0124]
In this anaerobic digestion process, the digested sludge extraction pump 38 is operated, the digested sludge in the acid generation tank 33 is introduced into the ultrasonic crushing processing tank 9 through the digested sludge extraction path 47, and processed by the ultrasonic crusher 30. Disperse solid matter in digested sludge. The digested sludge after the dispersion treatment is introduced into the ozone treatment tank 11 through the dispersion waste liquid discharge passage 10, and at the same time, the ozone gas generated by the ozone generator 31 is injected into the ozone treatment tank 11 through the ozone gas injection passage 32, Perform ozone treatment. That is, reforming treatment with ozone is added to the digested sludge after the dispersion treatment.
[0125]
The digested sludge after the ozone treatment is sent to the solid / liquid separation tank 17 through the treatment liquid discharge passage 18 and is separated into a solid and a solution in the solid / liquid separation tank 17. A solid substance is introduced into the acid generation tank 33 from the concentrated liquid introduction path 19, and the digested sludge treated with ozone is dissolved by microorganisms. On the other hand, a solution containing a large amount of phosphorus is sent to the phosphorus recovery tank 24 through the separation liquid discharge path 20. At this time, the flocculant introduction pump 22 is operated, the calcium carbonate solution held in the flocculant holding tank 21 is introduced into the separation liquid discharge path 20 via the flocculant introduction path 23, and phosphorus containing is passed through the separation liquid discharge path 20. The calcium carbonate solution is mixed with the treated water. In the phosphorus recovery tank 24, the precipitated calcium phosphate is separated and extracted from the phosphorus recovery path 25, and a solution containing no phosphorus is introduced into the acid generation tank 33 through the liquid recovery path 26 after phosphorus recovery.
[0126]
As described above, when ozone is reacted with the digested sludge in the acid generation tank, the strong oxidizing action of ozone modifies hardly soluble substances such as fibers and cell walls in the solid matter of the digested sludge, It can be converted into an easily soluble substance that is easily dissolved by sludge. In addition, by performing dispersion treatment by ultrasonic crushing before ozone treatment, the contact efficiency between the injected ozone and solid matter is significantly higher than in the case of ozone treatment alone, and dissolution of hardly soluble substances efficiently. Can be improved. In this way, by introducing a digested sludge modified with a poorly soluble substance using an ultrasonic treatment and an ozone treatment together and biologically treating it, an ultrasonic treatment alone or an ozone treatment alone, Compared with the simple sum of these treatments, the amount of sludge dissolved in the acid generator and the amount of methane converted in the methane generator can be greatly increased.
[0127]
At the same time, decomposition of the cell wall proceeds due to the strong oxidizing action of ozone, so that phosphorus contained in the solid matter of the digested sludge can be eluted with high efficiency into the solution outside the solid matter. By performing the dispersion treatment by ultrasonic crushing before the ozone treatment, the cell wall is further decomposed by the injected ozone, and the phosphorus elution amount can be increased more efficiently than when only the ozone treatment is performed. Furthermore, by solid-liquid separation of the sludge after the treatment, the phosphorus in the solution can be converted into solid phosphorus using a flocculant and can be recovered as reusable phosphorus.
[0128]
Therefore, by dispersing the digested sludge in the acid generation tank by ultrasonic treatment and then modifying it by ozone treatment, more efficient organic sludge treatment with simultaneous recovery of energy and phosphorus can be performed.
[0129]
In addition, a large amount of hardly soluble substances that are difficult to dissolve by living organisms are accumulated in the digested sludge of the acid generation tank. Therefore, as in the present embodiment, a part of the digested sludge is extracted from the acid generation tank, and the solid material in the extracted digested sludge is processed and converted into a readily soluble material, thereby more effectively energy, It becomes possible to proceed with phosphorus recovery.
[0130]
In addition, in the case where anaerobic digestion is performed separately in the former acid generation tank and the latter methane generation tank as in this embodiment, the ozone treatment is performed after dispersing the digested sludge in the acid generation tank by ultrasonic treatment. The UASB (upward flow anaerobic) used for high load anaerobic treatment as well as the conventional fluidized bed type and fixed bed type methane generation tanks as a methane generation tank in the latter stage by improving the solubility by A sludge blanket) type methane production tank can be used, and high-speed methane production becomes possible.
[0131]
Embodiment 5
An organic waste liquid processing apparatus and organic waste liquid processing using the same according to another embodiment of the present invention will be described.
[0132]
FIG. 17 is a diagram showing an outline of the configuration and the flow of processing for the organic waste liquid processing apparatus of the present embodiment.
[0133]
As shown in FIG. 17, an organic waste liquid introduction path 2 is connected to the anaerobic digester 1. A solid-liquid separation tank 4 is connected to the anaerobic digestion tank 1 via a digested sludge discharge path 3, and a concentrated sludge discharge path 5 and a treated water discharge path 8 are connected to the solid-liquid separation tank 4. The concentrated sludge discharge path 5 branches into a sludge disposal path 6 and a sludge return path 7, and an ultrasonic crushing treatment tank 9 and an ozone treatment tank 11 are provided in the subsequent stage of the sludge return path 7. An ultrasonic crusher 30 is installed in the ultrasonic crushing treatment tank 9, and an ozone generator 31 is connected to the ozone treatment tank 11 through an ozone gas injection path 32. The ultrasonic crushing treatment tank 9 and the ozone treatment tank 11 are concentrated by the dispersed waste liquid discharge passage 10, the ozone treatment tank 11 and the solid-liquid separation tank 17 are treated by the treatment liquid discharge passage 18, and the solid-liquid separation tank 17 and the anaerobic digestion tank 1 are concentrated. The liquid introduction paths 19 are connected to each other. In addition, a digestion gas discharge path 36 is connected to the anaerobic digestion tank 1. An organic waste liquid introduction pump 37 is installed in the organic waste liquid introduction path 2, and a sludge return pump 46 is installed in the sludge return path 7.
[0134]
Further, the solid-liquid separation tank 17 and the phosphorus recovery tank 24 are connected by a separation liquid discharge path 20, and the phosphorus recovery tank 24 is connected to the anaerobic digestion tank 1 through a phosphorus recovery post-liquid introduction path 26. . A flocculant introduction path 23 is connected to the separation liquid discharge path 20, and the other end of the flocculant introduction path 23 is connected to a flocculant holding tank 21. Further, a flocculant introduction pump 22 is installed in the flocculant introduction path 23. A phosphorus recovery path 25 is connected to the phosphorus recovery tank 24.
[0135]
Next, the operation of the processing apparatus of this embodiment will be described.
[0136]
The organic waste liquid introduction pump 37 is operated to introduce the organic sludge mixed with the first settling sludge and the excess sludge from the sewage treatment plant into the anaerobic digester 1 from the organic waste liquid introduction path 2 as an organic waste liquid. After digesting the organic sludge with microorganisms in the anaerobic digestion tank 1, the sludge in the anaerobic digestion tank 1 is discharged from the digested sludge discharge passage 3 and separated into a solid and a solution in the solid-liquid separation tank 4. The solution is discharged from the treated water discharge path 8, and the solid matter is discharged from the concentrated sludge discharge path 5. Further, the digestion gas generated in the anaerobic digester 1 is discharged through the digestion gas discharge path 36.
[0137]
In this anaerobic digestion process, a part of the concentrated sludge in the concentrated sludge discharge passage 5 is discharged out of the system from the sludge disposal passage 6 and the sludge return pump 46 is operated to remove the concentrated sludge in the concentrated sludge discharge passage 5. A part is introduced into the ultrasonic crushing tank 9 through the sludge return path 7 and processed by the ultrasonic crusher 30 to disperse the solid matter in the concentrated sludge. The concentrated sludge after the dispersion treatment is sent to the ozone treatment tank 11 through the dispersion waste liquid discharge passage 10, and the ozone gas generated by the ozone generator 31 is injected into the ozone treatment tank 11 through the ozone gas injection passage 32, and the ozone treatment of the concentrated sludge is performed. To do. That is, a reforming treatment with ozone is added to the concentrated sludge after the dispersion treatment.
[0138]
The concentrated sludge after the ozone treatment is sent to the solid-liquid separation tank 17 through the ozone treatment liquid discharge passage 18 and is separated into a solid and a solution in the solid-liquid separation tank 17. Solids are introduced into the anaerobic digester 1 from the treatment waste liquid introduction path 19 and the ozone-treated concentrated sludge is decomposed by microorganisms. On the other hand, a solution containing a large amount of phosphorus is sent to the phosphorus recovery tank 24 through the phosphorus-containing treated water discharge passage 20. At this time, the flocculant introduction pump 22 is operated, and the calcium carbonate solution held in the flocculant holding tank 21 is supplied to and mixed with the phosphorus-containing treated water passing through the phosphorus-containing treated water discharge path 20. The calcium phosphate precipitated in the phosphorus recovery tank 24 is separated and pulled out from the phosphorus recovery path 25, and a solution containing no phosphorus is introduced into the anaerobic digester 1 through the post-recovery treated water introduction path 26.
[0139]
In this way, by applying ozone treatment to the concentrated sludge concentrated in the anaerobic digester, the poorly soluble substances such as fibers and cell walls in the solid matter of organic sludge are modified by the strong oxidizing action of ozone. However, it can be converted into an easily soluble substance that is easily dissolved by the sludge in the digestion tank. In addition, by performing dispersion treatment by ultrasonic crushing before ozone treatment, the contact efficiency between the injected ozone and solid matter is significantly higher than in the case of ozone treatment alone, and dissolution of hardly soluble substances efficiently. Can be improved. In the case of ultrasonic treatment alone or ozone treatment alone by introducing biologically treated concentrated sludge that has been modified with poorly soluble substances by using ultrasonic treatment and ozone treatment together in this way Compared with the simple sum of these treatments, the amount of sludge dissolved and converted to methane can be greatly increased.
[0140]
At the same time, decomposition of the cell wall proceeds due to the strong oxidizing action of ozone, so that phosphorus contained in the solid matter of the concentrated sludge can be eluted with high efficiency into the solution outside the solid matter. By performing the dispersion treatment by ultrasonic crushing before the ozone treatment, the cell wall is further decomposed by the injected ozone, and the phosphorus elution amount can be increased more efficiently than when only the ozone treatment is performed. Furthermore, by solid-liquid separation of the sludge after the treatment, the phosphorus in the solution can be converted into solid phosphorus using a flocculant and can be recovered as reusable phosphorus.
[0141]
Therefore, the concentrated sludge concentrated in the anaerobic digester is dispersed by ultrasonic treatment and then modified by ozone treatment, enabling more efficient treatment of concentrated sludge with simultaneous recovery of energy and phosphorus. Become.
[0142]
In addition, in the digested sludge of the anaerobic digester, a large amount of hardly soluble substances that are difficult to dissolve by organisms are accumulated. Therefore, as in the present embodiment, the sludge in the anaerobic digester is concentrated, and the solid matter in the concentrated digested sludge is processed to convert it into a readily soluble substance, so that energy and phosphorus can be effectively applied. It becomes possible to proceed with the collection.
[0143]
In this embodiment, all of the digested sludge to be returned to the anaerobic digestion tank has been subjected to ultrasonic treatment and ozone treatment. However, ultrasonic treatment and ozone treatment are performed on a part of the digested sludge to be returned, and the remaining portion. You may make it return to an anaerobic digester without processing.
