WO2011040644A1

WO2011040644A1 - Carbonizing device

Info

Publication number: WO2011040644A1
Application number: PCT/JP2010/067604
Authority: WO
Inventors: 護伊藤; 昭幸金子; 恵美竹内
Original assignee: Ito Mamoru; Kaneko Akiyuki; Takeuchi Megumi
Priority date: 2009-10-01
Filing date: 2010-09-30
Publication date: 2011-04-07
Also published as: JP2011094138A; KR20120091163A; US20140079598A1; CN102575170A; US20120325642A1

Abstract

Disclosed is a carbonizing device capable of eliminating the possibility of leakage of a carbonization gas to the outside of the device and the possibility of explosion of the gas. Specifically disclosed is a carbonizing device which comprises heating chambers (21 to 24) that heat an object to be processed so as to thermally decompose the object; preliminary chambers (11, 12) that are disposed between the heating chambers (21 to 24) and the outside of the device and that is used for carrying the object to be processed from the outside into the heating chambers (21 to 24) while the heating chambers (21 to 24) are substantially shielded from the outside; a plurality of cooling chambers (31 to 33) in which processes subsequent to the thermal decomposition of the object to be processed are performed; shielding doors (5) each closing the preliminary chambers (11, 12), the heating chambers (21 to 24), and the cooling chambers (31 to 33) aligned in series; a conveying means that opens and closes the shielding doors (5) and conveys the object to be processed; and exhaust pipes (3) that extract gas ejected from the preliminary chambers (11, 12), the heating chambers (21 to 24), and the cooling chambers (31 to 33). In the carbonizing device that carbonizes the object to be processed while the object to be processed sequentially passes through the preliminary chambers (11, 12), the heating chambers (21 to 24), and the cooling chambers (31 to 33), the preliminary chambers (11, 12) are kept unheated.

Description

炭素化装置Carbonizer

　本発明は、廃タイヤ、木材、その他廃棄物等の有機系の処理物を乾留して油、ガス、炭素化物等に再生する炭素化装置の改良に関する。 The present invention relates to an improvement in a carbonization apparatus for carbonizing organically processed products such as waste tires, wood, and other wastes to regenerate them into oil, gas, carbonized products and the like.

　例えばゴム、プラスチック等の有機系の処理物を加熱分解した際に発生する乾留ガスは、冷却器を通して油分が分離されるが、この冷却器にて液化されない低沸点成分を含む余剰ガスが生じ、この余剰ガスは臭気を持ち、そのままでは大気に放出できない。このため、従来の炭素化装置は、余剰ガスを消臭消煙装置（燃焼炉）で燃焼させて無害化するとともに、脱臭することが行われる。
　従来、この種の炭素化装置として、遮断扉を介して閉塞される複数の処理室が直列に並んで設けられ、各処理室にて搬入工程、予熱工程、熱分解（乾留）工程、冷却工程、搬出工程等が順に行われるものである（特許文献１参照）。
　特許文献１に開示されたシステムは、複数の加熱室の前段に、第一及び第ニの予備室を設け、第一加熱室に隣接する第二予備室では、ヒータによりコンテナ内の処理物が所定温度条件で予備加熱されていて、第一加熱室に入る前の処理物を予備加熱して、第一加熱室での加熱効率の向上が図られている。
特開２００８−２９１０７６号公報 For example, in the dry distillation gas generated when heat-decomposing organic processing products such as rubber and plastic, oil components are separated through a cooler, but surplus gas containing a low boiling point component that is not liquefied by the cooler is generated, This surplus gas has an odor and cannot be released into the atmosphere as it is. For this reason, in the conventional carbonization apparatus, excess gas is burned in a deodorizing and smoking apparatus (combustion furnace) to make it harmless, and deodorization is performed.
Conventionally, as this type of carbonization apparatus, a plurality of treatment chambers closed via a shut-off door are provided in series, and in each treatment chamber, a loading process, a preheating process, a pyrolysis (dry distillation) process, and a cooling process. The unloading process and the like are sequentially performed (see Patent Document 1).
The system disclosed in Patent Document 1 is provided with first and second spare chambers in front of a plurality of heating chambers, and in the second spare chamber adjacent to the first heating chamber, the processed material in the container is heated by a heater. The preheating is performed under a predetermined temperature condition, and the processed product before entering the first heating chamber is preheated to improve the heating efficiency in the first heating chamber.
JP 2008-291076 A

　しかしながら、特許文献１に開示された炭素化装置にあっては、第二予備室で予備加熱されているため、処理物の種類によっては、該処理物から乾留ガスが発生する恐れがあり、仮に乾留ガスが発生して、これが第一予備室を通り装置外に排出されると、爆発するリスクすら存在するものであり、非常に好ましくないものである。即ち、安全面から、多少の加熱効率の低下を招くとしても、少なくとも爆発するリスクが、完全に排除されるシステムである必要があるものである。 However, in the carbonization apparatus disclosed in Patent Document 1, since it is preheated in the second preliminary chamber, there is a risk that dry distillation gas may be generated from the processed material depending on the type of the processed material. If dry distillation gas is generated and discharged outside the apparatus through the first preliminary chamber, there is even a risk of explosion, which is very undesirable. That is, from the viewpoint of safety, even if the heating efficiency is slightly reduced, it is necessary that the system at least eliminates the risk of explosion.

　本発明は上記の問題点に鑑みてなされたものであり、乾留ガスが装置外に漏出してこれが爆発する可能性を排除することのできる炭素化装置を提供することを目的とする。
　本発明は、処理物を加熱して熱分解する加熱室と、該加熱室と外部との間に設けられ、該加熱室と外部との間を実質的に遮蔽した状態で、前記処理物を外部から前記加熱室に搬入するための予備室と、処理物を熱分解した後の処理が行われる複数の冷却室と、直列に並ぶ各予備室と加熱室と各冷却室をそれぞれ閉塞する遮断扉と、遮断扉を開閉して処理物を搬送する搬送手段と、各予備室と加熱室と各冷却室から排出されるガスを取り出す排気管とを備え、処理物を前記予備室、加熱室、冷却室を順次通過させる中で、炭素化する炭素化装置において、前記予備室は非加熱の状態に維持されていることを特徴としている。
　また、前記搬送手段は、前記処理物が入れられるコンテナと、該コンテナを搬送するコンベアとを備えることを特徴としている。
３．　また、本発明は、コンテナに入れられた処理物を少なくとも加熱室を通過させることで炭素化することを特徴としている。
　また、前記コンテナは、上面が開口し、底部と四方を囲む側壁部とからなる箱体と、前記底部に対して傾斜を設けて配置され、前記処理物が載置される処理物載置部を有することを特徴としている。
　また、前記側壁部の一組の面の一方面に、前記処理物載置部へ前記処理物を投入する投入孔が設けられ、前記側壁部の一組の面の他方面に通気孔が設けられていることを特徴としている。
　また、前記通気孔と前記処理物載置部との間に、投入された前記処理物の前記通気孔からの落下を防止する段差が設けられていることを特徴としている。 This invention is made | formed in view of said problem, and it aims at providing the carbonization apparatus which can exclude the possibility that dry distillation gas will leak out of an apparatus and this may explode.
The present invention provides a heating chamber that heats and decomposes a processed material, and between the heating chamber and the outside, and the processed material is substantially shielded between the heating chamber and the outside. A preliminary chamber for carrying in the heating chamber from the outside, a plurality of cooling chambers in which processing is performed after pyrolyzing the processed material, and a block for closing each of the preliminary chambers, heating chambers and cooling chambers arranged in series. A door, a transfer means that opens and closes the shut-off door to transfer the processed material, and each preliminary chamber, a heating chamber, and an exhaust pipe that extracts gas discharged from each cooling chamber, and the processed material is disposed in the preliminary chamber and the heating chamber. In the carbonization apparatus that performs carbonization while sequentially passing through the cooling chamber, the preliminary chamber is maintained in an unheated state.
Moreover, the said conveyance means is equipped with the container in which the said processed material is put, and the conveyor which conveys this container, It is characterized by the above-mentioned.
3. In addition, the present invention is characterized in that the processed material put in the container is carbonized by passing it through at least a heating chamber.
In addition, the container has a box having an opening on the upper surface and a bottom and a side wall that surrounds the four sides, and a processing object mounting unit on which the processing object is mounted, and the container is disposed with an inclination with respect to the bottom. It is characterized by having.
In addition, an insertion hole is provided on one surface of the pair of surfaces of the side wall portion, and an air hole is provided on the other surface of the pair of surfaces of the side wall portion. It is characterized by being.
Further, a step is provided between the vent hole and the processing object mounting portion to prevent the thrown-in processing object from dropping from the vent hole.

　第１図は、本発明の実施の形態を示す炭素化装置のシステム図。
　第２図は、同じく図１の一部を拡大したシステム図。
　第３図は、同じく図１の一部を拡大したシステム図。
　第４図は、同じく図１の一部を拡大したシステム図。
　第５図は、同じく油分回収器の断面図。
　第６図は、同じく安全器の断面図。
　第７図は、本発明の炭素化装置で用いられるコンテナの斜視断面図。
　第８図は、本発明の炭素化装置で用いられる別のコンテナの斜視断面図。 FIG. 1 is a system diagram of a carbonization apparatus showing an embodiment of the present invention.
FIG. 2 is an enlarged system view of a part of FIG.
FIG. 3 is an enlarged system view of a part of FIG.
FIG. 4 is an enlarged system view of a part of FIG.
FIG. 5 is a cross-sectional view of the oil content recovery device.
FIG. 6 is a sectional view of the safety device.
FIG. 7 is a perspective sectional view of a container used in the carbonization apparatus of the present invention.
FIG. 8 is a perspective sectional view of another container used in the carbonization apparatus of the present invention.

