JP2004277464A - Apparatus for carbonization treatment of organic material-containing sludge - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide an apparatus for a carbonization treatment designed to prevent a carbonized product obtained by carrying out a carbonization treatment of sewage sludge from starting burning by self-heating during storage, etc., can be prevented. <P>SOLUTION: The apparatus for the carbonization treatment is composed by including the following. A drying furnace 14 for carrying out a drying treatment of the sludge to a state of a prescribed water content, a carbonization furnace 18 for carbonizing the sludge subjected to the drying treatment in the drying furnace 14 by a dry distillation treatment and a low-temperature oxidizing atmosphere treating furnace 64 for subjecting active groups having a high activity for an oxidizing reaction in the carbonized product after the carbonizing treatment in the carbonization furnace 18 to a noncombustion oxidizing reaction at a low temperature and stabilizing the active groups. <P>COPYRIGHT: (C)2005,JPO&NCIPI

Description

【００２０】
上に示しているように〜７００℃でメタン，エチレン，一酸化炭素が盛んに発生し、それが十分に行われている炭化製品が炭化度合いの高い炭化製品となる。
【００２１】
図６は上記特許願（特願２００３−６４３４９号：未公開）において提案した内容の一部を抜粋して示したもので、この図６に示すグラフは、図５に示す炭化処理装置で炭化処理した３種の炭化製品の酸素吸収（酸化反応）の挙動を調査した結果を示している。
図６の結果から明らかなように、何れの炭化製品についても時間とともに空気中の酸素濃度が減少し、炭化製品の重量が増加している。即ち６０℃の低温でも酸素吸収（酸化反応）は明らかに起っている。
また同時にＣＯ_２の発生が実質的に確認されなかったことから、炭化製品表面の酸化反応であると考えられる。
【００２２】
尚、時間の経過に伴い酸素吸収は収まって来る。石炭の場合の酸化反応は燃焼反応であることが一般的に知られている。燃焼反応の場合は時間経過とともに酸素吸収量が増加し、またこれと併せてＣＯ_２の発生量が増加する。
よって炭化製品の発熱現象は燃焼反応でないと考えることができる。
【００２３】
以上の他の詳しい点については上記の特許願（特願２００３−６４３４９号：未公開）に詳しく開示されているので、ここでは更なる詳しい説明は割愛する。
【００２４】
本発明者等は、その後更に研究を進める中で炭化製品の表面活性基を消失させる酸化反応（非燃焼酸化反応）は、必ずしも低温域でなくても、酸素濃度を所定以下に制御するならば２００℃以上、例えば４００℃以上の高温域においても可能であり、これによって炭化製品を安定化し得るとの知見を得た。
【００２５】
【特許文献１】
特開平１１−３７６４４号公報
【特許文献２】
特開平１１−３３５９９号公報
【特許文献３】
特開平１１−３７６４５号公報
【特許文献４】
特開平１１−３７６５６号公報
【００２６】
【課題を解決するための手段】
本発明はこのような事情の下に、有機物含有汚泥を炭化し且つ安定化することのできる炭化処理装置を提供することを目的としてなされたものである。
而して請求項１のものは、（イ）有機物含有汚泥を所定水分状態まで乾燥処理する乾燥炉と、（ロ）該乾燥炉で乾燥処理された該汚泥を乾留処理により炭化する炭化炉と、（ハ）該炭化炉で炭化処理された後の炭化製品を、該炭化製品の酸化反応に対し活性の高い活性基を非燃焼酸化反応させて安定化させる安定化処理炉とを備えていることを特徴とする。
【００２７】
請求項２のものは、請求項１において、前記汚泥が排水処理で生じた有機汚泥であることを特徴とする。
【００２８】
請求項３のものは、請求項１，２の何れかにおいて、前記安定化処理炉が、前記炭化製品を低温酸化反応させることによって安定化する低温酸化処理炉であることを特徴とする。
【００２９】
請求項４のものは、請求項３において、前記低温酸化処理炉が６０℃〜２００℃の温度の範囲内で酸化反応処理を行うものであることを特徴とする。
【００３０】
請求項５のものは、請求項１〜４の何れかにおいて、前記炭化炉で炭化処理された後の炭化製品を冷却する冷却器を設け、該冷却器で冷却後の炭化製品を前記安定化処理炉に供給して安定化処理するようになしてあることを特徴とする。
【００３１】
請求項６のものは、請求項１〜５の何れかにおいて、前記安定化処理炉から排出された炭化製品を加湿する加湿機が更に設けてあることを特徴とする。
【００３２】
請求項７のものは、請求項１〜６の何れかにおいて、前記炭化炉の高温の排ガスとの熱交換によって発生させた熱風を前記安定化処理炉用の加熱源として該安定化処理炉に供給するようになしたことを特徴とする。
【００３３】
請求項８のものは、請求項７において、前記熱風を水蒸気含有の蒸気として前記安定化処理炉に供給するようになしたことを特徴とする。
【００３４】
請求項９のものは、請求項１〜８の何れかにおいて、前記乾燥炉における乾燥用の熱風を発生させる熱風炉を設けて、該熱風炉で発生した熱風を、該乾燥炉を経由して該熱風炉に戻る循環路に沿って循環流通させるようになすとともに、該熱風炉から出た熱風の一部を該循環流通する熱風との間で熱交換させ、更に外気導入により所定温度まで温度降下させた上で、前記安定化処理炉に供給するようになしたことを特徴とする。
【００３５】
請求項１０のものは、請求項１〜８の何れかにおいて、前記乾燥炉における乾燥用の熱風を発生させる熱風炉を設けて、該熱風炉で発生した熱風を、該乾燥炉を経由して該熱風炉に戻る循環路に沿って循環流通させるようになすとともに、前記炭化炉からの排ガスを該循環流通する熱風との間で熱交換させ、更に外気導入により所定温度まで温度降下させた上で、前記安定化処理炉に供給するようになしたことを特徴とする。
【００３６】
【作用及び発明の効果】
以上のように本発明は、有機物含有汚泥を乾燥処理する乾燥炉と、その乾燥炉で乾燥処理された汚泥を乾留処理により炭化する炭化炉とを備え、更に加えて、炭化炉で炭化処理された後の炭化製品に対し、酸化反応に対し活性を有する活性基を非燃焼酸化反応させて安定化する安定化処理炉を備えて炭化処理装置を構成したもので、本発明によれば、炭化処理後において炭化製品が自己発熱するのを抑制し、その自己発熱によって炭化製品が燃焼を誘発する現象を有効に防止することができる。
【００３７】
本発明は、有機物含有の様々な汚泥の炭化処理装置として適用可能なものであるが、特に排水処理で生じた有機汚泥の炭化処理装置として好適に適用することができる（請求項２）。
【００３８】
本発明において、安定化処理炉はその内部を窒素パージするなどして酸素濃度を所定以下に制御することで、２００℃以上の高温域でも炭化製品を非燃焼酸化反応させて安定化処理することが可能である。
但しかかる安定化処理炉としては、内部の雰囲気温度を低温に保ち、炭化製品を酸化反応処理する低温酸化処理炉とするのが好適である（請求項３）。
このように安定化処理炉を低温酸化処理炉とすることで、大気条件の下で炭化製品を酸化反応処理することが可能となって、設備費及びランニングコストを安価となすことができる。
【００３９】
この場合において低温酸化処理炉は、６０℃〜２００℃の温度の範囲内で酸化反応を行わせるものとなしておくのが好適である（請求項４）。
その理由は、６０℃の低温でも炭化製品を燃焼とは別の酸化反応を十分に進行させ得ること、一方で２００℃を超えると炭化製品によっては発火点を超えるものが出て来る恐れがあることなどによる。