[0144]
Embodiment 6
An organic waste liquid treatment apparatus and an organic waste liquid treatment method using the same according to another embodiment of the present invention will be described.
[0145]
FIG. 18 is a diagram showing the outline of the configuration and the flow of processing of the organic waste liquid processing apparatus of the present embodiment, in the case where anaerobic digestion is performed in two tanks, an acid generation tank and a methane generation tank. Shows an example to which the present invention is applied.
[0146]
As shown in FIG. 18, the organic waste liquid introduction path 2 is connected to the acid generation tank 33. A solid-liquid separation tank 4 is provided downstream of the acid generation tank 33 via the digested sludge discharge path 3, and the concentrated sludge discharge path 5 and the treated water discharge path 8 are connected to the solid-liquid separation tank 4. The concentrated sludge discharge path 5 branches into a sludge disposal path 6 and a sludge return path 7, and an ultrasonic crushing treatment tank 9 and an ozone treatment tank 11 are provided in the subsequent stage of the sludge return path 7. An ultrasonic crusher 30 is installed in the ultrasonic crushing treatment tank 9, and an ozone generator 31 is connected to the ozone treatment tank 11 through an ozone gas injection path 32. The ultrasonic crushing treatment tank 9 and the ozone treatment tank 11 are provided with the dispersion waste liquid discharge path 10, the ozone treatment tank 11 and the solid-liquid separation tank 17 are provided with the treatment liquid discharge path 18, and the solid-liquid separation tank 17 and the acid generation tank 33 are concentrated liquid. Each is connected by an introduction path 19. On the other hand, the treated water discharge path 8 is connected to the methane generation tank 13. An organic waste liquid introduction pump 37 is installed in the organic waste liquid introduction path 2, and a sludge return pump 46 is installed in the sludge return path 7.
[0147]
Further, the solid-liquid separation tank 17 and the phosphorus recovery tank 24 are connected by a separation liquid discharge path 20, and the phosphorus recovery tank 24 is connected to the acid generation tank 33 via a phosphorus recovery post-liquid introduction path 26. A flocculant introduction path 23 is connected to the separation liquid discharge path 20, and the other end of the flocculant introduction path 23 is connected to a flocculant holding tank 21. Further, a flocculant introduction pump 22 is installed in the flocculant introduction path 23. A phosphorus recovery path 25 is connected to the phosphorus recovery tank 24.
[0148]
A solid-liquid separation tank 15 is provided downstream of the methane generation tank 13 via a digested sludge discharge path 14, and a concentrated sludge discharge path 27 and a treated water discharge path 16 are connected to the solid-liquid separation tank 15. The concentrated sludge discharge path 27 branches into a sludge disposal path 34 and a sludge return path 35, and the sludge return path 35 is connected to the methane generation tank 13. In addition, a digestion gas discharge path 36 is connected to the methane generation tank 13.
[0149]
Next, the operation of the processing apparatus of this embodiment will be described.
[0150]
The organic waste liquid introduction pump 37 is operated to introduce organic sludge, which is a mixture of primary sludge and excess sludge from the sewage treatment plant, into the acid generation tank 33 from the organic waste liquid introduction path 2 as an organic waste liquid. After the organic sludge is dissolved by microorganisms in the acid generation tank 33, the sludge in the acid generation tank 33 is discharged from the digested sludge discharge path 3, and is separated into solid and solution in the solid-liquid separation tank 4. The solution is introduced into the methane generation tank 13 through the treated water discharge path 8, and the solid matter is discharged from the concentrated sludge discharge path 5.
[0151]
After the solution is converted to methane by microorganisms in the methane generation tank 13, the sludge in the methane generation tank 13 is discharged from the digested sludge discharge path 14, and is separated into a solid and a solution in the solid-liquid separation tank 15. The solution is discharged from the treated water discharge path 16, and the solid is discharged from the concentrated sludge discharge path 27. In addition, the solid matter in the concentrated sludge discharge path 27 is returned to the methane generation tank 13 through the sludge return path 35 and a part thereof is discharged from the sludge disposal path 34 to the outside of the system. In addition, the digestion gas generated in the methane generation tank 13 is discharged through the digestion gas discharge path 36.
[0152]
In this anaerobic digestion process, a part of the concentrated sludge in the concentrated sludge discharge passage 5 is discharged out of the system from the sludge disposal passage 6 and the sludge return pump 46 is operated to remove the concentrated sludge in the concentrated sludge discharge passage 5. A part is introduced into the ultrasonic crushing tank 9 through the sludge return path 7 and processed by the ultrasonic crusher 30 to disperse the solid matter in the concentrated sludge. The concentrated sludge after the dispersion treatment is sent to the ozone treatment tank 11 through the dispersion waste liquid discharge passage 10, and at the same time, the ozone gas generated by the ozone generator 31 is injected into the ozone treatment tank 11 through the ozone gas injection passage 32, and the concentrated sludge is discharged. Perform ozone treatment. That is, a reforming treatment with ozone is added to the concentrated sludge after the dispersion treatment.
[0153]
The concentrated sludge after the ozone treatment is sent to the solid-liquid separation tank 17 through the ozone treatment liquid discharge passage 18 and is separated into a solid and a solution in the solid-liquid separation tank 17. Solids are introduced into the acid generation tank 33 from the treatment waste liquid introduction path 19 and the ozone-treated concentrated sludge is decomposed by microorganisms. On the other hand, a solution containing a large amount of phosphorus is sent to the phosphorus recovery tank 24 through the phosphorus-containing treated water discharge passage 20. At this time, the flocculant introduction pump 22 is operated, and the calcium carbonate solution held in the flocculant holding tank 21 is supplied to and mixed with the phosphorus-containing treated water passing through the phosphorus-containing treated water discharge path 20. Calcium phosphate precipitated in the phosphorus recovery tank 24 is separated and pulled out from the phosphorus recovery path 25, and a solution containing no phosphorus is introduced into the acid generation tank 33 through the post-phosphorous recovered water introduction path 26.
[0154]
In this way, when ozone is reacted with the concentrated digested sludge, the strong oxidizing action of ozone modifies hardly soluble substances such as fibers and cell walls in the solid matter of the concentrated sludge, and the sludge in the acid generation tank It can be converted into a readily soluble substance that is easily dissolved. In addition, by performing dispersion treatment by ultrasonic crushing before ozone treatment, the contact efficiency between the injected ozone and solid matter is significantly higher than in the case of ozone treatment alone, and dissolution of hardly soluble substances efficiently. Can be improved. In this way, by introducing a digested sludge modified with a poorly soluble substance using an ultrasonic treatment and an ozone treatment together and biologically treating it, an ultrasonic treatment alone or an ozone treatment alone, Compared with the simple sum of these treatments, the amount of sludge dissolved in the acid generator and the amount of methane converted in the methane generator can be greatly increased.
[0155]
At the same time, decomposition of the cell wall proceeds due to the strong oxidizing action of ozone, so that phosphorus contained in the solid matter of the concentrated sludge can be eluted with high efficiency into the solution outside the solid matter. By performing the dispersion treatment by ultrasonic crushing before the ozone treatment, the cell wall is further decomposed by the injected ozone, and the phosphorus elution amount can be increased more efficiently than when only the ozone treatment is performed. Furthermore, by solid-liquid separation of the sludge after the treatment, the phosphorus in the solution can be converted into solid phosphorus using a flocculant and can be recovered as reusable phosphorus.
[0156]
Therefore, by dispersing the concentrated sludge obtained by concentrating the digested sludge in the acid generation tank by ultrasonic treatment and then reforming it by ozone treatment, it is possible to treat the energy and phosphorus simultaneous recovery type more efficiently. .
[0157]
In addition, as in this embodiment, when anaerobic digestion is performed separately in the former acid generation tank and the subsequent methane generation tank, the concentrated sludge in the concentrated acid generation tank is subjected to ozone treatment to improve the solubility. By promoting, not only the conventional fluidized bed type or fixed bed type methane generation tank as a methane generation tank in the latter stage, but also UASB (upflow anaerobic sludge blanket) type methane generation used for high load anaerobic treatment A tank can be used, and high-speed methane production becomes possible.
[0158]
Moreover, in the digested sludge of the tank which performs an acid production | generation, many hardly soluble substances which are hard to melt | dissolve by living organisms accumulate. Therefore, as in the present embodiment, by processing the solid matter in the concentrated digested sludge and converting it into an easily soluble substance, it becomes possible to more effectively advance energy and phosphorus recovery.
[0159]
In this embodiment, all the concentrated sludge to be returned to the acid generation tank has been subjected to ultrasonic treatment and ozone treatment, but the digested sludge to be returned is subjected to ultrasonic treatment and ozone treatment. You may return to an acid production tank, without processing.
[0160]
Embodiment 7
An organic waste liquid treatment apparatus and an organic waste liquid treatment method using the same according to another embodiment of the present invention will be described.
[0161]
FIG. 19 is a diagram showing an outline of the configuration and a processing flow of the organic waste liquid processing apparatus of the present embodiment.
[0162]
The processing apparatus of the present embodiment shown in FIG. 19 is the same as the processing apparatus of the first embodiment shown in FIG. 13, wherein a digested sludge extraction path 47 is connected to the anaerobic digestion tank 1. It is connected to the sonication tank 9. A digested sludge extraction pump 38 is installed in the digested sludge extraction path 47. The processing apparatus of the present embodiment has the same configuration as the processing apparatus of the first embodiment shown in FIG. 13 except that a digested sludge extraction passage 47 and a digested sludge extraction pump 38 are provided.
[0163]
Next, the operation of the processing apparatus of this embodiment will be described.
[0164]
As in the first embodiment, organic sludge from a sewage treatment plant is introduced as an organic waste liquid, and ultrasonic treatment is performed in the ultrasonic crushing treatment tank 9. At this time, in this embodiment, the anaerobic digestion tank 1 is used. The digested sludge is introduced into the ultrasonic crushing tank 9 through the digested sludge extraction passage 47. That is, the inflowing organic sludge and the digested sludge in the anaerobic digestion tank 1 are mixed, and the ultrasonic treatment is performed on the mixed sludge in the ultrasonic crushing treatment tank 9, and then the ozone treatment is performed in the ozone treatment tank 11. The subsequent operation is the same as in the first embodiment.
[0165]
In this way, when ozone is reacted with mixed sludge of organic sludge and digested sludge, the poorly soluble substances such as fibers and cell walls in the solid matter of the mixed sludge are modified by the strong oxidizing action of ozone, and the digester It can be converted into an easily soluble substance that is easily dissolved by the sludge inside. In addition, by performing dispersion treatment by ultrasonic crushing before ozone treatment, the contact efficiency between the injected ozone and solid matter is significantly higher than in the case of ozone treatment alone, and the dissolution of hardly soluble substances efficiently. Can be improved. In this way, when ultrasonic treatment and ozone treatment are used in combination to introduce a mixed sludge obtained by modifying a poorly soluble substance into an anaerobic digester and biological treatment, ultrasonic treatment alone or ozone treatment alone, and Compared with the simple sum of these treatments, the amount of sludge dissolved and the amount converted to methane can be greatly increased.