　以下、本発明を廃棄される有機物を熱分解して炭素化する炭素化装置に適用した実施の形態を添付図面に基づいて説明する。
　図１~４に示すように、本実施例の炭素化装置は、炭素化工程の流れ方向に沿って第一、第二予備室１１、１２、第一~第四加熱室（炭素化室）２１~２４、第一~第三冷却室３１~３３が直列に並んで設けられる。
　図１に矢印で示すように、第一予備室１１に投入された処理物（被炭素化物）が第二予備室１２を経て、各処理室２１~２４、３１~３３に順に搬送され、後述するように各処理室２１~２４、３１~３３にて処理物中の有機物を炭素化するための処理が順に行われ、第三冷却室３３から炭素化物が取り出される。
　なお、予備室１１，１２及び各処理室２１~２４、３１~３３の設置数はこれに限らず、要求される処理能力等に応じて増減しても良い。例えば、４つの第一~第四加熱室２１~２４に限らず、３つ以下、または５つ以上の加熱室を設けても良い。
　炭素化装置は、搬送手段として処理物が入れられるコンテナ１００と、このコンテナ１００を搬送するコンベアを備える。このコンベアは各処理室１１、１２、２１~２４、３１~３３の内外に渡って延び、コンテナ１００を矢印で示す流れ方向（略水平方向）に搬送するようになっている。
　炭素化装置は、各予備室１１，１２と各処理室２１~２４、３１~３３を開閉する手段として、１０枚の遮断扉５を備える。各遮断扉５は図示しない駆動機構を介して昇降し、所定の開位置に引き上げられると各予備室１１，１２と各処理室２１~２４、３１~３３の出入口を開き、コンベアを介して搬送されるコンテナ１００が通過できるようにする一方、所定の閉位置に引き下げられ各予備室１１，１２と各処理室２１~２４、３１~３３をそれぞれ密閉するようになっている。
　各予備室１１，１２と各処理室２１~２４、３１~３３には窒素ガスを注入する窒素ガス注入管２と、室内のガスを排出する排気管３を備える。窒素ガス注入管２を介して窒素ガスが注入されるとともに、室内のガスが排気管３を介して強制的に排出する窒素置換によって低酸素濃度雰囲気を形成するようになっている。
　第一~第四加熱室２１~２４は炭素化工程の流れ方向について中央部に並んで設けられる。第一~第四加熱室２１~２４では図示しないヒータによりコンテナ１００内の処理物が所定温度条件（例えば３６０℃~４５０℃程度）で加熱され、処理物を低酸素濃度雰囲気にて燃焼させることなく熱分解（乾留）して炭素化する。第一~第四加熱室２１~２４ではこの熱分解によって処理物から高熱量の乾留ガスが発生し、窒素置換により第一~第四加熱室２１~２４から排気管３へと排出されるガスにおける可燃成分の濃度は高いものとなる。
　こうして第一~第四加熱室２１~２４では処理物を熱分解する炭素化処理が行われる。一方、本実施例においては、予備室１１，１２は非加熱の状態が維持されているので、各予備室１１，１２では処理物の熱分解は行われず、この結果、処理物から乾留ガスも発生しない状態となる。
　第二予備室１２は第一加熱室２１と第一加熱室２１との間に配置され、遮断扉５を開閉してコンテナ１００が第二予備室１２から第一加熱室２１に搬入される。この第二予備室１２では窒素置換が行われる。
　第二予備室１２では非加熱状態に維持されているので、処理物から乾留ガスは全く発生しない状態が維持されるが、遮断扉５の開閉時に隣接する第一加熱室２１内の乾留ガスが流入し、窒素置換により第二予備室１２から排気管３へと排出されるガスにおける可燃成分の濃度はある程度高いものとなる。
　第一予備室１１は炭素化工程の流れ方向について最前部に配置され、遮断扉５を開閉してコンテナ１００が第一予備室１１に搬入され、窒素置換が行われる。
　第一予備室１１は第二予備室１２の手前に配置され、遮断扉５を開閉してコンテナ１００が第一予備室１１から第二予備室１２に搬入される。この第一予備室１１では処理物の熱分解が行われないため処理物から乾留ガスは発生せず、遮断扉５の開閉時に隣接する第二予備室１２内に残留する少量の乾留ガスが流入するが、窒素置換により第一予備室１１から排気管３へと排出されるガスにおけるガス中の可燃成分の濃度は低いものとなる。
　第一~第四加熱室２１~２４の後方には熱分解した後の処理が行われる冷却室として第一~第三冷却室３１~３３が設けられる。
　第一冷却室３１は第四加熱室２４の後方に配置され、遮断扉５を開閉してコンテナ１００が第四加熱室２４から第一冷却室３１に搬入される。この第一冷却室３１では処理物の一段目の冷却が行われ、余熱により処理物から乾留ガスが発生すると共に、遮断扉５の開閉時に隣接する第四加熱室２４の乾留ガスが流入し、第一冷却室３１から排気管３へと排出されるガスにおける可燃成分の濃度はある程度高いものとなる。
　第二冷却室３２は第一冷却室３１の後方に配置され、遮断扉５を開閉してコンテナ１００が第一冷却室３１から第二冷却室３２に搬入される。この第二冷却室３２では処理物の二段目の冷却が行われ、余熱により処理物から乾留ガスはほとんど発生せず、遮断扉５の開閉時に隣接する第一冷却室３１内に残留する少量の乾留ガスが流入するが、窒素置換により第二冷却室３２から排気管３へと排出されるガスにおける可燃成分の濃度は低いものとなる。
　第三冷却室３３は第二冷却室３２の後方に配置され、遮断扉５を開閉してコンテナ１００が第二冷却室３２から第三冷却室３３に搬入される。この第三冷却室３３では処理物の三段目の冷却が行われ、余熱により処理物から乾留ガスはほとんど発生せず、遮断扉５の開閉時に隣接する第二冷却室３２内に残留するごく少量の乾留ガスが流入するが、窒素置換により第三冷却室３３から排気管３へと排出されるガスにおける可燃成分の濃度は低いものとなる。
　第三冷却室３３は炭素化工程の流れ方向について最後部に配置され、遮断扉５を開閉してコンテナ１００が第三冷却室３３から外部へと搬出される。
　第一~第四加熱室２１~２４では処理物の熱分解時に、処理物から高熱量の乾留ガスが発生し、この乾留ガスは炭化水素系の可燃成分を大量に含んでおり、排気管３を介して冷却器６にて冷却されることによりこの可燃成分が液化して可燃性の油が回収されるが、冷却器６を通過した余剰ガスには低沸点で液化しなかった可燃成分が含まれ、この余剰ガスは例えば千~１万ｋｃａｌ／ｍ^３程度の熱量を持つ。
　第二予備室１２では非加熱状態に維持されているので、処理物から乾留ガスは全く発生しないが、遮断扉５の開閉時に隣接する第一加熱室２１内の乾留ガスが流入しており、第二予備室１２から排出されるガスは排気管３を介して冷却器６にて冷却されることによりこの可燃成分が液化して可燃性の油が回収され、冷却器６を通過した余剰ガスには低沸点で液化しなかった可燃成分がある程度含まれる。
　第一冷却室３１では処理物の冷却時に、余熱により乾留ガスが発生するとともに、遮断扉５の開閉時に隣接する第四加熱室２４の乾留ガスが流入しており、第一冷却室３１から排出されるガスは排気管３を介して冷却器６にて冷却されることによりこの可燃成分が液化して可燃性の油が回収され、冷却器６を通過した余剰ガスには低沸点で液化しなかった可燃成分がある程度含まれる。
　各処理室１１、３２、３３から排出されるガスを処理する設備として、ガスの逆流を止める安全器８と、ガスを燃焼させる第一消臭消煙装置５１とを備える。
　各処理室１２、２１~２４、３１から排出されるガスを処理する設備として、ガスを冷却して油分を分離する冷却器６と、余剰ガスに含有される油分を回収する油分回収器７と、ガスの逆流を止める安全器８、９と、ガスを燃焼させる第二消臭消煙装置６１とを備える。
　本実施の形態では、２基の第二消臭消煙装置６１と１基の第一消臭消煙装置５１が設けられているが、これに限らず、これらの設置数は要求される処理能力等に応じて増減しても良い。
　第一予備室１１と第二冷却室３２と第三冷却室３３から排出される可燃成分の少ないガスは第一排気通路５０を通って第一消臭消煙装置５１に導入され、第一消臭消煙装置５１の高温雰囲気にて消臭消煙され、第一消臭消煙装置５１の排熱筒５５から外部に排出される。
　第一予備室１１、第二冷却室３２、第三冷却室３３から延びる各排気管３は一つの安全器８に接続され、この安全器８を通過したガスが第一排気通路５０を通って第一消臭消煙装置５１に導かれる。すなわち、第一予備室１１、第二冷却室３２、第三冷却室３３のガスが第一消臭消煙装置５１へと導かれる経路には冷却器と油分回収器が設けられていない。
　安全器８は後述する安全器９（図６参照）と同様の構造を持ち、これに溜められた水によって第一消臭消煙装置５１からのバックファイヤを止める働きをする。安全器８には後述する一次油タンク４１、各二次油タンク４２、各遠心分離機９７、清浄油タンク４３、屋内タンク４７、オーバーフロー受けタンク４４からのガスも導入される。
　第一排気通路５０には吸引ファン５６が介装され、この吸引ファン５６を介してガスが第一消臭消煙装置５１に送り込まれる。
　第一消臭消煙装置５１は、ガスを滞留させる燃焼炉５４と、この燃焼炉５４内に臨む燃焼炉内温度保持用のバーナ５３と、燃焼炉５４内で燃焼したガスを外部に排出する排熱筒５５とを備える。
　燃焼炉内温度保持用のバーナ５３は、燃焼炉５４内の出口寄りに設けられ、これに供給される燃料を燃焼炉５４内で燃焼し、燃焼炉５４内を所定温度（例えば８００℃程度）に保つようになっている。
　第一消臭消煙装置５１は、その燃焼炉５４を所要のガス滞留時間が得られる容量とし、ガス（乾留ガス＋窒素）が燃焼炉５４内の高温雰囲気を通過することにより、ガスの消臭処理が効率良く行われる。
　第二予備室１２、第一~第四加熱室２１~２４、第一冷却室３１から排出される可燃成分の多いガスは第二排気通路６０を通って第二消臭消煙装置６１に導入され、第二消臭消煙装置６１で燃焼後、高温雰囲気にて消臭消煙され、第二消臭消煙装置６１の排熱筒６５から外部に排出される。