但し実際上は１００℃以下でも十分に反応を進行させ得ることから、より望ましくは１００℃以下の温度で処理を行うのが良い。
またこの低温酸化処理炉での炭化製品の滞留時間としては、これを６０℃〜２００℃の温度範囲の下で１０時間以上加熱状態に保持しておくのが望ましい。
【００４０】
本発明においては、炭化炉からの炭化製品を一旦冷却器で冷却した上で安定化処理炉に供給し、そこで安定化処理するようになすことが望ましい（請求項５）。
このように炭化炉からの炭化製品を一旦冷却器で冷却した上で安定化処理炉に供給するようになすことで、炭化炉から排出された未だ高温状態の炭化製品が、安定化処理炉内で酸素の存在の下に燃焼してしまうといったことを確実に防止することが可能となる。
【００４１】
本発明ではまた、安定化処理炉で炭化製品を安定化処理した後において、これを加湿する加湿機を更に設けておくことが望ましい（請求項６）。
炭化製品を貯蔵するに際し、予めこれを加湿状態としておくことで、その後の炭化製品の自己発熱及びこれに由来する燃焼をより確実に防止することが可能となる。
尚炭化製品を加湿機で加湿するに際し、炭化製品の含水率が３０％以上となるようにこれを加湿しておくことが望ましい。
【００４２】
本発明においては、安定化処理炉内を所定温度に加熱するに際し、炭化炉の高温の排ガスとの熱交換により発生させた熱風を安定化処理炉に供給するようになすことができる（請求項７）。
このようにすることで、炭化炉で発生した高温の排ガスの熱を回収して安定化処理炉内の加熱用に有効利用でき、安定化処理炉を独立した専用の熱源により加熱する場合に比べて、燃料コスト，ランニングコストを安価となすことができる。
【００４３】
この場合において安定化処理炉に供給する熱風を、加熱蒸気の形で供給するようになすことができる（請求項８）。
この場合安定化処理炉内で炭化製品を加熱するに際し、炭化製品に当たったミストが加熱により気体化したときの体積膨張によって、炭化製品の細孔表面積を効果的に拡大することができ、いわば炭化製品を活性の高い活性炭に近い性状となすことが可能となる効果が得られる。
【００４４】
次に請求項９は、熱風炉で発生した熱風を、乾燥炉を経由して熱風炉に戻る循環路に沿って循環流通させるようになすとともに、熱風炉から出た熱風の一部を、循環路を循環流通する熱風との間で熱交換し、更に外気導入により所定温度まで温度降下した上で安定化処理炉内の加熱用の熱風として供給するようになしたものである。
この場合においても、従来外部に放出されていた熱エネルギーを安定化処理炉内の加熱のための熱源として有効に活用でき、安定化処理炉におけるランニングコストを低減することができる。
【００４５】
一方請求項１０は、炭化炉からの排ガスの有する熱を回収してこれを安定化処理炉内の加熱用として利用するようになしたもので、この場合においても、従来外部に放出されていた熱エネルギーを安定化処理炉内の加熱用として有効に活用でき、安定化処理炉のランニングコストを安価となすことができる。
【００４６】
【実施例】
次に本発明の実施例を図面に基づいて詳しく説明する。
図１は、本発明の一実施例である有機物含有汚泥、ここでは活性汚泥法による下水の排水処理で生じた余剰汚泥の炭化処理装置の全体構成を示したもので、図中１０は受入ホッパであり、含水率８０％程度まで脱水された汚泥ケーキがこの受入ホッパ１０に先ず受け入れられる。
ここに受け入れられた汚泥ケーキは、定量供給装置１２にて乾燥炉１４へと送られ、そこで所定の含水率、例えば４０％程度の含水率まで乾燥処理される。
尚この乾燥炉１４では、汚泥ケーキの乾燥と併せてその粉砕が行われる。
【００４７】
乾燥炉１４で乾燥処理された汚泥は、続いてコンベヤ１６により炭化炉１８へと搬送され、そこで乾留処理により汚泥の炭化が行われる。
この炭化炉１８においては、図２にも示しているように炉体２０の内部に回転ドラム（レトルト）２２が設けられており、前段の乾燥炉１４で乾燥処理された汚泥がコンベヤ１６により、更には回転ドラム２２の前端部（図中左端部）位置に設けられたスクリューフィーダ２１により回転ドラム２２内部に投入される。
【００４８】
回転ドラム２２内部に投入された汚泥は、先ず炉体２０内部に配設された助燃バーナ（外熱室用バーナ）２４による外熱室２６内部の雰囲気加熱によって加熱される。
すると汚泥中に含まれていた可燃ガスが、回転ドラム２２に設けられた吹出パイプ２８を通じて外熱室２６の雰囲気中に抜け出し、そしてこの可燃ガスが着火して、以後はその可燃ガスの燃焼により回転ドラム２２内部の汚泥の加熱が行われる。
この段階では助燃バーナ２４は燃焼停止される。
【００４９】
図２（Ｂ）に示しているように、炉体２０の内部には外熱室２６と仕切られた排ガス処理室３０が設けられており、外熱室２６からの排ガスはここに導かれる。
この排ガス処理室３０には排ガス処理室用バーナ３２が設けられており、この排ガス処理室用バーナ３２にて、排ガス処理室３０内に導かれた排ガス中の未燃ガスが燃焼される。
【００５０】
回転ドラム２２内部の汚泥は、図中左端の投入口から回転ドラム２２の回転とともに漸次図中右方向に移って行き（回転ドラム２２には若干の勾配が設けてある）、そして最終的に乾留残渣（炭化製品）が回転ドラム２２の図中右端の排出口、つまり炭化炉１８から排出される。
【００５１】
図１において、３４は乾燥炉１４に供給する熱風を発生させるための熱風炉で、ここでは供給された燃料が燃焼空気の供給の下で燃焼させられて熱風を発生する。
尚ここではパイロットバーナ用にＬＰＧが用いられ、燃焼バーナ用に灯油が用いられている。
【００５２】
熱風炉３４で発生した熱風は乾燥炉１４に供給され、更にこれを通過して、その後段の集塵機３６を通ってそこで集塵され、再び熱風炉３４に戻されるようになっている。
即ち熱風炉３４で発生した熱風は、乾燥炉１４，集塵機３６を通る循環路３８を循環ファン４０により循環流通させられるようになっている。
この循環系では、乾燥炉１４においてリークエアが循環する熱風中に入り込む。
【００５３】
一方で熱風炉３４には燃焼空気が定量供給されており、そのためここでは熱風の一部を抜き取るべく、熱風炉３４の下流部において分岐路４２が設けられており、熱風炉３４から出た熱風の一部がこの分岐路４２を通じて外部に取り出されるようになっている。
【００５４】
この分岐路４２に取り出された熱風は高温状態（約７００℃程度）にあり、そこで分岐路４２に取り出された熱風が、循環路３８上に設けられた熱風炉熱交換器４４で熱交換され、更に空気取入口４８から取り入れられた外気により希釈及び冷却された上で、排ガスファン４６により排気路５０，５１を通じて煙突５２から外部に放出される。
ここで分岐路４２に取り出された熱風の、熱風炉熱交換器４４で熱交換された後の温度が約４００℃程度であり、そして空気取入口４８からの外気の取入れによる希釈・冷却により、排ガスファン４６の下流部で温度は約２００℃〜２５０℃程度となる。
【００５５】
尚、空気取入口４８からの空気の取入量は調整弁５４によって調整される。
また循環路３８を循環流通する熱風は、熱風炉熱交換器４４で熱交換されることによりそこで温度上昇させられた上、熱風炉３４の入口に戻される。
【００５６】
上記炭化炉１８からは、その排ガスを排出するための排気路５６が延び出している。
この排気路５６に取り出された炭化炉１８からの排ガスは、温度が８００℃〜１０００℃程度の高温度であり、そこで先ず空気取入口６２からの外気の取入れによって希釈及び冷却された上で、循環路３８上に設けられた炭化炉熱交換器５８で熱交換され、そこで温度降下された後、更に炭化炉熱交換器５８の下流部において、空気取入口６３からの外気の取入れにより再び希釈・冷却された上で、排ガスファン６０により排気路６１，５１を通じて煙突５２から外部に放出される。
【００５７】
尚炭化炉１８から排出された排ガスは、空気取入口６２からの外気の取入れによる希釈・冷却により、その温度は約７００℃程度となり、そして炭化炉熱交換器５８における熱交換、更に空気取入口６３からの外気の取入れによる希釈・冷却によって２００℃〜２５０℃程度の温度まで温度降下された上で、排ガスファン６０により排気路６１，５１を通じ煙突５２から外部に放出される。
この炭化炉１８にはＬＰＧ，灯油等の燃料が燃焼空気とともに供給される。ここでＬＰＧはパイロットバーナの燃焼用として用いられ、また灯油は燃焼バーナ用の燃料として用いられる。
【００５８】
本例では、炭化炉１８の後段に安定化処理炉としての低温酸化雰囲気処理炉（低温酸化処理炉）６４が、更にその低温酸化雰囲気処理炉６４と炭化炉１８との間の位置において冷却器６６が設けられている。
炭化炉１８から排出された炭化製品は、一旦先ずこの冷却器６６に入れられて、そこで常温まで冷却された上で、コンベヤ６８により低温酸化雰囲気処理炉６４へと供給され、そこで安定化処理が施される。
【００５９】