[0166]
At the same time, decomposition of the cell wall proceeds due to the strong oxidizing action of ozone, so that phosphorus contained in the solid matter of the mixed sludge can be eluted with high efficiency into the solution outside the solid matter. By performing the dispersion treatment by ultrasonic crushing before the ozone treatment, the cell wall is further decomposed by the injected ozone, and the phosphorus elution amount can be increased more efficiently than when only the ozone treatment is performed. Furthermore, by solid-liquid separation of the sludge after the treatment, the phosphorus in the solution can be converted into solid phosphorus using a flocculant and can be recovered as reusable phosphorus. Therefore, it is possible to treat mixed sludge of the energy and phosphorus simultaneous recovery type.
[0167]
In addition, in the case where a large amount of hardly soluble substances are contained in the solid matter of the inflowing organic waste liquid, as in this embodiment, the organic waste liquid containing a large amount of hardly soluble substances and the hardly soluble substance are used. By mixing the digested sludge with a large amount of accumulated solids, dispersing the solid material in the mixed sludge containing a large amount of these poorly soluble substances by ultrasonic treatment and modifying them by ozone treatment, it is possible to effectively prevent the poorly soluble substances. The amount of energy and phosphorus recovered from the organic waste liquid can be reduced compared with the case where the treatment is applied only to the inflowing organic waste liquid and the case where the treatment is applied only to the digested sludge of the anaerobic digester. While being able to increase significantly, the amount of sludge to be disposed of can be greatly reduced.
[0168]
Embodiment 8
An organic waste liquid treatment apparatus and an organic waste liquid treatment method using the same according to still another embodiment of the present invention will be described.
[0169]
FIG. 20 is a diagram showing an outline of the configuration and a processing flow of the organic waste liquid processing apparatus of the present embodiment.
[0170]
The processing apparatus of the present embodiment shown in FIG. 20 is the same as the processing apparatus of the second embodiment shown in FIG. 14 except that a digested sludge extraction path 47 is connected to the acid generation tank 33, and the digested sludge extraction path 47 is ultrasonic. It is connected to the crushing treatment tank 9. A digested sludge extraction pump 38 is installed in the digested sludge extraction path 47. The processing apparatus of the present embodiment has the same configuration as the processing apparatus of the second embodiment shown in FIG. 14 except that the digested sludge extraction passage 47 and the digested sludge extraction pump 38 are provided.
[0171]
Next, the operation of the processing apparatus of this embodiment will be described.
[0172]
As in the second embodiment, organic sludge from a sewage treatment plant is introduced as an organic waste liquid, and ultrasonic treatment is performed in the ultrasonic crushing treatment tank 9. At this time, in the present embodiment, in the acid generation tank 33. The digested sludge is introduced into the ultrasonic crushing tank 9 through the digested sludge extraction passage 47. That is, the inflowing organic sludge and the digested sludge in the acid generation tank 33 are mixed and subjected to ultrasonic crushing treatment in the ultrasonic crushing treatment tank 9 and then ozone treatment in the ozone treatment tank 11. The subsequent operation is the same as in the second embodiment.
[0173]
In this way, when ozone reacts with the mixed sludge of organic sludge and sludge in the acid generation tank, the strong oxidative action of ozone modifies the hardly soluble substances such as fibers and cell walls in the solid matter of the mixed sludge. It can be converted into an easily soluble substance that is easily dissolved by the sludge in the acid generation tank. In addition, by performing dispersion treatment by ultrasonic crushing before ozone treatment, the contact efficiency between the injected ozone and solid matter is significantly higher than in the case of ozone treatment alone, and the dissolution of hardly soluble substances efficiently. Can be improved. As described above, when the mixed sludge obtained by modifying the hardly soluble substance by using ultrasonic treatment and ozone treatment in combination is introduced into the acid generation tank and biologically treated, ultrasonic treatment alone or ozone treatment alone, and these Compared with the simple sum of these treatments, the amount of sludge dissolved in the acid generator and the amount of methane converted in the methane generator can be greatly increased.
[0174]
At the same time, decomposition of the cell wall proceeds due to the strong oxidizing action of ozone, so that phosphorus contained in the solid matter of the mixed sludge can be eluted with high efficiency into the solution outside the solid matter. By performing the dispersion treatment by ultrasonic crushing before the ozone treatment, the cell wall is further decomposed by the injected ozone, and the phosphorus elution amount can be increased more efficiently than when only the ozone treatment is performed. Furthermore, by solid-liquid separation of the sludge after the treatment, the phosphorus in the solution can be converted into solid phosphorus using a flocculant and can be recovered as reusable phosphorus. Therefore, it is possible to treat mixed sludge of the energy and phosphorus simultaneous recovery type.
[0175]
In addition, as in this embodiment, when anaerobic digestion is performed separately in the former acid generation tank and the latter methane generation tank, the organic sludge introduced into the acid generation tank or the ozone of the digestion sludge in the acid generation tank By promoting the solubility by performing the treatment, not only the conventional fluidized bed type or fixed bed type methane generating tank as the subsequent methane generating tank, but also UASB (upward flow anaerobic) used for high load anaerobic treatment A sludge blanket) type methane production tank can be used, and high-speed methane production becomes possible.
[0176]
In addition, in the case where a large amount of hardly soluble substances are contained in the solid matter of the inflowing organic waste liquid, as in this embodiment, the organic waste liquid containing a large amount of hardly soluble substances and the hardly soluble substance are used. By mixing the digested sludge in the acid generation tank where a large amount of water is accumulated, dispersing the solid material in the mixed sludge containing a large amount of hardly soluble substances by ultrasonic treatment and modifying it by ozone treatment, it is effective. Increases the solubility of difficult-to-dissolve substances, and the amount of energy recovered from the organic waste liquid compared to when processing only the inflowing organic waste liquid or when processing only the digested sludge in the acid generation tank As well as the amount of sludge to be disposed of can be greatly reduced.
[0177]
Embodiment 9
An organic waste liquid treatment apparatus and an organic waste liquid treatment method using the same according to another embodiment of the present invention will be described.
[0178]
FIG. 21 is a diagram showing an outline of the configuration and processing flow of the organic waste liquid processing apparatus of the present embodiment.
[0179]
In the processing apparatus of the present embodiment shown in FIG. 21, the sludge return path 7 is connected to the ultrasonic crushing tank 9 in the processing apparatus of the first embodiment shown in FIG. 13. Further, a sludge return pump 46 is installed in the sludge return path 7. The treatment apparatus of the present embodiment is the same as the treatment apparatus of the first embodiment shown in FIG. 13 except that the sludge return path 7 is connected to the ozone treatment tank 11 and the sludge return pump 46 is installed. It is a configuration.
[0180]
Next, the operation of the processing apparatus of this embodiment will be described.
[0181]
As in the first embodiment, the organic sludge from the sewage treatment plant is introduced as the organic waste liquid, and the ultrasonic treatment is performed in the ultrasonic crushing tank 9. At this time, in the present embodiment, the solid-liquid separation tank 4 is used. The concentrated concentrated sludge is introduced into the ultrasonic crushing tank 9 through the sludge return path 7. That is, the inflowing organic sludge and the concentrated sludge after solid-liquid separation are mixed, and the mixed sludge is subjected to ultrasonic crushing treatment in the ultrasonic crushing treatment tank 9 and then subjected to ozone treatment in the ozone treatment tank 11. Subsequent operations are the same as those in the first embodiment.
[0182]
In this way, when ozone is reacted with mixed sludge of organic sludge and concentrated sludge, the poorly soluble substances such as fibers and cell walls in the solid matter of the mixed sludge are modified by the strong oxidizing action of ozone, and digesters It can be converted into an easily soluble substance that is easily dissolved by the sludge inside. In addition, by performing dispersion treatment by ultrasonic crushing before ozone treatment, the contact efficiency between the injected ozone and solid matter is significantly higher than in the case of ozone treatment alone, and dissolution of hardly soluble substances efficiently. Can be improved. As described above, when organic sludge obtained by modifying a poorly soluble substance using ultrasonic treatment and ozone treatment is introduced into an anaerobic digester and biologically treated, ultrasonic treatment alone or ozone treatment alone, and Compared with the simple sum of these treatments, the amount of sludge dissolved and the amount converted to methane can be greatly increased.
[0183]
At the same time, decomposition of the cell wall proceeds due to the strong oxidizing action of ozone, so that phosphorus contained in the solid matter of the mixed sludge can be eluted with high efficiency into the solution outside the solid matter. By performing the dispersion treatment by ultrasonic crushing before the ozone treatment, the cell wall is further decomposed by the injected ozone, and the phosphorus elution amount can be increased more efficiently than when only the ozone treatment is performed. Furthermore, by solid-liquid separation of the sludge after the treatment, the phosphorus in the solution can be converted into solid phosphorus using a flocculant and can be recovered as reusable phosphorus. Therefore, energy and phosphorus simultaneous recovery type organic sludge can be processed.
[0184]
In addition, in the case where a large amount of hardly soluble substances are contained in the solid matter of the inflowing organic waste liquid, as in this embodiment, the organic waste liquid containing a large amount of hardly soluble substances and the hardly soluble substance are used. By mixing the sludge concentrated in the digested sludge that has accumulated a lot, and dispersing the solid material in the mixed sludge containing a lot of hardly soluble substances by ultrasonic treatment and modifying it by ozone treatment, it is effective Increases the solubility of difficult-to-dissolve substances, and the energy from the organic waste liquid is higher than when processing only the inflowing organic waste liquid or when processing only the concentrated sludge from the anaerobic digester. The amount recovered can be increased significantly, and the amount of sludge to be disposed of can be greatly reduced.
[0185]
Embodiment 10
An organic waste liquid treatment apparatus and an organic waste liquid treatment method using the same according to another embodiment of the present invention will be described.
[0186]
FIG. 22 is a diagram showing an outline of the configuration and a processing flow of the organic waste liquid processing apparatus of the present embodiment.
[0187]
In the processing apparatus of the present embodiment shown in FIG. 22, the sludge return path 7 is connected to the ultrasonic crushing tank 9 in the processing apparatus of the second embodiment shown in FIG. 14. Further, a sludge return pump 46 is installed in the sludge return path 7. The processing apparatus of the present embodiment is the same as the processing apparatus of the second embodiment shown in FIG. 14 except that the sludge return path 7 is connected to the ultrasonic crushing tank 9 and the sludge return pump 46 is installed. It is the composition.
[0188]
Next, the operation of the processing apparatus of this embodiment will be described.
[0189]
As in the second embodiment, the organic sludge in the sewage treatment plant is introduced as the organic waste liquid, and the ultrasonic treatment is performed in the ultrasonic crushing tank 9. At this time, in this embodiment, the acid generation tank 33 is used. The concentrated sludge concentrated in the subsequent solid-liquid separation tank 4 is introduced into the ultrasonic crushing tank 9 through the sludge return path 7. That is, the inflowing organic sludge and the concentrated sludge after solid-liquid separation are mixed, and the mixed sludge is subjected to ultrasonic crushing treatment in the ultrasonic crushing treatment tank 9 and then subjected to ozone treatment in the ozone treatment tank 11. Subsequent operations are the same as those in the second embodiment.