　一方、第二予備室１２、第一~第四加熱室２１~２４、第一冷却室３１からのガスをそれぞれ排出する排気管３には冷却器６と油分回収器７と安全器９がそれぞれ直列に介装される。
　第二予備室１２、第一~第四加熱室２１~２４、第一冷却室３１から排気管３を通して排出される乾留ガスは各冷却器６にて冷却され、乾留ガスに含まれる油分が液化する。
　冷却器６は、冷却水が流れる冷却水配管群と、乾留ガスが通過するガス管のまわりを冷却水が循環する熱交換部とを備え、乾留ガスをこれらによって冷却して乾留ガスから液化した油や硫黄分等のスラッジを回収する。
　各冷却器６にて液化した油が配管１５を通して一次油タンク４１に送られ、この一次油タンク４１の油が配管１６と各送油ポンプ２６を介して３基の二次油タンク（油タンク）４２に送られ、各二次油タンク４２の油が各配管１７と各送油ポンプ２７を介して清浄油タンク４３に送られて貯留される。
　一次油タンク４１、各二次油タンク４２、４３からオーバーフローした油を貯留するオーバーフロー受けタンク４４が設けられる。一次油タンク４１からオーバーフローした油が配管３５を通してオーバーフロー受けタンク４４に送られ、二次油タンク４２からオーバーフローした油が配管３６を通してオーバーフロー受けタンク４４に送られ、清浄油タンク４３からオーバーフローした油が配管１９を通してオーバーフロー受けタンク４４に送られる。オーバーフロー受けタンク４４の油が配管３７と送油ポンプ３８を介して一次油タンク４１に戻される。
　地下タンク４６、屋内タンク４７には例えばＡ重油等の燃料油が各々れ貯留される。屋内タンク４７からオーバーフローした油が配管４９を通して地下タンク４６に送られる。地下タンク４６の油が送油ポンプ４８を介して屋内タンク４７に戻される。
　屋内タンク４７の油と清浄油タンク（燃料用タンク）４３の油は、燃料供給通路１８を通して第二消臭消煙装置６１の各燃焼炉バーナ６２、６３と、第一消臭消煙装置５１の燃焼炉バーナ５３に送られる。屋内タンク４７は切換弁５８を介して燃料供給通路１８に接続され、清浄油タンク（燃料用タンク）４３は切換弁５９を介して燃料供給通路１８に接続される。
　乾留開始時（清浄油タンク４３に清浄油が貯留されていない状態）および乾留中に清浄油タンク４３の清浄油が不足した際には、切換弁５９を閉じるとともに切換弁５８を開いて屋内タンク４７から重油を燃料供給通路１８を通して燃焼炉バーナ５３、６２、６３に供給する。清浄油タンク４３に清浄油が十分に貯留さると、切換弁５９を開くとともに切換弁５８を閉じて清浄油タンク４３から清浄油を燃料供給通路１８を通して燃焼炉バーナ５３、６２、６３に供給する。
　各安全器９、安全器８から取り出される廃水を貯留する廃水タンク４５が設けられる。廃水タンク４５には各安全器９からの廃水が配管６７を介して導かれるとともに、安全器８からの廃水が配管６８を介して導かれる。
　燃焼炉バーナ５３、６２、６３は水混合燃焼方式のものであり、清浄油タンク４３または屋内タンク４７から燃料供給通路１８を通って流量調整弁５７を介して供給される油と、廃水タンク４５から廃水供給通路６９を通って流量調整弁２０を介して供給される廃水を混合して燃焼させる。燃焼炉バーナ５３、６２、６３に供給される燃料油と水の量は適正な混合比となるように流量調整弁５７と流量調整弁２０の開度によって調整する。
　冷却器６を通過した余剰ガスは油分回収器７に送られ、余剰ガスに含まれる油とスラッジが回収される。油分回収器７にて回収された油とスラッジは配管１０を通して一次油タンク４１に送られる。
　油分回収器７は後述するように油分吸着液を溜め、この油分吸着液内に余剰ガスを通し、余剰ガス中に含まれる油が油分吸着液に触れることによって液化して回収される。油分回収器７にて油分吸着液上に出た余剰ガスが配管８を通して安全器９へと送られる。
　図５に示すように、油分回収器７は油分吸着液を溜める油分吸着液槽７５を備え、油分吸着液面上の空間が２枚の隔壁７９によって３つのガス室７６~７８に仕切られ、各ガス室７６~７８の下方の油分吸着液内に余剰ガスを流出する３本のガス流入管７１~７３を備える。
　なお、ガス室７６~７８、ガス流入管７１~７３の本数は、これに限らず、要求される処理能力等に応じて任意に設定される。
　冷却器６を通過した余剰ガスはガス流入管７１を通って油分吸着液槽７５の油分吸着液内に流出し、油分吸着液面上のガス室７６に出た余剰ガスはガス流入管７２を通って油分吸着液槽７５の油分吸着液内に流出し、油分吸着液面上のガス室７７に出た余剰ガスはガス流入管７３を通って油分吸着液槽７５の油分吸着液内に流出し、油分吸着液面上のガス室７８に出た余剰ガスはガス流出管８５を通って流出する。ガス流出管８５を通って油分回収器７を出た余剰ガスは余剰ガス導入管８５を通って安全器９に導かれる。
　油分吸着液槽７５には各ガス流入管７１~７３から流出した後に浮上する余剰ガスの気泡を通過させて細かい気泡に分割する気泡分割手段８０としてガス通過板８１が設けられる。各ガス流入管７１~７３から大きな気泡となって流出する余剰ガスは油分吸着液中を浮上する過程でガス通過板８１を通過することにより細かい気泡となり、余剰ガスに含まれる油分が油分吸着液に接触し、液化して油分吸着液に混ざることが促される。
　ガス通過板８１は多数の***が所定の間隔で開口している。なお、気泡分割手段８０はガス通過板８１に限らず、例えばメッシュ材等を用いても良い。
　３枚のガス通過板８１が上下方向に並んで設けられ、各ガス通過板８１に各ガス流入管７１~７３の下端部が挿通される。なお、ガス通過板８１の枚数はこれに限らず、要求される処理能力等に応じて任意に設定される。
　各ガス流入管７２、７３のガス室７７に対する開口端上部に切り欠き状のガス取り入れ口８２が形成され、このガス取り入れ口８２に対峙するオイルミスト衝突板８３が固定される。これにより、ガス室７７のガスはオイルミスト衝突板８３を超えてガス取り入れ口８２から中継管８８へと流入する。油分吸着液槽７５の油分吸着液が泡だってガス室７７にオイルミストが発生するような場合、このオイルミストがオイルミスト衝突板８３に当たって液化することが促される。
　ガス流出管８５のガス室７７に対する開口端に対峙する円盤状のオイルミスト衝突板８６が設けられる。これにより、ガス室７７のガスはオイルミスト衝突板８６を迂回してガス流出管８５へと流入する。油分吸着液槽７５の油分吸着液が泡だってガス室７７にオイルミストが発生するような場合、このオイルミストがオイルミスト衝突板８６に当たって液化することが促される。
　油分吸着液槽７５はその下部に出口８７が開口し、この出口８７を開閉するバルブ８９が設けられる。油分吸着液槽７５は出口８７に向けて傾斜する底部８８を有し、油分吸着液中に含まれるスラッジが重力により底部８８を介して出口８７に集まり、バルブ８９が開かれるとスラッジが油分吸着液と共に配管１０を通して一次油タンク４１に送られる。
　油分吸着液槽７５には油分吸着液として屋内タンク４７からＡ重油が配管９１を通して送油ポンプ９２を介して供給される。油分吸着液槽７５には油分吸着液の液面レベルを検出する液面計（図示せず）が設けられる。検出される液面レベルが所定値より低い場合にバルブ９０を開いて、屋内タンク４７からＡ重油が油分吸着液槽７５に供給される。
　油分吸着液としてＡ重油が用いられるが、Ａ重油は余剰ガスの気泡を包む液体として適度な粘度が得られ、これより粘度の低い軽油等に比べて油分の回収率を高められることが実験により確認された。
　油分吸着液はＡ重油に限らず、他の燃料油または水を用いることが考えられる。しかし、油分吸着液として水を用いる場合、水に浮かぶ油分を回収するのに油水分離器等が必要となる。
　油分吸着液槽７５からオーバーフローする油分吸着液は排出管９５から流出し、配管１５を通して一次油タンク４１に送られる。
　油分回収器７を通過した余剰ガスは安全器９を経て第二消臭消煙装置６１に送られ、第二消臭消煙装置６１にて燃焼する。
　安全器９内には水が溜められ、この水によって第二消臭消煙装置６１から配管５０を通って逆流するガスの流れを遮断する。安全器９の水は余剰ガスの通過に伴って汚濁するため、定期的に配管６７を通して廃水タンク４５へ排出する。
　図６に示すように、安全器９は水を溜める水槽９３と、水槽９３内の水中に臨む余剰ガス導入管９４とを備える。余剰ガス導入管９４を通して導かれる余剰ガスは気泡となって水槽９３内の水中に流出し、水上に出た余剰ガスが配管５０を通して第二消臭消煙装置６１へと送られる。第二消臭消煙装置６１から配管５０を通って安全器９へと逆流するガスの流れは安全器９内に溜められた水によって止められる。第二消臭消煙装置６１から火炎が配管５０を通って伝播する火炎は安全器９に溜められた水によって遮断される。
　安全器９の水槽９３には配管６８を介して供給される水が溜められる。水槽９３からオーバーフローする排水は配管６７を通して廃水タンク４５に流出する。安全器９のメンテナンス時にバルブ３９を開いて水が抜き取られる。
　冷却器６、油分回収器７を流れる乾留ガスからスラッジが析出されるが、このスラッジは液化した油と共に配管１５を通して一次油タンク４１に送られ、一次油タンク４１から配管１６を通して二次油タンク４２に溜められる。
　二次油タンク４２にはこれに溜められる油を循環させる油循環回路９６が設けられ、油循環回路９６の途中に油に含まれるスラッジ等を分離除去する遠心分離機９７が設けられる。油循環回路９６は二次油タンク４２と遠心分離機９７を連通する複数の配管によって構成される。二次油タンク４２内の油が一方の配管を通して遠心分離機９７のポンプに吸い込まれ、遠心分離機９７から流出する油が他方の配管を通して二次油タンク４２に流下する。遠心分離機９７は遠心力によってこれを循環する油からスラッジを分離する。こうしてスラッジが分離されるスラッジ分離除去工程が終了した後に、送油ポンプ２７が駆動され、二次油タンク４２の油が配管１７を通して清浄油タンク４３に送られて貯留される。