この低温酸化雰囲気処理炉６４は、炭化炉１８で炭化処理された後の炭化製品を、６０℃〜２００℃の範囲の低温で緩やかに酸化反応させ、これにより炭化製品の有する表面活性基を非燃焼酸化反応させて活性点を消失せしめ、その後の自己発熱及びこれにより引き起こされる燃焼を未然に防止するための処理炉である。
【００６０】
炭化製品は、この低温酸化雰囲気処理炉６４で１０時間以上滞留させられ、そこで安定化処理された上で排出される。
排出された安定化処理後の炭化製品は、この例では更に加湿機７６において加湿処理され、貯留ホッパへと送られてそこに貯留される。この加湿機７６では、この例では含水率３０％まで水分供給される。
尚低温酸化雰囲気処理炉６４での安定化処理は大気雰囲気中で行われる。
【００６１】
この低温酸化雰囲気処理炉６４では、その内部の雰囲気温度を所定温度に昇温し保持する必要がある。
そこでこの例では、炭化炉１８の排ガスの有する熱を回収して低温酸化雰囲気処理炉６４に熱風として供給するようにしている。
詳しくは、ここでは空気取入口６７から取り入れた空気を、図２（Ｂ）に示しているように炭化炉１８の排ガス処理室３０に導いてそこで熱交換させ、加熱をした上で熱風ファン７０により供給路７２を通じて、低温酸化雰囲気処理炉６４へと供給するようにしている。
【００６２】
但し排ガス処理室３０で熱交換した空気をそのまま熱風として低温酸化雰囲気処理炉６４に供給すると温度が高過ぎることから、ここでは空気取入口６９から外気を取り入れ、希釈及び冷却した上で、約６０℃の温度の熱風として低温酸化雰囲気処理炉６４へと供給するようにしている。
【００６３】
この場合、供給路７２を通じて供給される熱風の温度を制御するため、供給路７２内の熱風の温度を温度検知器７４で検知するとともに、その結果を受けて調整弁５４により空気取入口６９からの外気の取入量を制御するようにしている。
【００６４】
尚、低温酸化雰囲気処理炉６４における炭化製品の搬送形式には、スクリューフィーダ式，ケースコンベヤ式，ロータリーキルン式，振動式等があるが、炭化製品と酸素との反応効率上昇の観点から振動式が望ましい。
また低温酸化雰囲気処理炉６４の温度制御の方法として、熱風ファン７０の回転数制御により、熱風の供給量そのものを制御するようになすこともできる。
【００６５】
このような本例の炭化処理装置によれば、炭化製品がその後自己発熱を起して燃焼を誘発する現象を有効に防止できる。
また安定化処理炉を低温酸化雰囲気処理炉６４として構成し、大気条件の下で炭化製品を酸化反応処理していることから設備費及びランニングコストを安価となすことができる。
【００６６】
また本例では、炭化炉１８からの炭化製品を一旦冷却器６６で冷却した上で低温酸化雰囲気処理炉６４に供給し、そこで安定化処理するようになしていることから、炭化炉１８から排出された未だ高温状態の炭化製品が低温酸化雰囲気処理炉６４内で酸素の存在の下に燃焼してしまうといったことを確実に防止できる。
【００６７】
加えて本例では低温酸化雰囲気処理炉６４で炭化製品を安定化処理した後において、更にこれを加湿機７６にて加湿するようになしてあるため、その後の炭化製品の自己発熱及びこれに由来する燃焼をより確実に防止することができる。
【００６８】
更に本例では低温酸化雰囲気処理炉６４内を所定温度に加熱するに際し、炭化炉１８からの高温の排ガスから熱回収してこれを利用しているため、低温酸化雰囲気処理炉６４を独立した専用の熱源により加熱する場合に比べて燃料コストを削減でき、ランニングコストを安価となすことができる。
【００６９】
尚、炭化炉１８から排出された炭化製品の安定化処理炉として、上記低温酸化雰囲気処理炉６４の他、内部の酸素濃度を所定以下に保持することにより、２００℃以上の高温で炭化製品を非燃焼酸化反応させる他の形態の安定化処理炉として構成することも可能である。
この点は以下の実施例においても同様である。
【００７０】
図３は本発明の他の実施例を示している。
この例は、水タンク７８内部の水を水ポンプ８０にて炭化炉１８の排ガス処理室３０に導き、低温酸化雰囲気処理炉６４に対し蒸気を供給して、その蒸気加熱により炭化製品を非燃焼酸化反応処理し、安定化するようになしたものである。
他の点については基本的に上記実施例と同様である。
【００７１】
本例によれば、低温酸化雰囲気処理炉６４内で炭化製品に当たったミストが加熱により気体化したときの体積膨張により炭化製品の細孔表面積を効果的に拡大することができ、炭化製品を言わば活性の高い活性炭に近い性状となすことが可能となる。
【００７２】
図４は本発明の更に他の実施例を示したもので、この例は図１における熱風炉３４からの熱風を排出するための排ガスファン４６，炭化炉１８からの排ガスを排出するための排ガスファン６０の下流部の排ガスを、供給路８１を通じて低温酸化雰囲気処理炉６４に供給するようになし、その際に空気取入口６９からの外気の取入れにより排ガスを希釈及び冷却し、約６０℃の温度の熱風としてこれを低温酸化雰囲気処理炉６４に供給するようになした例である。
尚低温酸化雰囲気処理炉６４からの排ガスは、排気路８２を通じて煙突５２から外部に放出する。
他の点については図１の実施例と基本的に同様である。
【００７３】
本例においても、従来外部に放出されていた熱エネルギーを低温酸化雰囲気処理炉６４内の加熱のための熱源として有効に活用でき、低温酸化雰囲気処理炉６４におけるランニングコストを低減することができる。
【００７４】
以上本発明の実施例を詳述したがこれはあくまで一例示であり、本発明はその趣旨を逸脱しない範囲において種々変更を加えた形態で構成可能である。
【図面の簡単な説明】
【図１】本発明の一実施例である有機物含有汚泥の炭化処理装置を示す図である。
【図２】図１における炭化炉の構成を示す図である。
【図３】本発明の他の実施例の炭化処理装置を示す図である。
【図４】本発明の更に他の実施例の炭化処理装置を示す図である。
【図５】従来の炭化処理装置の例を示す図である。
【図６】本発明において安定化処理炉を設けることの意味を説明するための説明図である。
【符号の説明】
１４ 乾燥炉
１８ 炭化炉
３４ 熱風炉
３８ 循環路
６４ 低温酸化雰囲気処理炉（安定化処理炉）
６６ 冷却器
７６ 加湿機[0001]
TECHNICAL FIELD OF THE INVENTION
The present invention relates to a carbonization apparatus for carbonizing organic matter-containing sludge represented by sewage sludge by dry distillation.
[0002]
BACKGROUND OF THE INVENTION
Organic matter-containing wastewater discharged from homes and the like is generally subjected to wastewater treatment in a sewage treatment facility by an activated sludge method or the like.
Organic sludge is generated with this wastewater treatment, but the amount of organic sludge generated increases year by year with an increase in the amount of wastewater treatment, and its treatment and disposal has become a major problem.
[0003]
When disposing of organic sludge, the organic sludge contains about 99% of water and cannot be disposed of as it is, where it is concentrated and dehydrated for weight reduction, or further incinerated or melted. Various processes are currently being performed.
However, when sludge is incinerated or melted, a large amount of energy is consumed and the treatment cost is high.
Therefore, as one method of organic sludge reduction treatment with low energy consumption, carbonization of sludge by carbonization treatment has been proposed.
[0004]