[0190]
In this way, when ozone is reacted with the mixed sludge of organic sludge and concentrated acid generation tank sludge, the strong oxidative action of ozone modifies poorly soluble substances such as fibers and cell walls in the solid matter of the mixed sludge. However, it can be converted into an easily soluble substance that is easily dissolved by the sludge in the acid generation tank. In addition, by performing dispersion treatment by ultrasonic crushing before ozone treatment, the contact efficiency between the injected ozone and solid matter is significantly higher than in the case of ozone treatment alone, and dissolution of hardly soluble substances efficiently. Can be improved. As described above, when the mixed sludge obtained by modifying the hardly soluble substance by using ultrasonic treatment and ozone treatment in combination is introduced into the acid generation tank and biologically treated, ultrasonic treatment alone or ozone treatment alone, and these Compared with the simple sum of these treatments, the amount of sludge dissolved in the acid generator and the amount of methane converted in the methane generator can be greatly increased.
[0191]
At the same time, decomposition of the cell wall proceeds due to the strong oxidizing action of ozone, so that phosphorus contained in the solid matter of the mixed sludge can be eluted with high efficiency into the solution outside the solid matter. By performing the dispersion treatment by ultrasonic crushing before the ozone treatment, the cell wall is further decomposed by the injected ozone, and the phosphorus elution amount can be increased more efficiently than when only the ozone treatment is performed. Furthermore, by solid-liquid separation of the sludge after the treatment, the phosphorus in the solution can be converted into solid phosphorus using a flocculant and can be recovered as reusable phosphorus. Therefore, energy and phosphorus simultaneous recovery type organic sludge can be processed.
[0192]
In addition, as in the present embodiment, when anaerobic digestion is performed separately in the former acid generation tank and the latter methane generation tank, the sludge in the acid generation tank is subjected to dispersion and reforming treatment to achieve solubility. By promoting, not only the conventional fluidized bed type or fixed bed type methane generation tank as a methane generation tank in the latter stage, but also UASB (upflow anaerobic sludge blanket) type methane generation used for high load anaerobic treatment A tank can be used, and high-speed methane production becomes possible.
[0193]
In addition, in the case where a large amount of hardly soluble substances are contained in the solid matter of the inflowing organic waste liquid, as in this embodiment, the organic waste liquid containing a large amount of hardly soluble substances and the hardly soluble substance are used. By mixing the digested sludge in the acid generation tank where a large amount of acid is accumulated, the solid material in the mixed sludge containing a large amount of these poorly soluble substances is dispersed by sonication and modified by ozone treatment to make it difficult to dissolve. Increases the solubility of the substance, and the amount of energy recovered from the organic waste liquid is higher than when the treatment is applied only to the inflowing organic waste liquid or only to the concentrated sludge from the acid generation tank. While being able to increase greatly, the amount of sludge which should be disposed can be reduced more significantly.
[0194]
Embodiment 11
An organic waste liquid treatment apparatus and an organic waste liquid treatment method using the same according to another embodiment of the present invention will be described.
[0195]
FIG. 23 is a diagram showing an outline of the configuration and a processing flow of the organic waste liquid processing apparatus of the present embodiment.
[0196]
The processing apparatus of the present embodiment shown in FIG. 23 is the processing apparatus of the third embodiment shown in FIG. 15, wherein an ORP meter 49 is installed in the anaerobic digestion tank 1, and is connected to the controller 52 via the signal line 51. It is connected. The controller 52 is connected to the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump 38 via a signal line 28, a signal line 53, and a signal line 39, respectively. The processing apparatus of the present embodiment has the same configuration as the processing apparatus of the third embodiment shown in FIG. 15 except for the ORP meter, the controller, and the signal line.
[0197]
Next, the operation of the processing apparatus of this embodiment will be described.
[0198]
Similarly to Embodiment 3, the organic waste liquid is introduced into the anaerobic digestion tank 1 and digested with microorganisms, and the digested sludge is extracted from the anaerobic digestion tank 1 and subjected to ultrasonic treatment and ozone treatment. At this time, in this embodiment, the anaerobic degree of the anaerobic digester 1 is measured by the ORP meter 49 and the measurement result is sent to the controller 52 through the signal line 51. The controller 52 compares the sent measurement result with a preset ORP value.
[0199]
If the measured value is within a preset range, it is determined that the operating state of the anaerobic digester 1 is good, and at least one of the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump 38 is used. For, change the treatment conditions to expand the digested sludge treatment. Expansion of digested sludge treatment is realized by increasing the output of the ultrasonic crusher 30. Further, it is realized by increasing the ozone generation amount in the ozone generator 31 and increasing the ozone injection amount. Furthermore, this is realized by increasing the flow rate of the digested sludge extraction pump 38 and increasing the amount of sludge to be processed. Of course, some or all of these may be combined.
[0200]
The changed processing conditions are transmitted to the ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 through the signal line 28, the signal line 53, or the signal line 39. The ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 that has received the changed processing conditions performs processing of the expanded digested sludge according to the conditions.
[0201]
On the other hand, when the measured value exceeds the preset range, it is determined that the operating state of the anaerobic digester 1 is poor, and at least the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump. About one of 38, processing conditions are changed so that processing of digested sludge may be reduced. Reduction of digested sludge treatment is realized by reducing the output of the ultrasonic crusher 30. Further, it is realized by reducing the ozone generation amount in the ozone generator 31 and reducing the ozone injection amount. Furthermore, it is realized by reducing the flow rate of the digested sludge extraction pump 38 and reducing the amount of sludge to be treated. Of course, some or all of these may be combined.
[0202]
The changed processing condition is transmitted to the ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 through the signal line 28, the signal line 53, or the signal line 39. The ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 that has received the changed processing conditions performs processing of the digested sludge reduced according to the conditions.
[0203]
Thus, by measuring the ORP of the anaerobic digester, it is possible to always and accurately grasp the influence of the dispersion process and the reforming process on the operating state of the anaerobic digester. Furthermore, the operation state of the anaerobic digester can be stably maintained by controlling the solid dispersion process and the organic modification process after the dispersion process based on the ORP measurement result. Therefore, compared with the case where measurement control is not performed, the solubility of the solid substance in digested sludge can be increased more stably. Here, “stable” means that the performance (dissolution of solid matter) can be maintained over a long period of time.
[0204]
This stable increase in solubility can improve the conversion rate of organic matter in digested sludge to methane more stably, and can also stably reduce the amount of sludge generated to be disposed of.
[0205]
In the present embodiment, ORP is measured as an indicator of the operating state of the anaerobic digester 1. However, the present invention is not limited to this as long as it is an indicator of the anaerobic degree of the anaerobic digester such as the dissolved oxygen concentration. Further, not only the anaerobic degree but also the digested sludge concentration and pH of the anaerobic digester, and the indicators related to the microbial activity of the digested sludge are measured, and the same effect is obtained. The microbial activity of the digested sludge can be measured, for example, by measuring the coenzyme (F420) of the methane fermentation microorganism with a fluorometer.
[0206]
Further, in the present embodiment, the case where the digested sludge of the anaerobic digester is dispersed and reformed is shown. However, when the organic waste liquid flowing in as in Embodiment 1 is dispersed and reformed, In the case where the concentrated sludge after solid-liquid separation is dispersed and reformed as in the fifth embodiment, in the case where the mixed sludge of organic waste liquid and digested sludge is dispersed and reformed as in the seventh embodiment, the ninth embodiment. In the case where the mixed sludge of the organic waste liquid and the concentrated sludge is dispersed and reformed as described above, the same effect can be obtained by performing the same measurement and control.
[0207]
Embodiment 12
An organic waste liquid treatment apparatus and an organic waste liquid treatment method using the same according to still another embodiment of the present invention will be described.
[0208]
FIG. 24 is a diagram showing an outline of the configuration and a processing flow of the organic waste liquid processing apparatus of the present embodiment.
[0209]
The processing apparatus of the present embodiment shown in FIG. 24 is the processing apparatus of the fourth embodiment shown in FIG. 16, and an ORP meter 49 is installed in the acid generation tank 33 and connected to the controller 52 via the signal line 51. Has been. The controller 52 is connected to the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump 38 via a signal line 28, a signal line 53, and a signal line 39, respectively. The processing apparatus of the present embodiment has the same configuration as the processing apparatus of the fourth embodiment shown in FIG. 15 except for the ORP meter, the controller, and the signal line.
[0210]
Next, the operation of the processing apparatus of this embodiment will be described.
[0211]
As in the fourth embodiment, the organic waste liquid is introduced into the acid generation tank 33 and the organic sludge is dissolved by the microorganisms, and the digested sludge in the acid generation tank 33 is extracted to perform ultrasonic treatment and ozone treatment. At this time, in the present embodiment, the anaerobic degree of the acid generation tank 33 is measured by the ORP meter 49, and the measurement result is sent to the controller 52 through the signal line 51. The controller 52 compares the sent measurement result with a preset ORP value.
[0212]
When the measured value is within the preset value range, it is determined that the operating state of the acid generation tank 33 is good, and at least one of the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump 38 is used. For one, change the treatment conditions to extend the treatment of digested sludge. The changed processing condition is transmitted to the ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 through the signal line 28, the signal line 53, or the signal line 39. The ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 that has received the changed processing conditions performs processing of the expanded digested sludge according to the conditions.
[0213]
On the other hand, when the measured value exceeds the preset range, it is determined that the operation state of the acid generation tank 33 is defective, and at least the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump 38 are determined. About one of these, processing conditions are changed so that the process of digested sludge may be reduced. The changed processing condition is transmitted to the ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 through the signal line 28, the signal line 53, or the signal line 39. The ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 that has received the changed processing conditions performs processing of the digested sludge reduced according to the conditions.
[0214]
Thus, by measuring the ORP of the acid generation tank, it is possible to always and accurately grasp the influence of the dispersion process and the modification process on the operation state of the acid generation tank. Furthermore, the operation state of the acid generation tank can be stably maintained by controlling the solid dispersion process and the organic modification process after the dispersion process based on the ORP measurement result. Therefore, compared with the case where measurement control is not performed, the solubility of the solid substance in the digested sludge of the acid generation tank can be increased more stably.
[0215]
This stable increase in solubility can improve the conversion rate of organic matter in the digested sludge of the acid generation tank to methane in the methane generation tank more stably, and also reduce the amount of sludge to be disposed of in a stable manner. It becomes possible.
[0216]
In the present embodiment, ORP is used as an indicator of the operating state of the acid generation tank 33, but the present invention is not limited to this as long as it is an indicator of the anaerobic degree of the acid generation tank such as the dissolved oxygen concentration. Moreover, the same effect can be obtained by measuring and controlling not only the anaerobic degree but also the digested sludge concentration in the acid generation tank, the anaerobic degree, and the microorganism activity of the digested sludge.
[0217]
Further, in the present embodiment, the case where the digested sludge in the acid generation tank is dispersed and reformed is shown. However, in the case where the organic waste liquid flowing in as in the second embodiment is dispersed and reformed, the embodiment is described. When the concentrated sludge after solid-liquid separation is dispersed and reformed as in 6, the mixed sludge of the organic waste liquid and the digested sludge in the acid generation tank is dispersed and reformed as in the eighth embodiment. Even when the mixed sludge of the organic waste liquid and the concentrated sludge from the acid generation tank is dispersed and reformed as in Form 10, the same effect can be obtained by performing the same measurement and control.