　清浄油タンク４３の油を循環ポンプ９８を介して循環させる清浄油循環回路９９が設けられる。清浄油循環回路９９の吸込口は清浄油タンク４３の下部に接続される。循環ポンプ９８を駆動して清浄油タンク４３の油が清浄油循環回路９９を循環することにより、清浄油タンク４３の油に含まれるタール状物質が沈殿しないように撹拌される。これにより、清浄油タンク４３から燃料供給通路１８を通して各燃焼炉バーナ６２、６３、５３に送られる油にタール状物質が均一に混ざり、各燃焼炉バーナ６２、６３、５３にて油と共に燃焼する。
　第二排気通路６０には吸引ファン６６が介装され、この吸引ファン６６を介してガスが第二消臭消煙装置６１に送り込まれる。
　第二消臭消煙装置６１は、ガスを滞留させる燃焼炉６４と、この燃焼炉６４内に臨む可燃ガス点火用の小容量バーナ６２と、燃焼炉内温度保持用の大容量バーナ６３と、燃焼炉６４内で燃焼したガスを外部に排出する排熱筒６５とを備える。
　可燃ガス点火用の小容量バーナ６２は、燃焼炉６４内の入口寄りに設けられ、これに供給される燃料を燃焼炉６４内で燃焼し、燃焼炉６４内に流入するガス中に含まれる可燃成分に着火するようになっている。
　燃焼炉内温度保持用の大容量バーナ６３は、燃焼炉６４内の出口寄りに設けられ、これに供給される燃料を燃焼炉６４内で燃焼し、燃焼炉６４内を所定温度（例えば８００℃程度）以上に保つようになっている。
　第二消臭消煙装置６１は、ガス（乾留ガス＋窒素）の可燃成分を燃焼させて無害化するとともにガスの消臭をするものであり、ガスの可燃成分が燃焼するのに伴って燃焼炉６４内の温度が許容値（例えば千数百℃）を超えて高くならないように燃焼炉６４の容量を確保する。そして、燃焼炉６４は異常燃焼を防止するとともに、爆発を防止するようになっている。
　次に、本発明の炭素化装置で用いられるコンテナ１００について説明する。図７は、コンテナ１００の斜視断面図となっている。
　コンテナ１００は、上面１０３が開口し、底部１０４と四方を囲む側壁部１０５とからなる箱体１０２と、底部１０４に対して傾斜を設けて配置され、処理物が載置される複数の処理物載置部１１０を有している。
　また、側壁部１０５の一組の面の一方面１０６に、処理物載置部１１０へ処理物を投入する投入孔１１２が複数設けられ、側壁部１０５の一組の面の他方面１０７に通気孔１１４が複数設けられている。
　また、通気孔１１４と処理物載置部１１０の処理物が載置される側の面との間には、投入された処理物が通気孔１１４から落下することを防止する段差１１６が各々の処理物載置部１１０ごとに設けられている。
　なお、処理物載置部１１０の傾斜は、投入孔１１２の側から通気孔１１４の側に向かって下るように設けられている。また、処理物載置部１１０は、処理物の大きさや用途等に合わせて間隔を任意に設定できるようしても良いし、その取り付けも、はめ込み式や一体型等、種々の構成とすることが可能である。さらには、処理物載置部１１０は、熱伝導性の高い材質を利用したり、処理物載置部１１０にヒータ等を設置したり等、本願発明の目的を逸脱しない範囲で、種々変形可能であることは言うまでもない。
　一般に、処理物載置部１１０を有しないコンテナでは、該コンテナ内に投入された処理物が山状に盛り上げられてしまい、伝熱面積が小さい、即ち、ヒータからの熱を伝える低酸素濃度雰囲気（窒素雰囲気）と処理物との接触面積が小さくなるため、熱が投入された処理物の内部までうまく伝わらない状態となっていた。このため、このような処理物載置部１１０を有しないコンテナでは、コンテナに投入する処理物を少なくしたり、または、手作業で処理物をならしたりすること等が必要であった。
　しかしながら、上記にて説明した構成を有するコンテナ１００においては、処理物を投入孔１１２から投入するだけで、処理物が処理物載置部１１０の傾斜に従い略均一にならされるため、処理物に対して効率的にヒータの熱が伝えられることとなる。
　また、投入孔１１２が設けられた側壁部１０５の一組の面の一方面１０６に向かい合う、側壁部１０５の一組の面の他方面１０７に設けられた通気孔１１４により、低酸素濃度雰囲気（窒素雰囲気）が投入孔１１２と通気孔１１４との間を通過することが可能となっているので、処理物が効率よく加熱される。
　さらに、通気孔１１４の側に設けられた段差１１６は、処理物の投入時に通気孔１１４から落下することを防止するだけでなく、加熱により熱分解されて流動化した処理物がコンテナ１００から流出して、コンテナ１００を搬送するコンベア等の装置の駆動部やその他の本発明の炭素化装置の各部に漏れ出ることも防止することが可能である。
　次に、本発明の炭素化装置で用いられる別のコンテナ２００について説明する。図８は、別のコンテナ２００の斜視断面図となっている。
　別のコンテナ２００は、上面２０３が開口し、底部２０４と四方を囲む側壁部２０５とからなる箱体２０２と、底部２０４に対して傾斜を設けて配置され、処理物が載置される複数の処理物載置部２１０を有している。
　なお、処理物載置部２１０の傾斜は、底部２０４に対して垂直以外の角度を持って設けられている。また、処理物載置部２１０は、処理物の大きさや用途等に合わせて間隔を任意に設定できるようしても良いし、その取り付けも、はめ込み式や一体型等、種々の構成とすることが可能である。さらには、処理物載置部２１０は、熱伝導性の高い材質を利用したり、処理物載置部２１０にヒータ等を設置したり等、本願発明の目的を逸脱しない範囲で、種々変形可能であることは言うまでもない。
　このような構成を有する別のコンテナ２００においては、処理物を上面２０３から投入するだけで、処理物が処理物載置部２１０の傾斜に従い略均一にならされるため、処理物に対して効率的にヒータの熱が伝えられることとなる。
　以上のように構成されて、次に作用及び効果について説明する。
　遮断扉５を介して密閉された第一~第四加熱室２１~２４にて有機物を無酸素状態で間接加熱することによって、有機物を乾留化して炭素化物が作られると共に、油分を含む乾留ガスが排気管３を通して取り出される。
　第一~第四加熱室２１~２４から取り出される高温の乾留ガスは冷却器６にて冷却され、乾留ガス中の油分が液化して回収される。
　冷却器６から取り出される余剰ガスはここで液化されなかった油分を含むが、この油分が油分回収器７に溜められた油分吸着液に触れることによって液化し、この液化した油が油分吸着液に取り込まれて回収される。
　油分回収器７にて油分が十分に除去された余剰ガスが安全器９に送られることにより、安全器９に溜められた水に油分が液化して浮かぶことを抑えられ、廃水タンク４５を介して水混合燃焼方式の各燃焼炉バーナ６２、６３、５３に供給される水が不足することを防止できる。
　一方、安全器９を経て取り出される余剰ガスは第二消臭消煙装置６１に送られるが、安全器９を通過した余剰ガスに含まれる油分が低減されることにより、第二消臭消煙装置６１の入口に設けられるガス吸引ファンにて余剰ガスに含まれる油分が液化して外部に垂れ落ちることを防止できる。
　こうして第二予備室１２と第一~第四加熱室２１~２４と第一冷却室３１から排出される可燃成分の多いガスは第二排気通路６０を通って第二消臭消煙装置６１に導入され、第二消臭消煙装置６１にて燃焼するとともに、第二消臭消煙装置６１の高温雰囲気にて消臭消煙され、第二消臭消煙装置６１の排熱筒６５から外部に排出される。
　本実施形態では、処理物を熱分解する加熱室に安全に渡すための搬送処理が行われる複数の予備室（第一、第二予備室１１、１２）と、処理物を加熱して熱分解する加熱室（第一~第四加熱室２１~２４）と、処理物を熱分解した後の処理が行われる複数の冷却室（第一~第三冷却室３１~３３）と、直列に並ぶ各予備室（第一、第二予備室１１、１２）と加熱室（第一~第四加熱室２１~２４）と各冷却室（第一~第三冷却室３１~３３）をそれぞれ閉塞する遮断扉５と、遮断扉５を開閉して処理物を搬送する搬送手段と、各予備室（第一、第二予備室１１、１２）と加熱室（第一~第四加熱室２１~２４）と各冷却室（第一~第三冷却室３１~３３）から排出されるガスを取り出す排気管３とを備え、処理物を前記予備室、加熱室、冷却室を順次通過させる中で、炭素化する炭素化装置において、前記予備室を非加熱の状態に維持しているので、処理物が予備室を通過する際において、予備室は非加熱の状態に維持されているので、該予備室の通過に伴い、処理物がここで加熱されることはない。
　この結果、予備室において該処理物から乾留ガスが発生する恐れは完全に排除され、従って、予備室で処理物を予熱することにより例え僅かでも想定されていた乾留ガスの発生は、完全に排除されることになる。このようにして、例え、予備室が装置外と流通する状態となったとしても、予備室で乾留ガスは発生しないのであるから、この乾留ガスが装置外に漏れ出る事も無く、従って、乾留ガスが爆発する危険は、完全に排除されることとなり、安全性が極めて高いレベルで担保されることになる。
　本発明は上記の実施の形態に限定されずに、本願発明の目的を逸脱しない範囲で、種々変形可能であることは言うまでもない。 Hereinafter, an embodiment in which the present invention is applied to a carbonization apparatus that thermally decomposes and carbonizes an organic substance to be discarded will be described with reference to the accompanying drawings.
As shown in FIGS. 1 to 4, the carbonization apparatus of the present embodiment includes first and second