In this carbonization treatment, since the sludge contains about 45% by weight of carbon in the substrate, the carbon in the sludge is not consumed as in incineration and melting treatments, but the sludge is converted to oxygen-free or low-oxygen. By pyrolyzing (carbonizing) in an oxygen state, the carbon content remains, and is generated as a carbide (carbonized product) having a new composition.
[0005]
Patent Documents 1 to 4 below propose an apparatus for that purpose, that is, an apparatus for carbonizing organic matter-containing sludge.
FIG. 5 specifically shows a carbonization apparatus disclosed in Patent Document 4.
In the figure, reference numeral 200 denotes a receiving hopper which receives sludge cake dehydrated to a water content of about 80%.
[0006]
The sludge cake received by the receiving hopper 200 is sent to the drying furnace 204 by the constant-quantity supply device 202, where the drying process is performed to a predetermined moisture content, for example, about 40%.
In the drying furnace 204, the sludge cake is pulverized while being dried.
[0007]
The sludge that has been dried in the drying furnace 204 is subsequently conveyed to the carbonization furnace 208 by the conveyor 206, where the sludge is carbonized by dry distillation.
In the carbonization furnace 208, a rotary drum (retort) 228 is provided inside a furnace body 226, and the sludge that has been dried in the drying furnace 204 in the preceding stage is put into the rotary drum 228, and first the furnace body 226. It is heated by the atmosphere heating by the auxiliary burner disposed inside.
[0008]
Then, the combustible gas contained in the sludge escapes into the atmosphere through a blowing pipe provided on the rotary drum 228, and the combustible gas is ignited. Thereafter, the combustion of the combustible gas released from the sludge causes the inside of the rotary drum 228 to burn. Is heated.
At this stage, combustion of the auxiliary burner is stopped.
[0009]
The sludge inside the rotary drum 228 gradually moves rightward in the figure with the rotation of the rotary drum 228 from the input port at the left end in the figure (the rotary drum 228 has a slight gradient), and finally is carbonized. The residue (carbonized product) is discharged from the discharge port at the right end of the rotary drum 228 in the drawing, that is, from the carbonization furnace 208.
[0010]
Reference numeral 210 denotes a hot-air oven for generating hot air to be supplied to the drying furnace 204. Here, the supplied fuel is burned under the supply of combustion air to generate hot air.
Here, LPG is used for the pilot burner, and kerosene is used for the combustion burner.
[0011]
The hot air generated in the hot blast furnace 210 is supplied to the drying furnace 204, passes through the drying furnace 204, passes through a dust collector 212 at the subsequent stage, and is returned to the hot blast furnace 210 again.
That is, the hot air generated in the hot air furnace 210 can be circulated and circulated through the circulation path 213 passing through the drying furnace 204 and the dust collector 212.
[0012]
In this circulation system, leak air enters in the drying furnace 204.
On the other hand, the combustion air is supplied in a fixed amount in the hot stove 210, so that a portion of the hot air is taken out through the branch passage 214 in the downstream portion of the hot stove 210.
The hot air taken out of the branch passage 214 is at a high temperature, and the hot air taken out of the branch passage 214 is heat-exchanged in the hot-blast stove heat exchanger 216, cooled down, and then discharged from the chimney 220 by the exhaust gas fan 218. Released to
The hot air circulating through the circulation path 213 undergoes heat exchange in the hot air stove heat exchanger 216, and the temperature thereof rises there.
[0013]
High-temperature exhaust gas is also generated in the carbonizing furnace 208.