[0218]
Embodiment 13
An organic waste liquid treatment apparatus and an organic waste liquid treatment method using the same according to another embodiment of the present invention will be described.
[0219]
FIG. 25 is a diagram showing an outline of the configuration and a processing flow of the organic waste liquid processing apparatus of the present embodiment.
[0220]
The processing apparatus of the present embodiment shown in FIG. 25 is the same as the processing apparatus of the third embodiment shown in FIG. 15 except that the MLSS meter 45 is installed in the organic waste liquid introduction path 2 and the controller 52 is connected via the signal line 40. It is connected to the. The controller 52 is connected to the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump 38 via a signal line 28, a signal line 53, and a signal line 39, respectively. The processing apparatus of the present embodiment has the same configuration as the processing apparatus of the third embodiment shown in FIG. 15 except for the MLSS meter, the controller, and the signal line.
[0221]
Next, the operation of the processing apparatus of this embodiment will be described.
[0222]
Similarly to Embodiment 3, the organic waste liquid is introduced into the anaerobic digestion tank 1 and digested with microorganisms, and the digested sludge is extracted from the anaerobic digestion tank 1 to perform ultrasonic treatment and ozone treatment. At this time, in the present embodiment, the solids concentration of the waste liquid passing through the organic waste liquid introduction path 2 is measured by the MLSS meter 45, and the measurement result is sent to the controller 52 through the signal line 40. The controller 52 compares the sent measurement result with a preset MLSS concentration value.
[0223]
When the measured value is within a preset range, it is determined that the inflow load of the anaerobic digester 1 is appropriate and the operation state can be maintained well, and at least the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump About one of 38, processing conditions are changed so that processing of digested sludge may be expanded. The changed processing condition is transmitted to the ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 through the signal line 28, the signal line 53, or the signal line 39. The ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 that has received the changed processing conditions performs processing of the expanded digested sludge according to the conditions.
[0224]
On the other hand, if the measured value exceeds the preset range, it is determined that the inflow load of the anaerobic digester 1 is extremely high or extremely low, and the operating state cannot be maintained well, and at least the ultrasonic wave About one of the crusher 30, the ozone generator 31, and the digested sludge extraction pump 38, process conditions are changed so that the process of digested sludge may be reduced. The changed processing conditions are transmitted to the ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 through the signal line 28, the signal line 53, or the signal line 39, respectively. The ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 that has received the changed processing conditions performs processing of the digested sludge reduced according to the conditions.
[0225]
By measuring the MLSS concentration of the solid matter of the organic waste liquid flowing in in this way, the inflow load that affects the operating state of the anaerobic digester can be always and accurately grasped. Furthermore, by controlling the digestion sludge dispersion process and the modification process based on the measurement result of the MLSS concentration, the dispersion and the modification process can be performed while stably maintaining the operating state of the anaerobic digester. Therefore, compared with the case where measurement control is not performed, the solubility of the solid substance in digested sludge can be increased more stably.
[0226]
This stable increase in solubility can improve the conversion rate of organic matter in digested sludge to methane more stably, and can also stably reduce the amount of sludge generated to be disposed of. In addition, phosphorus elution from the digested sludge can be secured stably, so that the phosphorus recovery amount can be stably obtained.
[0227]
In this embodiment, the MLSS concentration is measured as an indicator of the solid matter concentration of the inflowing organic waste liquid. However, the present invention is not limited to this as long as it is an indicator of the solid matter concentration such as turbidity. In the present embodiment, the solid matter concentration is used as an index of the inflowing organic waste liquid. However, the present invention is not limited to this, and it is possible to measure and use an index related to the organic waste liquid such as pH and anaerobic degree. A similar effect can be obtained.
[0228]
Further, in the present embodiment, the case where the digested sludge of the anaerobic digester is dispersed and reformed is shown. However, when the organic waste liquid flowing in as in Embodiment 1 is dispersed and reformed, In the case where the concentrated sludge after solid-liquid separation is dispersed and reformed as in the fifth embodiment, in the case where the mixed sludge of organic waste liquid and digested sludge is dispersed and reformed as in the seventh embodiment, the ninth embodiment. In the case where the mixed sludge of the organic waste liquid and the concentrated sludge is dispersed and reformed as described above, the same effect can be obtained by performing the same measurement and control.
[0229]
Embodiment 14
An organic waste liquid treatment apparatus and an organic waste liquid treatment method using the same according to another embodiment of the present invention will be described.
[0230]
FIG. 26 is a diagram showing an outline of the configuration and a processing flow of the organic waste liquid processing apparatus of the present embodiment.
[0231]
The processing apparatus of the present embodiment shown in FIG. 26 is the same as the processing apparatus of the fourth embodiment shown in FIG. 16 except that the MLSS meter 45 is installed in the organic waste liquid introduction path 2 and is connected to the controller 52 via the signal line 40. It is connected. The controller 52 is connected to the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump 38 via a signal line 28, a signal line 53, and a signal line 39, respectively. The processing apparatus of the present embodiment has the same configuration as the processing apparatus of the fourth embodiment shown in FIG. 16 except for the MLSS meter, the controller, and the signal line.
[0232]
Next, the operation of the processing apparatus of this embodiment will be described.
[0233]
As in the fourth embodiment, the organic waste liquid is introduced into the acid generation tank 33 and the organic sludge is dissolved by the microorganisms, and the digested sludge in the acid generation tank 33 is extracted to perform ultrasonic treatment and ozone treatment. At this time, in the present embodiment, the solids concentration of the waste liquid passing through the organic waste liquid introduction path 2 is measured by the MLSS meter 45, and the measurement result is sent to the controller 52 through the signal line 40. The controller 52 compares the sent result with the preset MLSS concentration value.
[0234]
When the measured value is within a preset range, it is determined that the inflow load of the acid generation tank 33 is appropriate and the operation state can be maintained satisfactorily, and at least the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump 38 are determined. About one of these, processing conditions are changed so that processing of digested sludge may be expanded. The changed processing condition is transmitted to the ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 through the signal line 28, the signal line 53, or the signal line 39. The ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 that has received the changed processing conditions performs processing of the expanded digested sludge according to the conditions.
[0235]
On the other hand, when the measured value is out of the preset range, it is determined that the inflow load of the acid generation tank 33 is extremely high or extremely low, and the operation state cannot be satisfactorily maintained. The processing conditions of one of the ozone generator 31 and the digested sludge extraction pump 38 are changed so as to reduce the digested sludge processing. The changed processing condition is transmitted to the ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 through the signal line 28, the signal line 53, or the signal line 39. The ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump 38 that have received the processing conditions after the change process digested sludge reduced according to the conditions.
[0236]
In this way, by measuring the concentration of the solid matter in the inflow waste liquid, it is possible to always and accurately grasp the inflow load that affects the operation state of the acid generation tank. Furthermore, by controlling the dispersion treatment and the modification treatment of the digested sludge based on the measured solid concentration, the dispersion treatment and the modification treatment can be performed while stably maintaining the operation state of the acid generation tank. Therefore, compared with the case where measurement control is not performed, the solubility of the solid substance in digested sludge can be increased more stably.
[0237]
This stable increase in solubility can improve the conversion rate of organic matter in the digested sludge of the acid generation tank to methane in the methane generation tank more stably, and also reduce the amount of sludge to be disposed of in a stable manner. It becomes possible. In addition, phosphorus elution from the digested sludge can be secured stably, so that the phosphorus recovery amount can be stably obtained.
[0238]
In this embodiment, the MLSS concentration is measured as an indicator of the solid matter concentration of the inflowing organic waste liquid. However, the present invention is not limited to this as long as it is an indicator of the solid matter concentration such as turbidity. Moreover, the same effect can be obtained not only by the solid concentration but also by measuring and controlling an index related to organic waste liquid such as pH and anaerobic degree.
[0239]
Further, in the present embodiment, the case where the digested sludge in the acid generation tank is dispersed and reformed is shown. However, in the case where the organic waste liquid flowing in as in the second embodiment is dispersed and reformed, the embodiment is described. When the concentrated sludge after solid-liquid separation is dispersed and reformed as in 6, the mixed sludge of the organic waste liquid and the digested sludge in the acid generation tank is dispersed and reformed as in the eighth embodiment. Even when the mixed sludge of the organic waste liquid and the concentrated sludge from the acid generation tank is dispersed and reformed as in Form 10, the same effect can be obtained by performing the same measurement and control.
[0240]
Embodiment 15
An organic waste liquid treatment apparatus and an organic waste liquid treatment method using the same according to another embodiment of the present invention will be described.
[0241]
FIG. 27 is a diagram showing an outline of the configuration and processing flow of the organic waste liquid processing apparatus of the present embodiment.
[0242]
The processing apparatus of the present embodiment shown in FIG. 27 is the same as the processing apparatus of the third embodiment shown in FIG. 15 except that the ultrasonic crushing treatment tank 9 has an MLSS densitometer 41 and the ozone treatment tank 11 has an ORP meter 42. Are connected to the controller 52 via the signal line 43 and the signal line 44, respectively. The controller 52 is connected to the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump 38 via a signal line 28, a signal line 53, and a signal line 39, respectively. The processing apparatus of the present embodiment has the same configuration as the processing apparatus of the third embodiment shown in FIG. 15 except for the MLSS meter, the ORP meter, the controller, and the signal line.
[0243]
Next, the operation of the processing apparatus of this embodiment will be described.
[0244]
Similarly to Embodiment 3, the organic waste liquid is introduced into the anaerobic digestion tank 1 and digested with microorganisms, and the digested sludge is extracted from the anaerobic digestion tank 1 and subjected to ultrasonic treatment and ozone treatment. At this time, in the present embodiment, the solid matter concentration in the ultrasonic crushing treatment tank 9 is measured with the MLSS densitometer 41, and the anaerobic degree of the ozone treatment tank 11 is measured with the ORP meter 42. 43, and sent to the controller 52 through the signal line 44. The controller 52 compares the sent result with the preset MLSS concentration and ORP value.
[0245]
When the measured values of MLSS and ORP are both within the preset range, it is determined that the treatment in the ultrasonic crushing treatment tank 9 and the ozone treatment tank 11 is appropriate and the treatment state is well maintained, and digested sludge Is set to at least one of the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump 38, and the signal line 28, the signal line 53, or the signal line 39 is set. Communicate through. The ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 that has received the processing conditions performs the processing of the digested sludge for maintenance according to the conditions. That is, the controller 52 instructs the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump 38 to continue the operation under the current processing conditions.
[0246]
On the other hand, when the MLSS measurement value is out of the preset range or the ORP measurement value is out of the preset range, the processing in the ultrasonic crushing treatment tank 9 or the ozone treatment tank 11 is performed. Is not sufficient, and at least one of the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump 38 is changed so that the digested sludge treatment is expanded. The changed condition is transmitted to the ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 through the signal line 28, the signal line 53, or the signal line 39. The ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 that has received the changed processing conditions performs processing of the expanded digested sludge according to the conditions.
