JPH11276856A - Treatment of dioxin-containing gas and device therefor - Google Patents
Treatment of dioxin-containing gas and device thereforInfo
- Publication number
- JPH11276856A JPH11276856A JP10081399A JP8139998A JPH11276856A JP H11276856 A JPH11276856 A JP H11276856A JP 10081399 A JP10081399 A JP 10081399A JP 8139998 A JP8139998 A JP 8139998A JP H11276856 A JPH11276856 A JP H11276856A
- Authority
- JP
- Japan
- Prior art keywords
- adsorbent
- dioxin
- fluidized bed
- adsorbed
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、ダイオキシン含有
ガスを吸着処理してダイオキシン除去ガスとし、ダイオ
キシンを吸着した吸着剤を酸化分解処理してダイオキシ
ンと使用済吸着剤の両者を処理する方法及び装置に関す
る。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and an apparatus for treating a dioxin-containing gas into a dioxin-removing gas by an adsorption treatment and an oxidative decomposition treatment of the adsorbent adsorbing the dioxin to treat both the dioxin and the used adsorbent. About.
【０００２】[0002]
【従来の技術】ダイオキシン（ポリ塩化ジベンゾ−ｐ−
ジオキシン，ＰＣＤＤなど）の発生源は、ゴミ・廃棄物
焼却炉、産業廃棄物焼却炉が主体となっている。2. Description of the Related Art Dioxin (polychlorinated dibenzo-p-
Sources of dioxins, PCDDs, etc.) are mainly garbage / waste incinerators and industrial waste incinerators.
【０００３】従来における、ダイオキシンの発生抑制技
術およびその分解技術として一般的なものは以下の通り
である。[0003] Conventional techniques for controlling the generation of dioxins and their decomposition techniques are as follows.
【０００４】高温完全焼却法：焼却炉の燃焼ガス雰囲気
温度を高温範囲に保持してダイオキシンの発生を抑制す
る。但し、温度分布を均一かつ高温域に長期間維持する
こと及びガス滞溜時間を長くすることが比較的困難で、
結果的にダイオキシンの生成が避けられず、また、高温
プロセスゆえにエネルギー多消費型で装置寿命が短い。[0004] High-temperature complete incineration method: The generation of dioxin is suppressed by maintaining the combustion gas atmosphere temperature of an incinerator in a high temperature range. However, it is relatively difficult to maintain a uniform temperature distribution in a high temperature range for a long period of time and to increase the gas retention time.
As a result, the generation of dioxin is unavoidable, and because of the high-temperature process, energy consumption is high and the device life is short.
【０００５】低酸素熱分解法：低酸素雰囲気でダイオキ
シンを熱分解する。但し、反応速度が小さく、また、酸
素が混入するとダイオキシンが急増する。Low oxygen pyrolysis: Dioxin is pyrolyzed in a low oxygen atmosphere. However, the reaction rate is low, and when oxygen is mixed in, dioxin increases rapidly.
【０００６】ダイオキシン含有飛灰溶融法：飛灰を高温
溶融し、含まれているダイオキシンを分解する。但し、
ガス中のダイオキシンの処理は不可能で、高温溶融時に
発生する排ガス、揮発金属などの処理工程の不可が必要
である。Dioxin-containing fly ash melting method: Fly ash is melted at a high temperature to decompose the contained dioxin. However,
It is impossible to treat dioxin in gas, and it is necessary to eliminate the need for treatment steps for exhaust gas, volatile metal, etc. generated during high-temperature melting.
【０００７】光分解法：太陽光あるいは紫外線を照射し
てダイオキシンを分解する。但し、分解所要時間が長
く、エネルギー効率が低い。Photolysis method: Dioxin is decomposed by irradiating sunlight or ultraviolet rays. However, the decomposition time is long and the energy efficiency is low.
【０００８】微生物分解法：ダイオキシンを微生物分解
する。但し、分解所要時間が非常に長く、またダイオキ
シン類の構造によっては適用できない。[0008] Microbial decomposition method: Microbial decomposition of dioxin. However, the decomposition time is very long and cannot be applied depending on the structure of dioxins.
【０００９】さらに、従来におけるダイオキシンの分解
技術として、水熱処理を行うものは以下の通りである。Further, as a conventional dioxin decomposition technique, the one which performs hydrothermal treatment is as follows.