Then, the exhaust gas from the carbonization furnace 208 is taken out through the exhaust path 222, heat-exchanged in the carbonization furnace heat exchanger 224 provided on the circulation path 213, cooled down, and discharged to the outside through the exhaust path 230.
[0014]
In the carbonization furnace 208, LPG is used for the auxiliary burner and kerosene is used for the combustion burner, and these are burned under the supply of combustion air.
However, the inside of the rotating drum 228 as a retort is maintained in an oxygen-free or low-oxygen state for dry distillation.
[0015]
The carbonized product obtained by the carbonization apparatus has properties similar to those of charcoal, and is currently used for horticultural soil, snow melting agents, and the like.
The carbonized product manufactured in this manner is temporarily stored in a storage.
However, it has been found that the carbonized product may burn out during storage.
It is considered that the reason is that the carbonized product has a self-heating property, and the temperature of the carbonized product rises due to the self-heating during storage, and combustion occurs when the temperature exceeds a certain temperature.
[0016]
Carbonized products have properties close to charcoal as described above, and are expected to expand in various applications in the future, but for that purpose, they must not burn out during storage, It is necessary to solve that problem.
[0017]
Thus, the present inventors have conducted various studies to determine the cause of self-heating in carbonized products.
As a result, the following facts became clear. That is
(1) The degree of carbonization of carbonized products varies depending on the processing conditions, and particularly, the degree of carbonization is low but the self-heating is high.
(2) Carbonized products have active groups (surface functional groups) that are highly active in oxidation reactions (mainly alkyl groups bonded to aromatic rings), and the lower the degree of carbonization, the more the active groups are contained. , That the active groups increase self-heating
(3) Self-heating can occur even at low temperatures below 200 ° C
(4) The self-heating at low temperature is different from the combustion reaction, and is considered to be due to the air oxidation reaction of the active group.
(5) The self-heating at low temperature gradually converges while the carbonized product is kept in a low-temperature oxidizing atmosphere, that is, the active sites (active groups) gradually disappear and eventually become stable.
And so on.
[0018]
The present inventors have invented a method of treating organic matter-containing sludge based on this finding, and have proposed this in a patent application (Japanese Patent Application No. 2003-64349: not disclosed).
[0019]
In the process of sludge carbonization in the carbonization furnace, the following components are separated according to the temperature.
[Table 1]

[0020]
As shown above, methane, ethylene, and carbon monoxide are generated at 〜700 ° C., and a carbonized product in which methane, ethylene, and carbon monoxide are sufficiently produced becomes a carbonized product having a high degree of carbonization.
[0021]
FIG. 6 shows an excerpt of a part of the content proposed in the above-mentioned patent application (Japanese Patent Application No. 2003-64349: not disclosed). The graph shown in FIG. 6 is carbonized by the carbonizing apparatus shown in FIG. The results of investigating the behavior of oxygen absorption (oxidation reaction) of the three types of carbonized products thus treated are shown.
As is clear from the results in FIG. 6, the oxygen concentration in the air decreases with time for any of the carbonized products, and the weight of the carbonized product increases. That is, oxygen absorption (oxidation reaction) clearly occurs even at a low temperature of 60 ° C.
Also at the same time CO ₂ Since the generation of the carbonization was not substantially confirmed, it is considered to be an oxidation reaction on the surface of the carbonized product.
[0022]
Note that the oxygen absorption stops as time passes. It is generally known that the oxidation reaction in the case of coal is a combustion reaction. In the case of a combustion reaction, the amount of oxygen absorbed increases with the lapse of time. ₂ The amount of generation increases.
Therefore, it can be considered that the exothermic phenomenon of the carbonized product is not a combustion reaction.
[0023]
Since the other detailed points are disclosed in detail in the above-mentioned patent application (Japanese Patent Application No. 2003-64349: not disclosed), further detailed description is omitted here.
[0024]
The inventors of the present invention have been conducting further research, and the oxidation reaction (non-combustion oxidation reaction) for eliminating the surface active groups of the carbonized product is not limited to a low temperature range, provided that the oxygen concentration is controlled to a predetermined level or less. It has been found that it is possible even in a high temperature range of 200 ° C. or more, for example, 400 ° C. or more, thereby stabilizing carbonized products.
[0025]
[Patent Document 1]
JP-A-11-37644
[Patent Document 2]
JP-A-11-33599
[Patent Document 3]
JP-A-11-37645
[Patent Document 4]
JP-A-11-37656
[0026]
[Means for Solving the Problems]
The present invention has been made under the above circumstances to provide a carbonization treatment apparatus capable of carbonizing and stabilizing organic matter-containing sludge.
According to the first aspect of the present invention, there are provided (a) a drying furnace for drying sludge containing organic matter to a predetermined moisture state, and (b) a carbonizing furnace for carbonizing the sludge dried in the drying furnace by carbonization. (C) a stabilization furnace for stabilizing the carbonized product after carbonization in the carbonization furnace by non-combustion oxidation reaction of an active group having high activity with respect to the oxidation reaction of the carbonized product. It is characterized by the following.
[0027]
According to a second aspect of the present invention, in the first aspect, the sludge is an organic sludge generated by wastewater treatment.
[0028]
A third aspect of the present invention is characterized in that, in any one of the first and second aspects, the stabilization furnace is a low-temperature oxidation furnace that stabilizes the carbonized product by causing a low-temperature oxidation reaction.
[0029]
A fourth aspect of the present invention is characterized in that, in the third aspect, the low-temperature oxidation treatment furnace performs an oxidation reaction treatment within a temperature range of 60 ° C to 200 ° C.
[0030]
Claim 5 provides a cooler for cooling the carbonized product after being carbonized in the carbonizing furnace according to any one of Claims 1 to 4, and stabilizes the carbonized product after being cooled by the cooler. It is characterized in that it is supplied to a processing furnace for stabilization.
[0031]
According to a sixth aspect of the present invention, in any one of the first to fifth aspects, a humidifier for humidifying the carbonized product discharged from the stabilization furnace is further provided.
[0032]
In the stabilization processing furnace, the hot air generated by heat exchange with high-temperature exhaust gas of the carbonization furnace is used as a heating source for the stabilization processing furnace. It is characterized in that it is supplied.
[0033]
An eighth aspect of the present invention is characterized in that, in the seventh aspect, the hot air is supplied to the stabilization furnace as steam containing steam.
[0034]
The ninth aspect of the present invention is the method according to any one of the first to eighth aspects, wherein a hot blast stove for generating hot blast for drying in the drying oven is provided, and the hot blast generated by the hot blast stove is passed through the drying oven. The hot air stove is circulated and circulated along a circulation path returning to the hot blast stove, and a part of the hot air discharged from the hot stove is exchanged with the hot air circulating and circulated. After being lowered, it is supplied to the stabilization furnace.
[0035]
Claim 10 provides a hot air oven for generating hot air for drying in the drying oven according to any one of claims 1 to 8, wherein the hot air generated by the hot air oven is passed through the drying oven. While circulating along the circulation path returning to the hot blast stove, the exhaust gas from the carbonizing furnace was subjected to heat exchange with the circulating hot air, and the temperature was lowered to a predetermined temperature by introducing outside air. And supplying the gas to the stabilization furnace.