preliminary chambers

11 and 12 and first to fourth heating chambers (carbonization chambers) along the flow direction of the carbonization process. 21 to 24 and first to third cooling chambers 31 to 33 are provided side by side in series.
As shown by the arrows in FIG. 1, the processed material (carbonized material) charged into the first preliminary chamber 11 is sequentially transferred to the processing chambers 21 to 24 and 31 to 33 through the second preliminary chamber 12, which will be described later. Thus, the treatment for carbonizing the organic matter in the treatment product is sequentially performed in the treatment chambers 21 to 24 and 31 to 33, and the carbonization product is taken out from the third cooling chamber 33.
The number of the

spare chambers

11 and 12 and the processing chambers 21 to 24 and 31 to 33 is not limited to this, and may be increased or decreased depending on the required processing capacity. For example, not limited to the four first to fourth heating chambers 21 to 24, three or less or five or more heating chambers may be provided.
The carbonization apparatus includes a container 100 in which a processed product is placed as a transport unit, and a conveyor that transports the container 100. The conveyor extends inside and outside the

processing chambers

11, 12, 21 to 24, and 31 to 33, and conveys the container 100 in the flow direction (substantially horizontal direction) indicated by an arrow.
The carbonization apparatus includes ten blocking doors 5 as means for opening and closing the

preliminary chambers

11 and 12 and the processing chambers 21 to 24 and 31 to 33. Each shut-off door 5 is raised and lowered via a drive mechanism (not shown), and when it is lifted to a predetermined open position, the entrances and exits of the

preliminary chambers

11 and 12 and the processing chambers 21 to 24 and 31 to 33 are opened and conveyed via a conveyor. The container 100 is allowed to pass, while being pulled down to a predetermined closed position, the

spare chambers

11 and 12 and the processing chambers 21 to 24 and 31 to 33 are sealed.
Each of the

preliminary chambers

11 and 12 and each of the processing chambers 21 to 24 and 31 to 33 is provided with a nitrogen gas injection pipe 2 for injecting nitrogen gas and an exhaust pipe 3 for discharging the indoor gas. Nitrogen gas is injected through the nitrogen gas injection pipe 2 and a low oxygen concentration atmosphere is formed by nitrogen replacement in which the indoor gas is forcibly discharged through the exhaust pipe 3.
The first to fourth heating chambers 21 to 24 are provided side by side in the center in the flow direction of the carbonization process. In the first to fourth heating chambers 21 to 24, the processed material in the container 100 is heated at a predetermined temperature condition (for example, about 360 ° C. to 450 ° C.) by a heater (not shown), and the processed material is burned in a low oxygen concentration atmosphere. Instead, pyrolyze (dry distillation) and carbonize. In the first to fourth heating chambers 21 to 24, a high-calorie dry distillation gas is generated from the processed material by this pyrolysis, and the gas discharged from the first to fourth heating chambers 21 to 24 to the exhaust pipe 3 by nitrogen replacement. The concentration of the combustible component in is high.
In this way, in the first to fourth heating chambers 21 to 24, the carbonization treatment for thermally decomposing the processed material is performed. On the other hand, in the present embodiment, since the

preliminary chambers

11 and 12 are maintained in an unheated state, the thermal treatment of the processed products is not performed in the

preliminary chambers

11 and 12, and as a result, dry distillation gas is also generated from the processed products. It does not occur.
The second preliminary chamber 12 is disposed between the first heating chamber 21 and the first heating chamber 21, and the container 100 is carried into the first heating chamber 21 from the second preliminary chamber 12 by opening and closing the blocking door 5. Nitrogen replacement is performed in the second preliminary chamber 12.
Since the second preliminary chamber 12 is maintained in a non-heated state, a state in which no dry distillation gas is generated from the processed material is maintained. However, the dry distillation gas in the adjacent first heating chamber 21 is not closed when the shut-off door 5 is opened and closed. The concentration of the combustible component in the gas that flows in and is exhausted from the second preliminary chamber 12 to the exhaust pipe 3 by nitrogen replacement becomes high to some extent.
The first preliminary chamber 11 is disposed in the foremost part in the flow direction of the carbonization step, and the container 100 is carried into the first preliminary chamber 11 by opening and closing the blocking door 5 to perform nitrogen replacement.
The first preliminary chamber 11 is disposed in front of the second preliminary chamber 12, and the container 100 is carried into the second preliminary chamber 12 from the first preliminary chamber 11 by opening and closing the blocking door 5. In the first preliminary chamber 11, no pyrolysis gas is generated from the processed material because pyrolysis of the processed material is not performed, and a small amount of dry distillation gas remaining in the adjacent second preliminary chamber 12 flows in when the shut-off door 5 is opened and closed. However, the concentration of the combustible component in the gas in the gas discharged from the first preliminary chamber 11 to the exhaust pipe 3 due to nitrogen substitution is low.
Behind the first to fourth heating chambers 21 to 24, first to third cooling chambers 31 to 33 are provided as cooling chambers in which processing after thermal decomposition is performed.
The first cooling chamber 31 is disposed behind the fourth heating chamber 24, opens and closes the blocking door 5, and the container 100 is carried into the first cooling chamber 31 from the fourth heating chamber 24. In the first cooling chamber 31, the first stage cooling of the processed material is performed, and the dry distillation gas is generated from the processed material due to the residual heat, and the dry distillation gas of the adjacent fourth heating chamber 24 flows in when the shut-off door 5 is opened and closed. The concentration of the combustible component in the gas discharged from the first cooling chamber 31 to the exhaust pipe 3 becomes high to some extent.
The second cooling chamber 32 is disposed behind the first cooling chamber 31, opens and closes the blocking door 5, and the container 100 is carried into the second cooling chamber 32 from the first cooling chamber 31. In the second cooling chamber 32, the second stage cooling of the processed material is performed, and little carbonization gas is generated from the processed material due to residual heat, and a small amount remaining in the adjacent first cooling chamber 31 when the shut-off door 5 is opened and closed. However, the concentration of the combustible component in the gas discharged from the second cooling chamber 32 to the exhaust pipe 3 by nitrogen replacement is low.
The third cooling chamber 33 is disposed behind the second cooling chamber 32, opens and closes the blocking door 5, and the container 100 is carried into the third cooling chamber 33 from the second cooling chamber 32. In the third cooling chamber 33, the third stage of the processed product is cooled, and hardly any dry distillation gas is generated from the processed product due to the residual heat, and the remaining in the adjacent second cooling chamber 32 when the shut-off door 5 is opened and closed. A small amount of dry distillation gas flows in, but the concentration of combustible components in the gas discharged from the third cooling chamber 33 to the exhaust pipe 3 due to nitrogen replacement is low.
The 3rd cooling chamber 33 is arrange | positioned at the rearmost part with respect to the flow direction of a carbonization process, the door 100 is opened and closed, and the container 100 is carried out from the 3rd cooling chamber 33 outside.
In the first to fourth heating chambers 21 to 24, during the thermal decomposition of the processed material, a high-calorie dry distillation gas is generated from the processed material, and this dry distillation gas contains a large amount of hydrocarbon-based combustible components. This combustible component is liquefied and cooled to recover flammable oil by being cooled by the cooler 6 through the exhaust gas, but the surplus gas that has passed through the cooler 6 contains a combustible component that has not been liquefied at a low boiling point. This surplus gas is, for example, 1,000 to 10,000 kcal / m. ³ Has about the amount of heat.
Since the second preliminary chamber 12 is maintained in a non-heated state, no dry distillation gas is generated from the processed material, but the dry distillation gas in the adjacent first heating chamber 21 flows in when the shut-off door 5 is opened and closed. The gas discharged from the second preliminary chamber 12 is cooled by the cooler 6 through the exhaust pipe 3, whereby the combustible components are liquefied and the combustible oil is recovered, and surplus gas that has passed through the cooler 6. Contains some combustible components that have a low boiling point and have not liquefied.
In the first cooling chamber 31, dry distillation gas is generated due to residual heat when the processed material is cooled, and the dry distillation gas in the adjacent fourth heating chamber 24 flows in when the shut-off door 5 is opened and closed, and is discharged from the first cooling chamber 31. The combustible gas is cooled by the cooler 6 through the exhaust pipe 3 to liquefy this combustible component, and the combustible oil is recovered. The surplus gas that has passed through the cooler 6 is liquefied at a low boiling point. Contains some combustible components that were not present.
As equipment for processing the gas discharged from each processing

chamber

11, 32, 33, a safety device 8 that stops the backflow of the gas and a first deodorizing and smoke eliminating device 51 that combusts the gas are provided.
As equipment for processing the gas discharged from each of the