[0247]
Thus, by measuring the solid matter concentration in the ultrasonic crushing treatment tank 9 and the anaerobic index of the ozone treatment tank 11, the state of treatment in each tank can be always and accurately grasped. Furthermore, by controlling the dispersion treatment and reforming treatment of the digested sludge based on these measurement results, the dispersion and reforming treatment can be performed while keeping the treatment state in each treatment tank stable. Therefore, compared with the case where measurement control is not performed, the solubility of the solid substance in digested sludge can be increased more stably.
[0248]
This stable increase in solubility can improve the conversion rate of organic matter in digested sludge to methane more stably, and can also stably reduce the amount of sludge generated to be disposed of. In addition, phosphorus elution from the digested sludge can be secured stably, so that the phosphorus recovery amount can be stably obtained.
[0249]
In the present embodiment, the MLSS concentration of digested sludge is measured as the solid matter concentration in the ultrasonic crushing treatment tank, but is not limited to this as long as it is an indicator of the solid matter concentration such as turbidity. Moreover, the same effect is acquired even if it measures and controls the index regarding processed digested sludge, such as pH of an ultrasonic crushing processing tank, anaerobic degree, and the microbial activity of digested sludge not only in solid substance concentration.
[0250]
In the present embodiment, ORP is used as an anaerobic index of the ozone treatment tank, but the present invention is not limited to this as long as it is an anaerobic index such as a dissolved oxygen concentration. Further, not only the anaerobic degree, but also the same effect can be obtained by measuring and controlling the index regarding the treated digested sludge such as the pH of the ozone treatment tank, the digested sludge concentration, the microbial activity of the digested sludge.
[0251]
Moreover, although the example which performs measurement control simultaneously about the digested sludge of both an ultrasonic crushing processing tank and an ozone processing tank was shown in this Embodiment, measurement control is performed about either an ultrasonic crushing processing tank or an ozone processing tank. You may do it.
[0252]
Further, in the present embodiment, the case where the digested sludge in the anaerobic digester is dispersed and reformed is shown, but when the organic waste liquid flowing in as in Embodiment 1 is dispersed and reformed, When the concentrated sludge after solid-liquid separation is dispersed and reformed as in the fifth embodiment, the mixed sludge of organic waste liquid and digested sludge is dispersed and reformed as in the seventh embodiment. Even when the mixed sludge of organic waste liquid and concentrated sludge is dispersed and reformed as in 9, the same effect can be obtained by performing the same measurement and control.
[0253]
Embodiment 16
An organic waste liquid treatment apparatus and an organic waste liquid treatment method using the same according to another embodiment of the present invention will be described.
[0254]
FIG. 28 is a diagram showing an outline of the configuration and a processing flow of the organic waste liquid processing apparatus of the present embodiment.
[0255]
The processing apparatus of the present embodiment shown in FIG. 28 is the same as the processing apparatus of the fourth embodiment shown in FIG. 16, but the ultrasonic crushing treatment tank 9 has an MLSS densitometer 41 and the ozone treatment tank 11 has an ORP meter 42. Are connected to the controller 52 via the signal line 43 and the signal line 44, respectively. The controller 52 is connected to the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump 38 via a signal line 28, a signal line 53, and a signal line 39, respectively. The processing apparatus of the present embodiment has the same configuration as the processing apparatus of the fourth embodiment shown in FIG. 16 except for the MLSS meter, the ORP meter, the controller, and the signal line.
[0256]
Next, the operation of the processing apparatus of this embodiment will be described.
[0257]
As in the fourth embodiment, the organic waste liquid is introduced into the acid generation tank 33 and the organic sludge is dissolved by the microorganisms, and the digested sludge in the acid generation tank 33 is extracted to perform ultrasonic treatment and ozone treatment. At this time, in the present embodiment, the solid matter concentration in the ultrasonic crushing treatment tank 9 is measured with the MLSS densitometer 41, and the anaerobic degree of the ozone treatment tank 11 is measured with the ORP meter 42, and these measurement results are respectively signaled. The data is sent to the controller 52 through the line 43 and the signal line 44. The controller 52 compares the sent measurement result with the preset MLSS concentration and ORP value.
[0258]
When the measured values of MLSS and ORP are both within the preset range, it is determined that the treatment in the ultrasonic crushing treatment tank 9 and the ozone treatment tank 11 is appropriate and the treatment state is well maintained, and digested sludge Conditions are maintained and the conditions are transmitted to at least one of the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump 38 through the signal line 28, the signal line 53, or the signal line 39. . In the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump 38 that have received the processing conditions, the digested sludge is processed for maintenance in accordance with the conditions. That is, the controller 52 instructs the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump 38 to continue the operation under the current processing conditions.
[0259]
On the other hand, when the MLSS measurement value exceeds the preset range, or the ORP measurement value falls below the preset range, the processing in the ultrasonic crushing treatment tank 9 or the ozone treatment tank 11 is performed. It judges that it is inadequate, and changes process conditions so that the process of digested sludge may be extended about at least one of the ultrasonic crusher 30, the ozone generator 31, and the digested sludge extraction pump 38. FIG. The changed processing condition is transmitted to the ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 through the signal line 28, the signal line 53, or the signal line 39. The ultrasonic crusher 30, the ozone generator 31, or the digested sludge extraction pump 38 that has received the changed processing conditions performs processing of the expanded digested sludge according to the conditions.
[0260]
Thus, by measuring the solid matter concentration in the ultrasonic crushing treatment tank 9 and the anaerobic index of the ozone treatment tank 11, the state of treatment in each tank can be always and accurately grasped. Furthermore, by controlling the dispersion treatment and reforming treatment of digested sludge based on these measurement results, it is possible to stably carry out the dispersion and modification treatment while always maintaining the treatment state in each treatment tank in an appropriate state. it can. Therefore, compared with the case where measurement control is not performed, the solubility of the solid substance in digested sludge can be increased more stably.
[0261]
This stable increase in solubility can improve the conversion rate of organic matter in the digested sludge of the acid generation tank to methane in the methane generation tank more stably, and also reduce the amount of sludge to be disposed of in a stable manner. It becomes possible. In addition, phosphorus elution from the digested sludge can be secured stably, so that the phosphorus recovery amount can be stably obtained.
[0262]
In the present embodiment, the MLSS concentration of digested sludge is measured as the solid matter concentration in the ultrasonic crushing treatment tank, but is not limited to this as long as it is an indicator of the solid matter concentration such as turbidity. Moreover, the same effect is acquired even if it measures and controls the index regarding processed digested sludge, such as pH of an ultrasonic crushing processing tank, anaerobic degree, and the microbial activity of digested sludge not only in solid substance concentration.
[0263]
In the present embodiment, ORP is used as an anaerobic index of the ozone treatment tank, but the present invention is not limited to this as long as it is an anaerobic index such as a dissolved oxygen concentration. Further, not only the anaerobic degree, but also the same effect can be obtained by measuring and controlling the index regarding the treated digested sludge such as the pH of the ozone treatment tank, the digested sludge concentration, the microbial activity of the digested sludge.
[0264]
Moreover, although the example which performs measurement control simultaneously about the digested sludge of both an ultrasonic crushing processing tank and an ozone processing tank was shown in this Embodiment, measurement control is performed about either an ultrasonic crushing processing tank or an ozone processing tank. You may do it.
[0265]
Further, in the present embodiment, the case where the digested sludge in the acid generation tank is dispersed and reformed is shown, but when the organic waste liquid flowing in as in Embodiment 2 is dispersed and reformed, In the case where the concentrated sludge after solid-liquid separation is dispersed and reformed as in the sixth embodiment, in the case where the mixed sludge of organic waste liquid and digested sludge is dispersed and reformed as in the eighth embodiment, the tenth embodiment. In the case where the mixed sludge of the organic waste liquid and the concentrated sludge is dispersed and reformed as described above, the same effect can be obtained by performing the same measurement and control.
[0266]
Embodiment 17
An organic waste liquid treatment apparatus and an organic waste liquid treatment method using the same according to another embodiment of the present invention will be described.
[0267]
FIG. 29 is a diagram showing an outline of the configuration and processing flow of the organic waste liquid processing apparatus of the present embodiment.
[0268]
The processing apparatus of the present embodiment shown in FIG. 29 is the same as the processing apparatus of the first embodiment shown in FIG. 13 except that a phosphoric acid concentration meter 48 is installed in the separation liquid discharge path 20 and a controller 52 is connected via a signal line 54. It is connected to the. The controller 52 is connected to the ultrasonic crusher 30 and the ozone generator 31 via a signal line 28 and a signal line 53, respectively. The processing apparatus of the present embodiment has the same configuration as the processing apparatus of the thirteenth embodiment shown in FIG. 5 except for the phosphate concentration meter, the controller, and the signal line.
[0269]
Next, the operation of the processing apparatus of this embodiment will be described.
[0270]
Similarly to Embodiment 1, the organic sludge is subjected to ozone treatment, separated into solids and solutions in the solid-liquid separation tank 17, and the solids are introduced into the anaerobic digestion tank 1 for digestion. On the other hand, a solution containing a large amount of phosphorus is sent to the phosphorus recovery tank 24, a calcium carbonate solution is introduced, and the precipitated calcium phosphate is extracted from the phosphorus recovery path 25. At this time, in the present embodiment, the phosphoric acid concentration of the solution containing a large amount of phosphorus passing through the separation liquid discharge path 20 is measured by the phosphoric acid concentration meter 48, and the measurement result is sent to the controller 52 through the signal line 54. The controller 52 compares the sent measurement result with a preset phosphoric acid concentration value.
[0271]
If the measured value is within the preset range, it is judged that phosphorus elution from organic sludge is good and that phosphorus recovery from organic sludge is well maintained, and ozone treatment of inflowing organic sludge should be maintained. This condition is set, and the condition is transmitted to at least one of the ultrasonic crusher 30 and the ozone generator 31 through the signal line 28 or the signal line 53. In the ultrasonic crusher 30 and the ozone generator 31 that have received the processing conditions, the digested sludge is processed for maintenance in accordance with the conditions. That is, the controller 52 instructs the ultrasonic crusher 30 and the ozone generator 31 to continue the operation under the current processing conditions.
[0272]
On the other hand, when the measured value falls below the preset range, it is determined that phosphorus elution from organic sludge is low and phosphorus recovery is insufficient, and at least one of the ultrasonic crusher 30 and the ozone generator 31 is used. For one, change the treatment conditions to extend the treatment of digested sludge. The changed processing conditions are transmitted to the ultrasonic crusher 30 or the ozone generator 31 through the signal line 28 or the signal line 53. The ultrasonic crusher 30 or the ozone generator 31 that has received the changed processing conditions performs processing of the digested sludge expanded according to the conditions.
[0273]
In this way, the phosphoric acid concentration of the solution after ozone treatment and solid-liquid separation is measured, and by controlling the dispersion treatment and reforming treatment of organic sludge based on this measurement result, phosphorus elution from organic sludge is stably secured. it can. Therefore, the amount of phosphorus recovered from organic sludge can be maintained more stably than when measurement control is not performed.
[0274]
In the present embodiment, the phosphoric acid concentration is measured as an indicator of phosphorus in the solution after ozone treatment and solid-liquid separation. However, the present invention is not limited to this as long as it is an indicator of phosphorus such as the total phosphorus concentration.