【００１０】飛灰の水熱処理法：ダイオキシン（ＰＣＤ
Ｄ、ＰＯＣＤＦなど）を含む飛灰のアルカリ性スラリー
を３００℃の水熱分解条件で処理する。但し、ガス中の
ダイオキシンの分解法ではない。Fly ash hydrothermal treatment method: dioxin (PCD
D, POCDF, etc.) are treated under hydrothermal decomposition conditions at 300 ° C. However, this is not a method for decomposing dioxin in gas.
【００１１】飛灰の超臨界水酸化処理法：ダイオキシン
を含む飛灰を酸化剤（空気、酸素あるいは過酸化水素）
の存在下で４００℃以上の超臨界水分解条件で処理して
超臨界水酸化する。但し、ガス中のダイオキシンの分解
法ではない。[0011] Fly ash supercritical water oxidation treatment: Fly ash containing dioxin is converted to an oxidizing agent (air, oxygen or hydrogen peroxide).
And supercritical water oxidation in the presence of supercritical water at 400 ° C. or higher. However, this is not a method for decomposing dioxin in gas.
【００１２】また、従来におけるダイオキシンの吸着技
術として一般的なものは以下の通りである。The general dioxin adsorption technology in the related art is as follows.
【００１３】固定床式吸着法：ペレット状あるいは塊状
の吸着剤を用いる固定床式吸着塔によって吸着処理す
る。しかし、比表面積が小さくなるので、充分な吸着能
力を得ようとすると安定した処理を行うことができな
い。[0013] Fixed bed adsorption method: Adsorption treatment is carried out by a fixed bed adsorption tower using a pellet-like or bulk adsorbent. However, since the specific surface area is small, stable treatment cannot be performed in order to obtain sufficient adsorption capacity.
【００１４】[0014]
【発明が解決しようとする課題】本発明の目的は、ダイ
オキシン含有ガスを連続的に吸着処理してダイオキシン
除去ガスを得、ダイオキシンを吸着した吸着剤を、吸着
したダイオキシンと共に連続的に酸化分解するダイオキ
シン含有ガスの処理方法及び装置を提供することにあ
る。SUMMARY OF THE INVENTION It is an object of the present invention to obtain a dioxin-removed gas by continuously adsorbing a dioxin-containing gas and continuously oxidatively decompose the adsorbent adsorbing dioxin together with the adsorbed dioxin. An object of the present invention is to provide a method and an apparatus for treating a dioxin-containing gas.
【００１５】[0015]
【課題を解決するための手段】本発明においては、流動
床式吸着技術・流動床式吸着装置が用いられる。In the present invention, a fluidized bed adsorption technique and a fluidized bed adsorption apparatus are used.
【００１６】即ち、本発明のダイオキシン含有ガスの連
続的処理方法においては、ダイオキシン含有ガスを微粉
乃至粉体状の活性炭またはコークスから成る吸着剤を投
入された流動床式吸着塔の下部に導入し、上記吸着剤を
流動化させると共にこれが含有するダイオキシンを吸着
剤に吸着させつつ上昇させ、次いで上記流動床式吸着塔
の上部よりダイオキシンを吸着・除去されたガスを分離
・導出し、さらに気−固分離手段によって同伴する固型
分を除去・分離してダイオキシン除去ガスとし、上記の
ようにして形成されたダイオキシンを吸着した吸着剤の
１部を補給・供給される吸着剤とバランスさせつつ取出
し、取出されたダイオキシンを吸着した吸着剤を燃焼炉
または水熱酸化分解反応装置に導入して、吸着されたダ
イオキシンと吸着剤の両者を酸化分解することによって
ダイオキシン含有ガスを連続的に処理する。That is, in the method for continuously treating a dioxin-containing gas according to the present invention, the dioxin-containing gas is introduced into a lower part of a fluidized bed type adsorption tower charged with an adsorbent composed of fine or powdery activated carbon or coke. The adsorbent is fluidized and the dioxin contained therein is raised while adsorbing the adsorbent, and then the gas from which dioxin has been adsorbed / removed from the upper part of the fluidized bed adsorption tower is separated and led out, and further vaporized. A solid component is removed and separated by solid separation means to obtain a dioxin-removed gas, and a part of the adsorbent adsorbing dioxin formed as described above is taken out while being balanced with the supplied and supplied adsorbent. The adsorbent that adsorbs the dioxin removed is introduced into a combustion furnace or a hydrothermal oxidative decomposition reactor to adsorb the adsorbed dioxin. Continuously processing the dioxin-containing gas by oxidative decomposition of both.