[0036]
[Action and effect of the invention]
As described above, the present invention includes a drying furnace for drying the organic matter-containing sludge, and a carbonization furnace for carbonizing the sludge dried in the drying furnace by the carbonization treatment. According to the present invention, the carbonized product is provided with a stabilization treatment furnace for stabilizing the carbonized product after the oxidation by reacting an active group having an activity to the oxidation reaction by non-combustion oxidation reaction. It is possible to suppress the carbonized product from self-heating after the treatment, and effectively prevent the carbonized product from inducing combustion due to the self-heating.
[0037]
INDUSTRIAL APPLICABILITY The present invention is applicable as an apparatus for carbonizing various kinds of sludge containing organic matter, and can be particularly suitably applied as an apparatus for carbonizing organic sludge generated in wastewater treatment (claim 2).
[0038]
In the present invention, the stabilization treatment furnace performs a non-combustion oxidation reaction of the carbonized product even in a high temperature range of 200 ° C. or more by performing a stabilization treatment by controlling the oxygen concentration to a predetermined value or less by purging the inside with nitrogen or the like. Is possible.
However, such a stabilizing furnace is preferably a low-temperature oxidizing furnace that maintains an internal atmosphere temperature at a low temperature and performs an oxidation reaction treatment on a carbonized product.
By using the low-temperature oxidation treatment furnace as the stabilization treatment furnace, the carbonized product can be subjected to an oxidation reaction treatment under atmospheric conditions, and equipment costs and running costs can be reduced.
[0039]
In this case, it is preferable that the low-temperature oxidation treatment furnace is configured to perform the oxidation reaction within a temperature range of 60 ° C to 200 ° C (claim 4).
The reason is that, even at a low temperature of 60 ° C., the carbonized product can sufficiently proceed an oxidation reaction different from combustion, while if the temperature exceeds 200 ° C., some of the carbonized products may exceed the ignition point. It depends.
However, in practice, the reaction can sufficiently proceed even at a temperature of 100 ° C. or less, so that it is more preferable to perform the treatment at a temperature of 100 ° C. or less.
As the residence time of the carbonized product in the low-temperature oxidation furnace, it is desirable to keep the carbonized product in a heated state for 10 hours or more in a temperature range of 60 ° C to 200 ° C.
[0040]
In the present invention, it is desirable that the carbonized product from the carbonization furnace is once cooled by the cooler and then supplied to the stabilization processing furnace, where it is subjected to the stabilization processing (claim 5).
In this way, the carbonized product from the carbonization furnace is once cooled by the cooler and then supplied to the stabilization furnace, so that the still high-temperature carbonized product discharged from the carbonization furnace is discharged into the stabilization furnace. Thus, combustion in the presence of oxygen can be reliably prevented.
[0041]
Further, in the present invention, it is desirable to further provide a humidifier for humidifying the carbonized product after stabilizing the carbonized product in the stabilizing furnace (claim 6).
By storing the carbonized product in a humidified state before storage, it is possible to more reliably prevent the self-heating of the carbonized product and combustion resulting from the heat generation.
When the carbonized product is humidified by a humidifier, it is desirable to humidify the carbonized product so that the moisture content of the carbonized product is 30% or more.
[0042]
In the present invention, when heating the inside of the stabilization processing furnace to a predetermined temperature, hot air generated by heat exchange with high-temperature exhaust gas of the carbonization furnace can be supplied to the stabilization processing furnace. 7).
By doing so, the heat of the high-temperature exhaust gas generated in the carbonization furnace can be recovered and effectively used for heating in the stabilization processing furnace, as compared with the case where the stabilization processing furnace is heated by an independent dedicated heat source. Thus, fuel cost and running cost can be reduced.
[0043]
In this case, the hot air supplied to the stabilization processing furnace can be supplied in the form of heated steam.
In this case, when heating the carbonized product in the stabilization furnace, the volume expansion when the mist hitting the carbonized product is gasified by heating can effectively expand the pore surface area of the carbonized product, so to speak An effect is obtained in which the carbonized product can be made to have properties close to activated carbon having high activity.
[0044]
Next, the circulating hot air generated in the hot blast stove is circulated along a circulation path returning to the hot blast stove via the drying furnace, and a part of the hot blast out of the hot blast stove is circulated. The heat is exchanged with the hot air circulating in the passage, and the temperature is further reduced to a predetermined temperature by introducing outside air, and then supplied as hot air for heating in the stabilization furnace.
Also in this case, the heat energy that has been conventionally released to the outside can be effectively utilized as a heat source for heating the inside of the stabilization processing furnace, and the running cost in the stabilization processing furnace can be reduced.
[0045]
On the other hand, claim 10 recovers the heat of the exhaust gas from the carbonization furnace and uses the recovered heat for heating the inside of the stabilization processing furnace. In this case, the heat is conventionally released to the outside. The heat energy can be effectively used for heating the inside of the stabilization processing furnace, and the running cost of the stabilization processing furnace can be reduced.
[0046]
【Example】
Next, embodiments of the present invention will be described in detail with reference to the drawings.
FIG. 1 shows an entire configuration of an apparatus for carbonizing surplus sludge generated by sewage drainage treatment by an activated sludge method, which is an embodiment of the present invention, in which 10 is a receiving hopper. The sludge cake dehydrated to a water content of about 80% is first received in the receiving hopper 10.
The sludge cake received here is sent to the drying furnace 14 by the quantitative supply device 12, where it is dried to a predetermined moisture content, for example, about 40%.
In the drying furnace 14, the sludge cake is pulverized while being dried.
[0047]
The sludge dried in the drying furnace 14 is subsequently conveyed to the carbonization furnace 18 by the conveyor 16, where the sludge is carbonized by dry distillation.
In the carbonization furnace 18, as shown in FIG. 2, a rotary drum (retort) 22 is provided inside a furnace body 20, and the sludge that has been dried in the drying furnace 14 in the preceding stage is conveyed by the conveyor 16. Further, it is fed into the rotating drum 22 by a screw feeder 21 provided at a front end (left end in the figure) of the rotating drum 22.
[0048]
The sludge introduced into the rotary drum 22 is first heated by the atmosphere heating inside the external heat chamber 26 by the auxiliary burner (burner for external heat chamber) 24 disposed inside the furnace body 20.
Then, the combustible gas contained in the sludge escapes into the atmosphere of the external heat chamber 26 through the blowing pipe 28 provided on the rotary drum 22, and the combustible gas is ignited. The sludge inside the rotating drum 22 is heated.
At this stage, combustion of the auxiliary burner 24 is stopped.
[0049]
As shown in FIG. 2 (B), an exhaust gas treatment chamber 30 partitioned from the external heat chamber 26 is provided inside the furnace body 20, and the exhaust gas from the external heat chamber 26 is guided here.
An exhaust gas processing chamber burner 32 is provided in the exhaust gas processing chamber 30, and the unburned gas in the exhaust gas guided into the exhaust gas processing chamber 30 is burned by the exhaust gas processing chamber burner 32.