[0275]
Further, in the present embodiment, the case where the digested sludge in the anaerobic digester is dispersed and reformed is shown, but when the organic waste liquid flowing in as in Embodiment 1 is dispersed and reformed, When the concentrated sludge after solid-liquid separation is dispersed and reformed as in the fifth embodiment, the mixed sludge of organic waste liquid and digested sludge is dispersed and reformed as in the seventh embodiment. Even when the mixed sludge of organic waste liquid and concentrated sludge is dispersed and reformed as in 9, the same effect can be obtained by performing the same measurement and control.
[0276]
Embodiment 18
An organic waste liquid treatment apparatus and an organic waste liquid treatment method using the same according to another embodiment of the present invention will be described.
[0277]
FIG. 30 is a diagram showing an outline of the configuration and a processing flow of the organic waste liquid processing apparatus of the present embodiment.
[0278]
The processing apparatus of the present embodiment shown in FIG. 30 is the same as the processing apparatus of the second embodiment shown in FIG. 14 except that a phosphate concentration meter 48 is installed in the separation liquid discharge path 20 and the controller 52 is connected via a signal line 54. It is connected to the. The controller 52 is connected to the ultrasonic crusher 30 and the ozone generator 31 via a signal line 28 and a signal line 53, respectively. The processing apparatus of the present embodiment has the same configuration as the processing apparatus of the second embodiment shown in FIG. 14 except for the phosphate concentration meter, the controller, and the signal line.
[0279]
Next, the operation of the processing apparatus of this embodiment will be described.
[0280]
Similarly to Embodiment 2, the organic sludge is subjected to ozone treatment, separated into a solid and a solution in the solid-liquid separation tank 17, and the solid is introduced into the acid generation tank 33 and dissolved. On the other hand, a solution containing a large amount of phosphorus is sent to the phosphorus recovery tank 24, a calcium carbonate solution is introduced, and the precipitated calcium phosphate is extracted from the phosphorus recovery path 25. At this time, in the present embodiment, the phosphoric acid concentration of the solution containing a large amount of phosphorus passing through the separation liquid discharge path 20 is measured by the phosphoric acid concentration meter 48, and the measurement result is sent to the controller 52 through the signal line 54. The controller 52 compares the sent measurement result with a preset phosphoric acid concentration value.
[0281]
If the measured value is within the preset range, it is judged that phosphorus elution from organic sludge is good and that phosphorus recovery from organic sludge is well maintained, and ozone treatment of inflowing organic sludge should be maintained. This condition is set, and the condition is transmitted to at least one of the ultrasonic crusher 30 and the ozone generator 31 through the signal line 28 or the signal line 53. In the ultrasonic crusher 30 and the ozone generator 31 that have received the processing conditions, the digested sludge is processed for maintenance in accordance with the conditions. That is, the controller 52 instructs the ultrasonic crusher 30 and the ozone generator 31 to continue the operation under the current processing conditions.
[0282]
On the other hand, when the measured value falls below the preset range, it is determined that phosphorus elution from organic sludge is low and phosphorus recovery is insufficient, and at least one of the ultrasonic crusher 30 and the ozone generator 31 is used. For one, change the treatment conditions to extend the treatment of digested sludge. The changed processing conditions are transmitted to the ultrasonic crusher 30 or the ozone generator 31 through the signal line 28 or the signal line 53. The ultrasonic crusher 30 or the ozone generator 31 that has received the changed processing conditions performs processing of the digested sludge expanded according to the conditions.
[0283]
Thus, by measuring the phosphoric acid concentration of the solution after ozone treatment and solid-liquid separation, and controlling the ozone treatment of the organic sludge based on the measurement result, phosphorus elution from the organic sludge can be secured stably. Therefore, the amount of phosphorus recovered from organic sludge can be maintained more stably than when measurement control is not performed.
[0284]
In the present embodiment, the phosphoric acid concentration is measured as an indicator of phosphorus in the solution after ozone treatment and solid-liquid separation. However, the present invention is not limited to this as long as it is an indicator of phosphorus such as the total phosphorus concentration.
[0285]
Further, in the present embodiment, the case where the digested sludge in the acid generation tank is dispersed and reformed is shown, but when the organic waste liquid flowing in as in Embodiment 2 is dispersed and reformed, In the case where the concentrated sludge after solid-liquid separation is dispersed and reformed as in the sixth embodiment, in the case where the mixed sludge of organic waste liquid and digested sludge is dispersed and reformed as in the eighth embodiment, the tenth embodiment. In the case where the mixed sludge of the organic waste liquid and the concentrated sludge is dispersed and reformed as described above, the same effect can be obtained by performing the same measurement and control.
[0286]
Embodiment 19
An organic waste liquid treatment apparatus and an organic waste liquid treatment method using the same according to another embodiment of the present invention will be described.
[0287]
FIG. 31 is a diagram showing an outline of the configuration and processing flow of the organic waste liquid processing apparatus of the present embodiment.
[0288]
The processing apparatus of the present embodiment shown in FIG. 31 is the same as the processing apparatus of the first embodiment shown in FIG. 13 except that a phosphoric acid concentration meter 48 is installed in the separation liquid discharge path 20 and the controller 52 is connected via a signal line 54. It is connected to the. The controller 52 is connected to the flocculant introduction pump 22 via a signal line 55. The processing apparatus of the present embodiment has the same configuration as the processing apparatus of the first embodiment shown in FIG. 13 except for the phosphate concentration meter, the controller, and the signal line.
[0289]
Next, the operation of the processing apparatus of this embodiment will be described.
[0290]
Similarly to Embodiment 1, the organic sludge is subjected to ozone treatment, separated into solids and solutions in the solid-liquid separation tank 17, and the solids are introduced into the anaerobic digestion tank 1 for digestion. On the other hand, a solution containing a large amount of phosphorus is sent to the phosphorus recovery tank 24, a calcium carbonate solution is introduced, and the precipitated calcium phosphate is extracted from the phosphorus recovery path 25. At this time, in the present embodiment, the phosphoric acid concentration of the solution containing a large amount of phosphorus passing through the separation liquid discharge path 20 is measured by the phosphoric acid concentration meter 48, and the measurement result is sent to the controller 52 through the signal line 54. The controller 52 calculates the amount of calcium carbonate necessary for precipitating phosphorus in the solution from the measurement results sent, and changes the flow rate of the flocculant introduction pump 22 through the signal line 55 so as to ensure this amount.
[0291]
In this way, the phosphoric acid concentration of the solution after ozone treatment and solid-liquid separation is measured, and by controlling the amount of flocculant added based on the measurement result, almost all the phosphorus in the solution does not remain in the solution. It can be recovered as calcium phosphate and can avoid overdosing of the flocculant. Therefore, the amount of phosphorus recovered from the organic sludge can be obtained more efficiently and reliably than when measurement control is not performed.
[0292]
In the present embodiment, the phosphoric acid concentration is measured as an indicator of phosphorus in the solution after ozone treatment and solid-liquid separation. However, the present invention is not limited to this as long as it is an indicator of phosphorus such as the total phosphorus concentration.
[0293]
Moreover, although the case where the organic sludge which flows in in this Embodiment is ozone-treated was shown, when the digestive sludge of an anaerobic digester is ozone-treated like Embodiment 3, it is solid-liquid like Embodiment 5. When the concentrated sludge after separation is ozone treated, the mixed sludge of organic sludge and digested sludge is ozone treated as in Embodiment 7, and the mixed sludge of organic sludge and concentrated sludge is ozone treated as in Embodiment 9. Even in this case, the same effect can be obtained by performing the same measurement and control.
[0294]
Embodiment 20
An organic waste liquid treatment apparatus and an organic waste liquid treatment method using the same according to another embodiment of the present invention will be described.
[0295]
FIG. 32 is a diagram showing an outline of the configuration and the processing flow of the organic waste liquid processing apparatus of the present embodiment.
[0296]
The processing apparatus of the present embodiment shown in FIG. 32 is the same as the processing apparatus of the second embodiment shown in FIG. 14 except that a phosphate concentration meter 48 is installed in the separation liquid discharge path 20 and the controller 52 is connected via a signal line 54. It is connected to the. The controller 52 is connected to the flocculant introduction pump 22 via a signal line 55. The processing apparatus of the present embodiment has the same configuration as the processing apparatus of the second embodiment shown in FIG. 14 except for the phosphate concentration meter, the controller, and the signal line.
[0297]
Next, the operation of the processing apparatus of this embodiment will be described.
[0298]
Similarly to Embodiment 2, the organic sludge is subjected to ozone treatment, separated into a solid and a solution in the solid-liquid separation tank 17, and the solid is introduced into the acid generation tank 33 and dissolved. On the other hand, a solution containing a large amount of phosphorus is sent to the phosphorus recovery tank 24, a calcium carbonate solution is introduced, and the precipitated calcium phosphate is extracted from the phosphorus recovery path 25. At this time, in the present embodiment, the phosphoric acid concentration of the solution containing a large amount of phosphorus passing through the separation liquid discharge path 20 is measured by the phosphoric acid concentration meter 48, and the measurement result is sent to the controller 52 through the signal line 54. The controller 52 calculates the amount of calcium carbonate necessary for precipitating phosphorus in the solution from the measurement results sent, and changes the flow rate of the flocculant introduction pump 22 through the signal line 55 so as to ensure this amount.
[0299]
In this way, the phosphoric acid concentration of the solution after ozone treatment and solid-liquid separation is measured, and by controlling the amount of flocculant added based on the measurement result, almost all the phosphorus in the solution does not remain in the solution. It can be recovered as calcium phosphate and can avoid overdosing of the flocculant. Therefore, the amount of phosphorus recovered from the organic sludge can be obtained more efficiently and reliably than when measurement control is not performed.
[0300]
In the present embodiment, the phosphoric acid concentration is measured as an indicator of phosphorus in the solution after ozone treatment and solid-liquid separation. However, the present invention is not limited to this as long as it is an indicator of phosphorus such as the total phosphorus concentration.
[0301]
Further, in the present embodiment, the case where the organic sludge that flows in is treated with ozone is shown. However, when the digested sludge in the acid generation tank is treated with ozone as in the fourth embodiment, solid-liquid separation is performed as in the sixth embodiment. When the subsequent sludge is ozone treated, the mixed sludge of organic sludge and digested sludge is ozone treated as in the eighth embodiment, and the mixed sludge of organic sludge and concentrated sludge is ozone treated as in the tenth embodiment. Even in this case, the same effect can be obtained by performing the same measurement and control.
[0302]
Embodiment 21
In Embodiments 1 to 20, ultrasonic treatment was shown as a method for dispersing organic sludge, digested sludge and concentrated sludge, and ozone treatment was shown as a method for modifying these sludge after dispersion. It is not limited. As the dispersion treatment method, homogenization, mill crushing, collision by high pressure injection, roller, fuse press, pressurization, decompression, Waring blender can be used. Also, the modification treatment methods include acid addition, alkali addition, surfactant addition, hydrogen peroxide addition, ultraviolet irradiation, heating, high voltage pulse, thermal plasma, hydrothermal reaction treatment such as using supercritical water and subcritical water. Even if it is used, the same or better effect can be obtained.