processing chambers

12, 21 to 24, 31, a cooler 6 that cools the gas and separates the oil content, and an oil content recovery device 7 that recovers the oil content contained in the surplus gas, , Safety devices 8 and 9 for stopping the backflow of gas, and a second deodorizing and smoke eliminating device 61 for burning the gas.
In the present embodiment, two second deodorizing and smoking devices 61 and one first deodorizing and smoking device 51 are provided. However, the present invention is not limited to this, and the number of installations is required. You may increase / decrease according to capability etc.
The gas having a small amount of combustible components discharged from the first preliminary chamber 11, the second cooling chamber 32, and the third cooling chamber 33 is introduced into the first deodorizing and smoke eliminating device 51 through the first exhaust passage 50. Deodorized and smoke is removed in the high temperature atmosphere of the odor and smoke eliminating device 51, and discharged from the exhaust heat cylinder 55 of the first odor and smoke eliminating device 51 to the outside.
Each exhaust pipe 3 extending from the first preliminary chamber 11, the second cooling chamber 32, and the third cooling chamber 33 is connected to one safety device 8, and the gas that has passed through the safety device 8 passes through the first exhaust passage 50. Guided to the first deodorizing and smoke eliminating device 51. That is, the cooler and the oil content recovery unit are not provided in the path through which the gas in the first preliminary chamber 11, the second cooling chamber 32, and the third cooling chamber 33 is led to the first deodorizing and smoke eliminating device 51.
The safety device 8 has the same structure as a safety device 9 (see FIG. 6) described later, and functions to stop the backfire from the first deodorizing and smoke eliminating device 51 by water stored in the safety device 8. Gases from a primary oil tank 41, each secondary oil tank 42, each centrifugal separator 97, a clean oil tank 43, an indoor tank 47, and an overflow receiving tank 44, which will be described later, are also introduced into the safety device 8.
A suction fan 56 is interposed in the first exhaust passage 50, and gas is sent to the first deodorizing and smoke eliminating device 51 through the suction fan 56.
The first deodorization and smoke eliminating device 51 discharges the gas burned in the combustion furnace 54, the burner 53 for holding the temperature in the combustion furnace facing the combustion furnace 54, and the gas burned in the combustion furnace 54 to the outside. And a heat exhaust cylinder 55.
The burner 53 for maintaining the temperature in the combustion furnace is provided near the outlet in the combustion furnace 54, and the fuel supplied thereto is combusted in the combustion furnace 54, and the combustion furnace 54 has a predetermined temperature (for example, about 800 ° C.). To keep on.
The first deodorizing and smoke eliminating device 51 uses the combustion furnace 54 as a capacity capable of obtaining a required gas residence time, and the gas (dry distillation gas + nitrogen) passes through the high temperature atmosphere in the combustion furnace 54, thereby eliminating the gas. Odor treatment is performed efficiently.
Gases containing a large amount of combustible components discharged from the second preliminary chamber 12, the first to fourth heating chambers 21 to 24, and the first cooling chamber 31 are introduced into the second deodorizing and smoke eliminating device 61 through the second exhaust passage 60. Then, after combustion in the second deodorization and smoke eliminating device 61, the smoke is deodorized and deodorized in a high temperature atmosphere, and is discharged to the outside from the exhaust heat cylinder 65 of the second deodorization and smoke eliminating device 61.
On the other hand, in the exhaust pipe 3 for discharging the gas from the second preliminary chamber 12, the first to fourth heating chambers 21 to 24, and the first cooling chamber 31, respectively, a cooler 6, an oil recovery unit 7 and a safety unit 9 are provided. It is inserted in series.
The dry distillation gas discharged from the second preliminary chamber 12, the first to fourth heating chambers 21 to 24 and the first cooling chamber 31 through the exhaust pipe 3 is cooled by each cooler 6, and the oil contained in the dry distillation gas is liquefied. To do.
The cooler 6 includes a cooling water pipe group through which cooling water flows and a heat exchange unit in which cooling water circulates around a gas pipe through which the dry distillation gas passes. The dry distillation gas is cooled by these to be liquefied from the dry distillation gas. Collect sludge such as oil and sulfur.
The oil liquefied in each cooler 6 is sent to the primary oil tank 41 through the pipes 15, and the oil in the primary oil tank 41 passes through the pipes 16 and the oil feed pumps 26 to form three secondary oil tanks (oil tanks). ) 42, and the oil in each secondary oil tank 42 is sent to the clean oil tank 43 via each pipe 17 and each oil feed pump 27 and stored.
An overflow receiving tank 44 for storing oil overflowed from the primary oil tank 41 and the

secondary oil tanks

42 and 43 is provided. Oil that has overflowed from the primary oil tank 41 is sent to the overflow receiving tank 44 through the pipe 35, and oil that has overflowed from the secondary oil tank 42 is sent to the overflow receiving tank 44 through the pipe 36, and the oil that has overflowed from the clean oil tank 43 It is sent to the overflow receiving tank 44 through the pipe 19. The oil in the overflow receiving tank 44 is returned to the primary oil tank 41 via the pipe 37 and the oil feed pump 38.
In the underground tank 46 and the indoor tank 47, for example, fuel oil such as A heavy oil is stored. Oil overflowed from the indoor tank 47 is sent to the underground tank 46 through the pipe 49. The oil in the underground tank 46 is returned to the indoor tank 47 via the oil feed pump 48.
The oil in the indoor tank 47 and the oil in the clean oil tank (fuel tank) 43 pass through the fuel supply passage 18 and the

combustion furnace burners

62 and 63 of the second deodorization and smoke removal device 61 and the first deodorization and smoke removal device 51. To the combustion furnace burner 53. The indoor tank 47 is connected to the fuel supply passage 18 via a switching valve 58, and the clean oil tank (fuel tank) 43 is connected to the fuel supply passage 18 via a switching valve 59.
When dry distillation starts (when clean oil is not stored in the clean oil tank 43) and when there is not enough clean oil in the clean oil tank 43 during dry distillation, the switching valve 59 is closed and the switching valve 58 is opened to open the indoor tank. Heavy oil is supplied from 47 through the fuel supply passage 18 to the

combustion furnace burners

53, 62, 63. When the cleaning oil is sufficiently stored in the cleaning oil tank 43, the switching valve 59 is opened and the switching valve 58 is closed to supply the cleaning oil from the cleaning oil tank 43 to the

combustion furnace burners

53, 62, 63 through the fuel supply passage 18. .
A waste water tank 45 for storing waste water taken out from each safety device 9 and safety device 8 is provided. Waste water from each safety device 9 is guided to the waste water tank 45 through the piping 67 and waste water from the safety device 8 is guided through the piping 68.
The

combustion furnace burners

53, 62, 63 are of the water mixed combustion type, and the oil supplied from the clean oil tank 43 or the indoor tank 47 through the fuel supply passage 18 through the flow rate adjusting valve 57 and the wastewater tank 45. The waste water supplied through the waste water supply passage 69 through the flow rate adjustment valve 20 is mixed and burned. The amount of fuel oil and water supplied to the