[0050]
The sludge inside the rotary drum 22 gradually moves rightward in the figure with the rotation of the rotary drum 22 from the input port at the left end in the figure (the rotary drum 22 has a slight gradient), and finally carbonizes. The residue (carbonized product) is discharged from the discharge port at the right end of the rotary drum 22 in the drawing, that is, from the carbonization furnace 18.
[0051]
In FIG. 1, reference numeral 34 denotes a hot blast stove for generating hot blast to be supplied to the drying furnace 14, wherein the supplied fuel is burned under the supply of combustion air to generate hot blast.
Here, LPG is used for the pilot burner, and kerosene is used for the combustion burner.
[0052]
The hot air generated in the hot air furnace 34 is supplied to the drying furnace 14, further passes through the drying furnace 14, passes through a dust collector 36 at a subsequent stage, is collected there, and is returned to the hot air furnace 34 again.
That is, the hot air generated in the hot air furnace 34 is circulated and circulated through the circulation path 38 passing through the drying furnace 14 and the dust collector 36 by the circulation fan 40.
In this circulation system, the leak air enters the hot air circulating in the drying furnace 14.
[0053]
On the other hand, a fixed amount of combustion air is supplied to the hot stove 34, and therefore a branch 42 is provided downstream of the hot stove 34 in order to extract a part of the hot air. Is taken out to the outside through the branch path 42.
[0054]
The hot air taken out to the branch passage 42 is in a high temperature state (about 700 ° C.), and the hot air taken out to the branch passage 42 is heat-exchanged by a hot stove heat exchanger 44 provided on the circulation passage 38. After being diluted and cooled by the outside air introduced from the air intake 48, the exhaust gas is discharged from the chimney 52 to the outside through the exhaust passages 50 and 51 by the exhaust gas fan 46.
Here, the temperature of the hot air taken out to the branch passage 42 after heat exchange in the hot air stove heat exchanger 44 is about 400 ° C., and by dilution / cooling by taking in outside air from the air inlet 48, The temperature is about 200 ° C. to 250 ° C. downstream of the exhaust gas fan 46.
[0055]
The amount of air taken in from the air inlet 48 is adjusted by the adjusting valve 54.
Further, the hot air circulating through the circulation path 38 is heat-exchanged by a hot-air stove heat exchanger 44, the temperature thereof is raised there, and then returned to the inlet of the hot-air stove 34.
[0056]
An exhaust passage 56 for discharging the exhaust gas extends from the carbonization furnace 18.
The exhaust gas from the carbonization furnace 18 taken out to the exhaust passage 56 has a high temperature of about 800 ° C. to 1000 ° C., and is diluted and cooled by taking in outside air from the air inlet 62 first. The heat is exchanged in the carbonization furnace heat exchanger 58 provided on the circulation path 38, and the temperature is reduced there. Then, at the downstream part of the carbonization furnace heat exchanger 58, the dilution is performed again by taking in the outside air from the air intake 63. After being cooled, it is discharged from the chimney 52 to the outside through the exhaust paths 61 and 51 by the exhaust gas fan 60.
[0057]
The temperature of the exhaust gas discharged from the carbonization furnace 18 becomes about 700 ° C. due to dilution and cooling by taking in outside air from the air intake 62, and heat exchange in the carbonization furnace heat exchanger 58, and further, air intake After the temperature is lowered to a temperature of about 200 ° C. to 250 ° C. by dilution / cooling by taking in the outside air from 63, the exhaust gas is discharged to the outside from the chimney 52 through the exhaust paths 61 and 51 by the exhaust gas fan 60.
Fuel such as LPG and kerosene is supplied to the carbonizing furnace 18 together with combustion air. Here, LPG is used for combustion of a pilot burner, and kerosene is used as fuel for a combustion burner.
[0058]
In this example, a low-temperature oxidizing atmosphere processing furnace (low-temperature oxidizing furnace) 64 as a stabilizing processing furnace is provided downstream of the carbonizing furnace 18, and a cooler is further provided at a position between the low-temperature oxidizing atmosphere processing furnace 64 and the carbonizing furnace 18. 66 are provided.
The carbonized product discharged from the carbonizing furnace 18 is first put into the cooler 66, cooled to room temperature, and then supplied to the low-temperature oxidizing atmosphere processing furnace 64 by the conveyor 68, where the stabilizing process is performed. Will be applied.
[0059]
The low-temperature oxidizing atmosphere treatment furnace 64 causes the carbonized product after the carbonizing treatment in the carbonizing furnace 18 to slowly oxidize at a low temperature in the range of 60 ° C. to 200 ° C., thereby deactivating the surface active groups of the carbonized product. This is a processing furnace for causing active sites to disappear by a combustion oxidation reaction, thereby preventing self-heating and subsequent combustion caused thereby.
[0060]
The carbonized product is retained in the low-temperature oxidizing atmosphere processing furnace 64 for 10 hours or more, where it is stabilized and discharged.
The discharged carbonized product after the stabilization treatment is further humidified in the humidifier 76 in this example, sent to a storage hopper, and stored therein. In this humidifier 76, water is supplied to a water content of 30% in this example.
The stabilization process in the low-temperature oxidizing atmosphere processing furnace 64 is performed in the air atmosphere.
[0061]
In the low-temperature oxidizing atmosphere processing furnace 64, it is necessary to raise and maintain the internal atmospheric temperature to a predetermined temperature.
Therefore, in this example, the heat of the exhaust gas from the carbonization furnace 18 is recovered and supplied to the low-temperature oxidizing atmosphere processing furnace 64 as hot air.
More specifically, here, the air taken in from the air inlet 67 is guided to the exhaust gas processing chamber 30 of the carbonization furnace 18 as shown in FIG. To supply it to the low-temperature oxidizing atmosphere processing furnace 64 through the supply path 72.
[0062]
However, if the air exchanged in the exhaust gas treatment chamber 30 is supplied as it is as hot air to the low-temperature oxidizing atmosphere treatment furnace 64, the temperature is too high. It is supplied to the low-temperature oxidizing atmosphere processing furnace 64 as hot air at a temperature of ° C.
[0063]
In this case, in order to control the temperature of the hot air supplied through the supply path 72, the temperature of the hot air in the supply path 72 is detected by the temperature detector 74, and the result is received from the air inlet 69 by the adjustment valve 54. Outside air intake is controlled.
[0064]
In addition, there are a screw feeder type, a case conveyor type, a rotary kiln type, a vibration type, and the like as a conveyance type of the carbonized product in the low-temperature oxidizing atmosphere processing furnace 64. desirable.
Further, as a method of controlling the temperature of the low-temperature oxidizing atmosphere processing furnace 64, the supply amount of the hot air itself can be controlled by controlling the rotation speed of the hot air fan 70.
[0065]
According to such a carbonization apparatus of this example, it is possible to effectively prevent a phenomenon in which the carbonized product subsequently generates heat and induces combustion.