[0303]
Embodiment 22
In Embodiments 1 to 20, calcium carbonate is used as a flocculant for the recovery of eluted phosphorus, but the present invention is not limited to this, and the same effect can be obtained even with substances containing other calcium such as calcium hydrogen carbonate. A general flocculant such as (polyaluminum chloride) may be used. In the above-described embodiment, the flocculant is used as a method for recovering eluted phosphorus. However, the present invention is not limited to this, and another phosphorus solidification method such as a crystallization method may be used.
[0304]
Further, in these embodiments, the liquid after phosphorus recovery is returned to the anaerobic digestion tank using the post-phosphorus recovery post-treatment water introduction path 26, but the present invention is not limited to this, and the liquid after phosphorus recovery is anaerobic. A separate process may be performed without returning to the digester.
[0305]
Embodiment 23
In the experiment and the embodiment, the organic sludge mixed with the primary sludge of the sewage treatment plant and the excess sludge was used as the organic waste liquid. However, the present invention is not limited to this, and the primary sludge and excess sludge of the sewage treatment plant are used. The same or higher effects can be obtained for sludge, waste, and waste liquid with high organic matter concentration, such as food waste, food residue, livestock manure, human waste, factory waste liquid, and mixtures thereof.
[0306]
【The invention's effect】
According to the organic waste liquid treatment method and apparatus of the present invention, the solid waste in the organic waste liquid is subjected to a dispersion treatment or a modification by performing a treatment that combines the dispersion treatment and the modified organic matter after the dispersion. There is an effect that the solubility of the solid matter in the influent waste liquid can be increased as compared with the single treatment of the quality treatment. This increase in solubility makes it possible to further improve the conversion rate of organic matter into methane in the influent wastewater, and to further reduce the amount of sludge generated to be disposed of, while at the same time reducing the phosphorus contained in the solid matter. Can be eluted with high efficiency out of the solid matter.
[0307]
This increase in solubility can improve the conversion rate of the organic matter in the influent waste liquid into methane and reduce the amount of sludge to be disposed of. At the same time, phosphorus, which is a limited resource, can be efficiently recovered by high-efficiency elution of phosphorus out of the solid.
[0308]
In addition, according to the present invention, digestion sludge in a tank that performs anaerobic digestion is performed by performing a process that combines a dispersion process and a modification process of organic matter after dispersion, or in a tank that performs anaerobic digestion. The sludge is separated into solid and liquid, and the solid matter in the digested sludge after solid-liquid separation is treated by combining the dispersion treatment and the organic matter modification treatment after the dispersion, thereby allowing the dispersion treatment or the modification treatment alone. Compared with the treatment, there is an effect that the solubility of the solid matter remaining without being dissolved in the anaerobic digestion can be increased, and at the same time, phosphorus contained in the solid matter can be eluted out of the solid matter with high efficiency.
[0309]
In particular, digested sludge from tanks that perform anaerobic digestion and solids after solid-liquid separation contain a large amount of hardly soluble substances that are difficult to dissolve by living organisms. By performing a combination treatment of the dispersion treatment and the modification treatment on the solid matter after the solid sludge separation of the digested sludge, the increase in solubility of the hardly soluble substance can be promoted.
[0310]
This increase in solubility can improve the conversion rate of organic matter in the influent waste liquid to methane and further reduce the amount of sludge to be disposed of. At the same time, phosphorus, which is a limited resource, can be recovered more efficiently by high-efficiency elution of phosphorus out of the solid.
[0311]
Further, according to the present invention, the digested sludge of the tank for anaerobic digestion and the influent waste liquid are mixed, or the digested sludge of the tank for anaerobic digestion is solid-liquid separated, and the digested sludge and the influent waste liquid after separation are separated. Compared with the single treatment of the dispersion treatment or the modification treatment, the solid matter in the mixed solution is subjected to a treatment that combines the dispersion treatment and the modification treatment of the organic matter after the dispersion. It is possible to increase the solubility of the solid that remains without being dissolved during digestion, and at the same time, it is possible to elute phosphorus contained in the solid out of the solid with high efficiency.
[0312]
In particular, when the inflowing waste liquid contains a lot of hardly soluble substances, the digested sludge from the tank that performs anaerobic digestion that contains a lot of hardly soluble substances, or the digested sludge after the solid-liquid separation. By mixing them together and treating them simultaneously, it is possible to further promote the increase in solubility of the hardly soluble substance.
[0313]
This increase in solubility can improve the conversion rate of organic matter in the influent waste liquid to methane and further reduce the amount of sludge to be disposed of. At the same time, phosphorus, which is a limited resource, can be recovered more efficiently by high-efficiency elution of phosphorus out of the solid.
[Brief description of the drawings]
FIG. 1 is a graph showing the relationship between elapsed time and VSS concentration in the organic waste liquid treatment method of the present invention.
FIG. 2 is a graph showing the relationship between elapsed time and digestion gas generation amount in the organic waste liquid treatment method of the present invention.
FIG. 3 is a graph showing the concentration of eluted phosphorus in the organic waste liquid treatment method of the present invention.
FIG. 4 is a graph showing the relationship between residence time and VSS reduction rate in the organic waste liquid treatment method of the present invention.
FIG. 5 is a graph showing digestion gas generation rates for the organic waste liquid treatment method of the present invention.
FIG. 6 is a graph showing phosphorus recovery rates for the organic waste liquid treatment method of the present invention.
FIG. 7 is a graph showing the relationship between residence time and VSS reduction rate in the organic waste liquid treatment method of the present invention.
FIG. 8 is a diagram showing the digestion gas generation rate for the organic waste liquid treatment method of the present invention.
FIG. 9 is a graph showing phosphorus recovery rates for the organic waste liquid treatment method of the present invention.
FIG. 10 is a graph showing the relationship between residence time and VSS reduction rate for the organic waste liquid treatment method of the present invention.
FIG. 11 is a diagram showing the digestion gas generation rate for the organic waste liquid treatment method of the present invention.
FIG. 12 is a graph showing phosphorus recovery rates for the organic waste liquid treatment method of the present invention.
FIG. 13 is a diagram showing a configuration and a processing flow of an organic waste liquid treatment apparatus according to an embodiment of the present invention.
FIG. 14 is a diagram showing the configuration and processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
FIG. 15 is a diagram showing the configuration and processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
FIG. 16 is a diagram showing a configuration and a processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
FIG. 17 is a diagram showing a configuration and a processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
FIG. 18 is a diagram showing the configuration and processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
FIG. 19 is a diagram showing a configuration and a processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
FIG. 20 is a diagram showing a configuration and a processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
FIG. 21 is a diagram showing a configuration and a processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
FIG. 22 is a diagram showing a configuration and a processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
FIG. 23 is a diagram showing a configuration and a processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
FIG. 24 is a diagram showing the configuration and processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
FIG. 25 is a diagram showing the configuration and processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
FIG. 26 is a diagram showing the configuration and processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
FIG. 27 is a diagram showing a configuration and a processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
FIG. 28 is a diagram showing the configuration and processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
FIG. 29 is a diagram showing the configuration and processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
FIG. 30 is a diagram showing a configuration and a processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
FIG. 31 is a diagram showing a configuration and a processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
FIG. 32 is a diagram showing a configuration and a processing flow of an organic waste liquid treatment apparatus according to another embodiment of the present invention.
[Explanation of symbols]
1 Anaerobic digestion tank 2 Organic waste liquid introduction path 3 Digested sludge discharge path 4 Solid-liquid separation tank 5 Concentrated sludge discharge path 6 Sludge disposal path 7 Sludge return path 8 Treated water discharge path 9 Ultrasonic wave Crushing treatment tank, 11 ozone treatment tank, 13 methane generation tank, 14 digested sludge discharge path, 15 solid-liquid separation tank, 16 treated water discharge path, 17 solid-liquid separation tank, 18 treatment liquid discharge path, 19 concentrated liquid introduction path, 20 Separation liquid discharge path, 21 Coagulant holding tank, 22 Coagulant introduction pump, 23 Coagulant introduction path, 24 Phosphorus recovery tank, 25 Phosphorus recovery path, 26 Phosphorus recovery post-liquid introduction path, 27 Concentrated sludge discharge path, 28 signal Line, 30 ultrasonic crusher, 31 ozone generator, 32 ozone gas injection path, 33 acid generation tank, 34 sludge disposal path, 35 sludge return path, 36 digestion gas discharge path, 37 organic waste liquid introduction pump, 38 digestion sludge extraction Pump, 39 signal line , 40 signal line, 41 MLSS meter, 42 ORP meter, 43 signal line, 44 signal line, 45 MLSS meter, 46 sludge return pump, 47 digested sludge extraction path, 48 phosphoric acid concentration meter, 49 ORP meter, 52 controller, 51 Signal line, 53 Signal line, 54 Signal line, 55 Signal line, 102 Membrane separation device, 103 Reforming tank, 104 Processed liquid path, 105 Return sludge path, 111 Connection path, 117 Concentrated liquid take-out path, 123 Reformed sludge Road.

Claims (6)

An organic waste liquid treatment method for anaerobic digestion,
At least one of the inflowing organic waste liquid, the digested sludge extracted from the anaerobic digestion process, and the solid sludge after solid-liquid separation of the digested sludge, or the organic sludge, digested sludge or the concentrated A dispersion treatment step of dispersing at least a part of the solid in the sludge mixture;
A reforming treatment step for modifying the organic matter in the organic waste liquid, the digested sludge or the concentrated sludge after the dispersion treatment, or the mixture of the organic sludge, the digested sludge or the concentrated sludge;
A separation step of separating the organic waste liquid after the reforming treatment, the digested sludge or the concentrated sludge, or the mixture of the organic sludge, the digested sludge or the concentrated sludge into a solution and a solid;
Anaerobic digestion of the solid after the separation step ;
A phosphorus recovery step of recovering phosphorus from the solution after the separation step . The method of claim 1, wherein performing the anaerobic digestion of the solution by introducing a part or all of the solution after the phosphorus recovery process in a bath of performing anaerobic digestion. In the phosphorus recovery process, method according to any one of claims 1-2 for recovering phosphorus as solid calcium phosphate. An organic waste liquid treatment apparatus including an apparatus for anaerobic digestion,
At least one of the inflowing organic waste liquid, the digested sludge extracted from the anaerobic digester, and the solid sludge after solid-liquid separation of the digested sludge, or the organic sludge, digested sludge or the A dispersion treatment device for dispersing at least a part of solids in the mixture of concentrated sludge;
A reforming treatment device for reforming organic matter in at least one of the organic waste liquid, digested sludge and the concentrated sludge, or the mixture of the organic sludge, the digested sludge or the concentrated sludge after being treated by the dispersion treatment device;
A separation device for separating the organic waste liquid, digested sludge or the concentrated sludge, or the mixture of the organic sludge, digested sludge or the concentrated sludge, which has been treated by the reforming device, into a solution and a solid;
An introduction device for introducing the solid material after being treated in the separation device into the device for performing the anaerobic digestion ;
An apparatus comprising: a phosphorus recovery apparatus that recovers phosphorus from the solution that has been treated by the separation apparatus. The apparatus according to claim 4 , further comprising a tank for performing anaerobic digestion by introducing a part or all of the solution after the phosphorus recovery in the phosphorus recovery apparatus for recovering phosphorus from the solution. In the phosphorus recovery device, device according to any one of claims 4-5 comprising means for recovering phosphorus as solid calcium phosphate.

Images