combustion furnace burners

53, 62, 63 is adjusted by the opening degree of the flow rate adjusting valve 57 and the flow rate adjusting valve 20 so as to obtain an appropriate mixing ratio.
The surplus gas that has passed through the cooler 6 is sent to the oil content collector 7 where oil and sludge contained in the surplus gas are recovered. The oil and sludge recovered by the oil recovery unit 7 are sent to the primary oil tank 41 through the pipe 10.
As will be described later, the oil content collector 7 accumulates an oil content adsorbing liquid, passes surplus gas into the oil content adsorbing liquid, and the oil contained in the surplus gas is liquefied and recovered by touching the oil content adsorbing liquid. The surplus gas that has come out on the oil adsorbent in the oil recovery unit 7 is sent to the safety unit 9 through the pipe 8.
As shown in FIG. 5, the oil recovery unit 7 includes an oil adsorbing liquid tank 75 for storing an oil adsorbing liquid, and a space on the oil adsorbing liquid surface is divided into three gas chambers 76 to 78 by two partition walls 79, Three gas inflow pipes 71 to 73 through which excess gas flows out into the oil adsorbing liquid below the gas chambers 76 to 78 are provided.
The numbers of the gas chambers 76 to 78 and the gas inflow pipes 71 to 73 are not limited to this, and are arbitrarily set according to the required processing capacity.
The surplus gas that has passed through the cooler 6 flows out into the oil adsorbing liquid in the oil adsorbing liquid tank 75 through the gas inflow pipe 71, and the surplus gas that has exited into the gas chamber 76 on the oil adsorbing liquid surface passes through the gas inflow pipe 72. It passes through the oil adsorbing liquid in the oil adsorbing liquid tank 75 and flows out into the gas adsorbing liquid in the oil adsorbing liquid tank 75 through the gas inflow pipe 73. Then, surplus gas that has exited into the gas chamber 78 on the surface of the oil adsorbing liquid flows out through the gas outflow pipe 85. The surplus gas that has left the oil recovery unit 7 through the gas outflow pipe 85 is guided to the safety device 9 through the surplus gas introduction pipe 85.
The oil adsorbing liquid tank 75 is provided with a gas passage plate 81 as a bubble dividing means 80 that allows excess gas bubbles that flow after flowing out from the gas inflow pipes 71 to 73 to pass through and divide into fine bubbles. The surplus gas flowing out as large bubbles from the gas inflow pipes 71 to 73 becomes fine bubbles by passing through the gas passage plate 81 in the process of rising in the oil adsorbing liquid, and the oil contained in the surplus gas becomes the oil adsorbing liquid. Is liquefied and mixed with the oil adsorbing liquid.
The gas passage plate 81 has a large number of small holes opened at predetermined intervals. The bubble dividing means 80 is not limited to the gas passage plate 81 but may be a mesh material, for example.
Three gas passage plates 81 are provided side by side in the vertical direction, and the lower end portions of the gas inflow pipes 71 to 73 are inserted into the gas passage plates 81. The number of gas passage plates 81 is not limited to this, and may be arbitrarily set according to the required processing capacity.
A notch-like gas intake port 82 is formed at the upper opening end of each gas inflow pipe 72, 73 with respect to the gas chamber 77, and an oil mist collision plate 83 facing the gas intake port 82 is fixed. Thereby, the gas in the gas chamber 77 flows from the gas intake port 82 to the relay pipe 88 beyond the oil mist collision plate 83. When the oil adsorbing liquid in the oil adsorbing liquid tank 75 is a bubble and oil mist is generated in the gas chamber 77, the oil mist strikes the oil mist collision plate 83 to be liquefied.
A disk-shaped oil mist collision plate 86 is provided opposite to the opening end of the gas outflow pipe 85 with respect to the gas chamber 77. As a result, the gas in the gas chamber 77 bypasses the oil mist collision plate 86 and flows into the gas outflow pipe 85. When the oil adsorbing liquid in the oil adsorbing liquid tank 75 is a bubble and oil mist is generated in the gas chamber 77, the oil mist strikes the oil mist collision plate 86 and is liquefied.
The oil adsorbing liquid tank 75 has an outlet 87 opened at a lower portion thereof, and a valve 89 for opening and closing the outlet 87 is provided. The oil adsorbing liquid tank 75 has a bottom portion 88 that is inclined toward the outlet 87, and sludge contained in the oil adsorbing liquid gathers at the outlet 87 through the bottom portion 88 due to gravity, and the sludge is adsorbed when the valve 89 is opened. It is sent to the primary oil tank 41 through the pipe 10 together with the liquid.
A heavy oil A is supplied from the indoor tank 47 through the pipe 91 to the oil adsorbing liquid tank 75 through the oil feed pump 92 as an oil adsorbing liquid. The oil adsorbing liquid tank 75 is provided with a liquid level gauge (not shown) for detecting the liquid level of the oil adsorbing liquid. When the detected liquid level is lower than a predetermined value, the valve 90 is opened, and A heavy oil is supplied from the indoor tank 47 to the oil component adsorbing liquid tank 75.
A heavy oil is used as the oil adsorbing liquid, but A heavy oil has an appropriate viscosity as a liquid that wraps bubbles of excess gas, and it has been experimentally shown that the oil recovery rate can be increased compared to light oil or the like having a lower viscosity. confirmed.
It is conceivable that the oil adsorbing liquid is not limited to A heavy oil but other fuel oil or water. However, when water is used as the oil adsorbing liquid, an oil / water separator or the like is required to recover the oil floating in the water.
The oil adsorbing liquid overflowing from the oil adsorbing liquid tank 75 flows out from the discharge pipe 95 and is sent to the primary oil tank 41 through the pipe 15.
The surplus gas that has passed through the oil recovery unit 7 is sent to the second deodorizing and smoke eliminating device 61 through the safety device 9 and combusted in the second deodorizing and smoke eliminating device 61.
Water is stored in the safety device 9, and the flow of gas flowing backward from the second deodorizing and smoke eliminating device 61 through the pipe 50 is blocked by this water. Since the water in the safety device 9 is polluted with the passage of surplus gas, it is periodically discharged to the waste water tank 45 through the pipe 67.
As shown in FIG. 6, the safety device 9 includes a water tank 93 that stores water and a surplus gas introduction pipe 94 that faces the water in the water tank 93. The surplus gas guided through the surplus gas introduction pipe 94 becomes bubbles and flows out into the water in the water tank 93, and surplus gas discharged onto the water is sent to the second deodorizing and smoke eliminating device 61 through the pipe 50. The flow of gas that flows backward from the second deodorizing and smoke eliminating device 61 through the pipe 50 to the safety device 9 is stopped by the water stored in the safety device 9. The flame that propagates through the pipe 50 from the second deodorizing and smoke eliminating device 61 is blocked by water stored in the safety device 9.
Water supplied through a pipe 68 is stored in the water tank 93 of the safety device 9. Waste water overflowing from the water tank 93 flows out to the waste water tank 45 through the pipe 67. During maintenance of the safety device 9, the valve 39 is opened to drain water.
Sludge is deposited from the dry distillation gas flowing through the cooler 6 and the oil content collector 7, and this sludge is sent together with the liquefied oil to the primary oil tank 41 through the pipe 15, and from the primary oil tank 41 through the pipe 16 to the secondary oil tank. 42.
The secondary oil tank 42 is provided with an oil circulation circuit 96 that circulates oil accumulated therein, and a centrifuge 97 that separates and removes sludge and the like contained in the oil is provided in the middle of the oil circulation circuit 96. The oil circulation circuit 96 includes a plurality of pipes that communicate the secondary oil tank 42 and the centrifugal separator 97. The oil in the secondary oil tank 42 is sucked into the pump of the centrifuge 97 through one pipe, and the oil flowing out from the centrifuge 97 flows down to the secondary oil tank 42 through the other pipe. The centrifugal separator 97 separates sludge from the oil circulating through the centrifugal force. After the sludge separation and removal step in which the sludge is separated in this way, the oil feed pump 27 is driven, and the oil in the secondary oil tank 42 is sent to the clean oil tank 43 through the pipe 17 and stored.
A clean oil circulation circuit 99 that circulates the oil in the clean oil tank 43 via a circulation pump 98 is provided. The suction port of the clean oil circulation circuit 99 is connected to the lower part of the clean oil tank 43. The circulation pump 98 is driven and the oil in the clean oil tank 43 circulates through the clean oil circulation circuit 99, so that the tar-like substance contained in the oil in the clean oil tank 43 is stirred so as not to precipitate. As a result, the tar-like substance is uniformly mixed with the oil sent from the clean oil tank 43 through the fuel supply passage 18 to the

combustion furnace burners

62, 63, 53, and combusts with the oil in each

combustion furnace burner

62, 63, 53. .
A suction fan 66 is interposed in the second exhaust passage 60, and gas is sent to the second deodorizing and smoke eliminating device 61 through the suction fan 66.
The second deodorizing and smoke eliminating device 61 includes a combustion furnace 64 that retains gas, a small-capacity burner 62 for igniting combustible gas facing the combustion furnace 64, a large-capacity burner 63 for maintaining the temperature in the combustion furnace, And an exhaust heat cylinder 65 for discharging the gas burned in the combustion furnace 64 to the outside.
The small-capacity burner 62 for igniting the combustible gas is provided near the inlet in the combustion furnace 64, and the fuel supplied thereto is combusted in the combustion furnace 64 and combustible contained in the gas flowing into the combustion furnace 64. The ingredients are ignited.
A large-capacity burner 63 for maintaining the temperature in the combustion furnace is provided near the outlet in the combustion furnace 64, and the fuel supplied thereto is combusted in the combustion furnace 64, and the inside of the combustion furnace 64 is heated to a predetermined temperature (for example, 800 ° C.). Degree) or more.
The second deodorizing and smoke eliminating device 61 burns incombustible components of gas (dry distillation gas + nitrogen) and detoxifies the gases, and burns as the combustible components of the gas burn. The capacity of the combustion furnace 64 is ensured so that the temperature in the furnace 64 does not exceed a permissible value (for example, several hundreds of degrees Celsius). The combustion furnace 64 prevents abnormal combustion and prevents explosion.
Next, the container 100 used with the carbonization apparatus of this invention is demonstrated. FIG. 7 is a perspective sectional view of the container 100.
The container 100 has an upper surface 103 opened, a box body 102 having a bottom portion 104 and a side wall portion 105 surrounding the four sides, and a plurality of processing objects on which the processing object is placed. The mounting unit 110 is provided.
In addition, a plurality of input holes 112 are provided on one surface 106 of the pair of surfaces of the side wall portion 105 so as to input the processed material into the processed material mounting portion 110, and are passed through the other surface 107 of the pair of surfaces of the side wall portion 105. A plurality of pores 114 are provided.
In addition, there is a step 116 between the air hole 114 and the surface of the processing object mounting unit 110 on the side where the processing object is placed, which prevents the input processing object from falling from the air hole 114. It is provided for each processing object placing unit 110.
In addition, the inclination of the processing object mounting portion 110 is provided so as to be lowered from the charging hole 112 side toward the vent hole 114 side. In addition, the processing object mounting unit 110 may be configured so that the interval can be arbitrarily set according to the size and application of the processing object, and the mounting is also of various configurations such as a fitting type and an integral type. Is possible. Furthermore, the processing object mounting unit 110 can be variously modified without departing from the object of the present invention, such as using a material having high thermal conductivity or installing a heater or the like on the processing object mounting unit 110. Needless to say.
In general, in a container that does not have the processing object mounting unit 110, the processing object thrown into the container is raised in a mountain shape, and the heat transfer area is small, that is, a low oxygen concentration atmosphere that transfers heat from the heater. Since the contact area between the (nitrogen atmosphere) and the treated product is small, the heat treatment is not conducted well to the inside of the treated product. For this reason, in a container that does not have such a processed material placement unit 110, it is necessary to reduce the amount of processed material that is put into the container, or to manually process the processed material.
However, in the container 100 having the configuration described above, the processing object is made substantially uniform according to the inclination of the processing object mounting unit 110 simply by charging the processing object through the charging hole 112. On the other hand, the heat of the heater is efficiently transmitted.
In addition, a low oxygen concentration atmosphere (by a vent hole 114 provided on the other surface 107 of the set of side walls 105 facing the one surface 106 of the set of surfaces of the side wall 105 provided with the introduction holes 112 is provided. Nitrogen atmosphere) can pass between the input hole 112 and the vent hole 114, so that the processed material is efficiently heated.
Further, the step 116 provided on the side of the vent hole 114 not only prevents falling from the vent hole 114 when the processing object is charged, but also the processing object thermally decomposed and fluidized by heating flows out of the container 100. Thus, it is possible to prevent leakage to a drive unit of a device such as a conveyor that conveys the container 100 and other parts of the carbonization device of the present invention.
Next, another container 200 used in the carbonization apparatus of the present invention will be described. FIG. 8 is a perspective sectional view of another container 200.
Another container 200 has an upper surface 203 open, a box body 202 having a bottom portion 204 and a side wall portion 205 that surrounds the four sides, and an inclination with respect to the bottom portion 204. A processing object placing unit 210 is provided.
In addition, the inclination of the workpiece placement unit 210 is provided with an angle other than perpendicular to the bottom 204. In addition, the processing object placing unit 210 may be configured to arbitrarily set the interval according to the size and application of the processing object, and the mounting thereof may be of various configurations such as a fitting type and an integral type. Is possible. Furthermore, the processing object mounting unit 210 can be variously modified without departing from the object of the present invention, such as using a material having high thermal conductivity, or installing a heater or the like on the processing object mounting unit 210. Needless to say.
In another container 200 having such a configuration, the processing object is made to be substantially uniform according to the inclination of the processing object mounting unit 210 just by charging the processing object from the upper surface 203, so that the efficiency with respect to the processing object is improved. Therefore, the heat of the heater is transmitted.
Next, the operation and effect will be described.
By indirectly heating the organic matter in an oxygen-free state in the first to fourth heating chambers 21 to 24 sealed through the shut-off door 5, the organic matter is carbonized to produce a carbonized product, and a carbonized gas containing oil Is taken out through the exhaust pipe 3.
The high-temperature dry distillation gas taken out from the first to fourth heating chambers 21 to 24 is cooled by the cooler 6, and the oil in the dry distillation gas is liquefied and recovered.
The surplus gas taken out from the cooler 6 contains the oil that has not been liquefied here, but this oil is liquefied by touching the oil adsorbed liquid stored in the oil recovering unit 7, and this liquefied oil becomes the oil adsorbed liquid. Captured and recovered.
The surplus gas from which the oil has been sufficiently removed by the oil recovery unit 7 is sent to the safety unit 9, whereby the oil component is prevented from being liquefied and floating in the water stored in the safety unit 9, and passed through the waste water tank 45. Therefore, it is possible to prevent a shortage of water supplied to each