Further, since the stabilization processing furnace is configured as the low-temperature oxidizing atmosphere processing furnace 64 and the carbonized product is subjected to the oxidation reaction processing under the atmospheric conditions, the equipment cost and the running cost can be reduced.
[0066]
Further, in this example, the carbonized product from the carbonizing furnace 18 is once cooled by the cooler 66 and then supplied to the low-temperature oxidizing atmosphere processing furnace 64, where the carbonized product is stabilized. It is possible to reliably prevent the carbonized product in the still high temperature state from burning in the presence of oxygen in the low temperature oxidizing atmosphere processing furnace 64.
[0067]
In addition, in this example, after stabilizing the carbonized product in the low-temperature oxidizing atmosphere treatment furnace 64, the carbonized product is further humidified by the humidifier 76. Combustion can be more reliably prevented.
[0068]
Further, in this example, when the inside of the low-temperature oxidizing atmosphere processing furnace 64 is heated to a predetermined temperature, heat is recovered from the high-temperature exhaust gas from the carbonization furnace 18 and is used. The fuel cost can be reduced and the running cost can be reduced as compared with the case of heating by the heat source.
[0069]
In addition, as a stabilization furnace for the carbonized product discharged from the carbonization furnace 18, in addition to the low-temperature oxidizing atmosphere treatment furnace 64, the carbonized product is maintained at a high temperature of 200 ° C. or more by maintaining the internal oxygen concentration at a predetermined value or less. It is also possible to configure as a stabilization furnace of another form in which a non-burning oxidation reaction is performed.
This is the same in the following embodiments.
[0070]
FIG. 3 shows another embodiment of the present invention.
In this example, water in a water tank 78 is guided to an exhaust gas treatment chamber 30 of a carbonizing furnace 18 by a water pump 80, steam is supplied to a low-temperature oxidizing atmosphere processing furnace 64, and the carbonized product is not burned by the steam heating. An oxidation reaction treatment is performed to stabilize.
The other points are basically the same as those in the above embodiment.
[0071]
According to the present example, the mist hitting the carbonized product in the low-temperature oxidizing atmosphere treatment furnace 64 can expand the pore surface area of the carbonized product effectively by volume expansion when the mist is gasified by heating. In other words, it becomes possible to obtain properties close to activated carbon with high activity.
[0072]
FIG. 4 shows still another embodiment of the present invention, which is an exhaust gas fan 46 for discharging hot air from the hot blast furnace 34 and an exhaust gas for discharging exhaust gas from the carbonization furnace 18 in FIG. Exhaust gas downstream of the fan 60 is supplied to the low-temperature oxidizing atmosphere processing furnace 64 through the supply path 81. At this time, the exhaust gas is diluted and cooled by taking in outside air from the air intake 69, and the temperature of about 60 ° C. This is an example in which the hot air having a temperature is supplied to a low-temperature oxidizing atmosphere processing furnace 64.
The exhaust gas from the low-temperature oxidizing atmosphere processing furnace 64 is discharged from the chimney 52 to the outside through the exhaust path 82.
Other points are basically the same as those of the embodiment of FIG.
[0073]
Also in this example, the thermal energy that has been conventionally released to the outside can be effectively used as a heat source for heating the low-temperature oxidizing atmosphere processing furnace 64, and the running cost in the low-temperature oxidizing atmosphere processing furnace 64 can be reduced.
[0074]
Although the embodiment of the present invention has been described in detail, this is merely an example, and the present invention can be configured in variously modified forms without departing from the spirit thereof.
[Brief description of the drawings]
FIG. 1 is a view showing an apparatus for carbonizing organic matter-containing sludge according to one embodiment of the present invention.
FIG. 2 is a diagram showing a configuration of a carbonization furnace in FIG.
FIG. 3 is a view showing a carbonizing apparatus according to another embodiment of the present invention.
FIG. 4 is a view showing a carbonizing apparatus according to still another embodiment of the present invention.
FIG. 5 is a diagram showing an example of a conventional carbonization apparatus.
FIG. 6 is an explanatory diagram for explaining the meaning of providing a stabilization furnace in the present invention.
[Explanation of symbols]
14 Drying furnace
18 Carbonization furnace
34 Hot air stove
38 Circulation
64 Low-temperature oxidizing atmosphere processing furnace (stabilization processing furnace)
66 Cooler
76 Humidifier

Claims (10)

(A) a drying furnace for drying the organic matter-containing sludge to a predetermined moisture state, (b) a carbonizing furnace for carbonizing the sludge dried in the drying furnace by dry distillation, and (c) a carbonizing treatment in the carbonizing furnace. An organic matter-containing sludge carbonization apparatus, comprising: a stabilization furnace for stabilizing the carbonized product after the non-combustion oxidation reaction of an active group having high activity with respect to the oxidation reaction of the carbonized product. . 2. The carbonization treatment apparatus for sludge containing organic matter according to claim 1, wherein the sludge is an organic sludge generated by wastewater treatment. The apparatus for carbonizing organic matter-containing sludge according to any one of claims 1 and 2, wherein the stabilization furnace is a low-temperature oxidation furnace for stabilizing the carbonized product by causing a low-temperature oxidation reaction. 4. The apparatus for carbonizing organic matter-containing sludge according to claim 3, wherein the low-temperature oxidation treatment furnace performs an oxidation reaction treatment within a temperature range of 60 ° C. to 200 ° C. 5. The cooler according to any one of claims 1 to 4, wherein the cooler cools the carbonized product after being carbonized in the carbonization furnace, and supplies the carbonized product cooled by the cooler to the stabilization furnace to stabilize the product. A carbonization treatment device for sludge containing organic matter, wherein the sludge treatment is performed. The apparatus for carbonizing organic matter-containing sludge according to any one of claims 1 to 5, further comprising a humidifier for humidifying the carbonized product discharged from the stabilization furnace. The stabilizing furnace according to any one of claims 1 to 6, wherein hot air generated by heat exchange with high-temperature exhaust gas from the carbonizing furnace is supplied to the stabilizing furnace as a heating source for the stabilizing furnace. An organic matter-containing sludge carbonization treatment apparatus characterized by the above-mentioned. The apparatus for carbonizing organic matter-containing sludge according to claim 7, wherein the hot air is supplied as steam containing steam to the stabilization furnace. A circulation path according to any one of claims 1 to 8, further comprising a hot-air stove for generating hot air for drying in the drying oven, and returning the hot air generated by the hot-air stove to the hot-air stove via the drying oven. Along with circulating and flowing along, a portion of the hot air from the hot blast stove is exchanged heat with the circulating hot air, and after further reducing the temperature to a predetermined temperature by introducing outside air, An organic matter-containing sludge carbonization apparatus characterized by being supplied to a stabilization furnace. A circulation path according to any one of claims 1 to 8, further comprising a hot-air stove for generating hot air for drying in the drying oven, and returning the hot air generated by the hot-air stove to the hot-air stove via the drying oven. While circulating the exhaust gas from the carbonizing furnace with the hot air circulating and circulating, and further lowering the temperature to a predetermined temperature by introducing outside air. A carbonization treatment device for sludge containing organic matter, characterized in that it is supplied to a sludge.

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