combustion furnace burner

62, 63, 53 of the water mixed combustion system.
On the other hand, the surplus gas taken out through the safety device 9 is sent to the second deodorization and smoke eliminating device 61. By reducing the oil content contained in the surplus gas that has passed through the safety device 9, the second deodorization and smoke removal is performed. It is possible to prevent the oil contained in the surplus gas from being liquefied and dripping down by the gas suction fan provided at the inlet of the device 61.
Thus, the gas containing a large amount of combustible components discharged from the second preliminary chamber 12, the first to fourth heating chambers 21 to 24, and the first cooling chamber 31 passes through the second exhaust passage 60 to the second deodorizing and smoke eliminating device 61. Introduced and combusted in the second deodorant and smoke eliminating device 61, and deodorized and smoke eliminated in the high temperature atmosphere of the second deodorant and smoke eliminating device 61. It is discharged outside.
In the present embodiment, a plurality of preliminary chambers (first and second preliminary chambers 11 and 12) in which a conveyance process for safely passing to a heating chamber that thermally decomposes the processed material is performed, and the processed material is heated and pyrolyzed. The heating chambers (first to fourth heating chambers 21 to 24) to be processed and a plurality of cooling chambers (first to third cooling chambers 31 to 33) in which processing is performed after pyrolyzing the processing object are arranged in series. The preliminary chambers (first and second preliminary chambers 11 and 12), the heating chambers (first to fourth heating chambers 21 to 24), and the cooling chambers (first to third cooling chambers 31 to 33) are respectively closed. The shut-off door 5, the transfer means for opening and closing the shut-off door 5 and transferring the processed material, the respective spare chambers (first and second spare chambers 11 and 12), and the heating chamber (first to fourth heating chambers 21 to 24). ) And an exhaust pipe 3 for taking out gas discharged from each cooling chamber (first to third cooling chambers 31 to 33), and sequentially passes the processed material through the preliminary chamber, heating chamber, and cooling chamber. In the carbonization apparatus for carbonization, since the preliminary chamber is maintained in an unheated state, when the processed material passes through the preliminary chamber, the preliminary chamber is maintained in an unheated state. The processed material is not heated here as it passes through the preliminary chamber.
As a result, the possibility that dry distillation gas is generated from the processed material in the preliminary chamber is completely eliminated, and therefore, the generation of dry distillation gas, which is assumed even slightly by preheating the processed material in the preliminary chamber, is completely excluded. Will be. In this way, even if the spare chamber is in a state where it circulates outside the apparatus, no dry distillation gas is generated in the spare chamber, so that this dry distillation gas does not leak out of the apparatus. The risk of gas explosion is completely eliminated and the safety is guaranteed at a very high level.
It goes without saying that the present invention is not limited to the above-described embodiment, and various modifications can be made without departing from the object of the present invention.

　本発明によると、処理物が予備室を通過する際において、予備室は非加熱の状態に維持されているので、該予備室の通過に伴い、処理物がここで加熱されることはない。この結果、予備室において該処理物から乾留ガスが発生する恐れは完全に排除され、従って、予備室で処理物を予熱することにより例え僅かでも想定されていた乾留ガスの発生は、完全に排除されることになる。このようにして、例え、予備室が装置外と流通する状態となったとしても、予備室で乾留ガスは発生しないのであるから、この乾留ガスが装置外に漏れ出る事も無く、従って、乾留ガスが爆発する危険は、完全に排除されることとなり、安全性が極めて高いレベルで担保されることになる。
　また、本発明によると、処理物が入れられるコンテナの内部に設けられた処理物載置部が、処理物中の有機物を熱分解（乾留）して炭素化するための加熱処理の熱分解効率を向上することになる。 According to the present invention, when the processed material passes through the preliminary chamber, the preliminary chamber is maintained in an unheated state, so that the processed material is not heated here with the passage of the preliminary chamber. As a result, the possibility that dry distillation gas is generated from the processed material in the preliminary chamber is completely eliminated, and therefore, the generation of dry distillation gas, which is assumed even slightly by preheating the processed material in the preliminary chamber, is completely excluded. Will be. In this way, even if the spare chamber is in a state where it circulates outside the apparatus, no dry distillation gas is generated in the spare chamber, so that this dry distillation gas does not leak out of the apparatus. The risk of gas explosion is completely eliminated and the safety is guaranteed at a very high level.
In addition, according to the present invention, the thermal decomposition efficiency of the heat treatment for carbonizing the organic matter in the processed material by pyrolyzing (dry-distilling) the organic material in the processed material is provided in the container in which the processed material is placed. Will be improved.

Claims

　処理物を加熱して熱分解する加熱室と、該加熱室と外部との間に設けられ、該加熱室と外部との間を実質的に遮蔽した状態で、前記処理物を外部から前記加熱室に搬入するための予備室と、処理物を熱分解した後の処理が行われる複数の冷却室と、直列に並ぶ各予備室と加熱室と各冷却室をそれぞれ閉塞する遮断扉と、遮断扉を開閉して処理物を搬送する搬送手段と、各予備室と加熱室と各冷却室から排出されるガスを取り出す排気管とを備え、処理物を前記予備室、加熱室、冷却室を順次通過させる中で、炭素化する炭素化装置において、前記予備室を非加熱の状態に維持することを特徴とする炭素化装置。 A heating chamber that heats and decomposes the processed material, and the heating chamber and the outside are provided between the heating chamber and the outside. A spare chamber for carrying into the chamber, a plurality of cooling chambers in which processing is performed after pyrolyzing the processed material, a preliminary chamber, a heating chamber, and a shut-off door that respectively closes each cooling chamber, It includes a transport means for opening and closing the door to transport the processed material, and an exhaust pipe for extracting the gas discharged from each preliminary chamber, the heating chamber, and each cooling chamber, and the processed material is disposed in the preliminary chamber, the heating chamber, and the cooling chamber. In the carbonization apparatus that performs carbonization while sequentially passing, the preliminary chamber is maintained in an unheated state.
　前記搬送手段は、前記処理物が入れられるコンテナと、該コンテナを搬送するコンベアとを備えることを特徴とする請求項１に記載の炭素化装置。 2. The carbonization apparatus according to claim 1, wherein the transport unit includes a container in which the processed material is placed and a conveyor that transports the container.
　コンテナに入れられた処理物を少なくとも加熱室を通過させることで炭素化する炭素化装置。 A carbonization device that carbonizes the processed material in the container by passing it through at least the heating chamber.
　前記コンテナは、上面が開口し、底部と四方を囲む側壁部とからなる箱体と、前記底部に対して傾斜を設けて配置され、前記処理物が載置される処理物載置部を有することを特徴とする請求項２又は請求項３に記載の炭素化装置。 The container has a box body having an open top surface and a bottom portion and side wall portions surrounding the four sides, and a processing object mounting portion on which the processing object is mounted, and is disposed with an inclination with respect to the bottom portion. The carbonization apparatus of Claim 2 or Claim 3 characterized by the above-mentioned.
　前記側壁部の一組の面の一方面に、前記処理物載置部へ前記処理物を投入する投入孔が設けられ、前記側壁部の一組の面の他方面に通気孔が設けられていることを特徴とする請求項４に記載の炭素化装置。 An insertion hole is provided on one surface of the set of side wall portions to input the processing object to the processing object mounting portion, and a vent hole is provided on the other surface of the set of side wall portions. The carbonization apparatus of Claim 4 characterized by the above-mentioned.
　前記通気孔と前記処理物載置部との間に、投入された前記処理物の前記通気孔からの落下を防止する段差が設けられていることを特徴とする請求項５に記載の炭素化装置。 6. The carbonization according to claim 5, wherein a step is provided between the vent hole and the treatment object mounting portion to prevent the thrown-in treatment object from dropping from the vent hole. apparatus.