【００１７】また、本発明のダイオキシン含有ガスの連
続処理装置は、ダイオキシン含有ガスよりダイオキシン
を吸着・除去してダイオキシン除去ガスとする流動床式
吸着装置と生成するダイオキシンを吸着した吸着剤を処
理して吸着されたダイオキシンと吸着剤の両者を酸化分
解する酸化処理装置とを有し、上記流動床式吸着装置が
流動床式吸着塔と補給用の吸着剤を供給する補給用吸着
剤供給手段とダイオキシンを吸着した吸着剤を取出す吸
着剤取出手段とを具備し、上記流動床式吸着塔が微粉乃
至粉体状の吸着剤として活性炭またはコークスを投入さ
れており、ダイオキシン含有ガスが上記流動床式吸着塔
下部に導入されて、上部に向って流れる間に上記吸着剤
はダイオキシン含有ガスの上昇流によって流動化される
と共にダイオキシン含有ガス中のダイオキシンを吸着
し、ダイオキシンを吸着・除去されたガスは上記流動床
式吸着塔上部を経て流動床式吸着装置外へダイオキシン
除去ガスとして分離・導出され、またダイオキシンを吸
着した吸着剤の１部が上記吸着剤取出手段によって上記
補給用吸着剤供給手段の供給量とバランスさせつつ取出
されるように構成され、また上記酸化処理装置が燃焼炉
また水熱酸化分解反応装置を含み、上記吸着剤取出手段
によって取出されたダイオキシンを吸着した吸着剤を上
記酸化処理装置に導入することによって、ダイオキシン
と吸着剤との両者を酸化分解するように構成されたダイ
オキシン含有ガスの連続処理装置である。Further, the continuous treatment device for dioxin-containing gas of the present invention is a fluidized bed adsorber for adsorbing and removing dioxin from a dioxin-containing gas to produce a dioxin-removing gas and an adsorbent for adsorbing dioxin produced. An oxidation treatment device for oxidizing and decomposing both the adsorbed dioxin and the adsorbent, wherein the fluidized bed adsorption device is a fluidized bed adsorption tower and a replenishing adsorbent supply means for supplying a replenishing adsorbent; Adsorbent take-out means for taking out the adsorbent adsorbing dioxin, wherein the fluidized bed type adsorption tower is charged with activated carbon or coke as a fine powder or powdery adsorbent, and the dioxin-containing gas is mixed with the fluidized bed type adsorbent. The adsorbent is introduced into the lower part of the adsorption tower and is fluidized by the upward flow of the dioxin-containing gas while flowing toward the upper part. The gas adsorbing dioxin in the contained gas and adsorbing and removing dioxin is separated and led out as dioxin-removed gas outside the fluidized bed adsorber through the upper part of the fluidized bed adsorption tower, and the adsorbent adsorbs dioxin Is configured to be taken out by the adsorbent take-out means while balancing the supply amount of the replenishing adsorbent supply means, and the oxidation treatment apparatus includes a combustion furnace or a hydrothermal oxidative decomposition reaction apparatus, By introducing the adsorbent adsorbing the dioxin taken out by the adsorbent take-out means to the oxidation treatment device, the dioxin-containing gas continuous treatment device is configured to oxidatively decompose both the dioxin and the adsorbent. is there.
【００１８】ここで、ダイオキシンとは、ポリ塩化ジベ
ンゾ−ｐ−ジオキシン（ＰＣＤＤ、ダイオキシン）とそ
の類縁化合物である。上記類縁化合物としては、ポリ臭
化ジベンゾ−ｐ−ジオキシン、ポリ塩化ベゾフラン（Ｐ
ＣＤＦ）、ポリ塩化ビフェニル（ＰＣＢＣ）およびこれ
らの類似化合物がある。Here, dioxin is polychlorinated dibenzo-p-dioxin (PCDD, dioxin) and its analogous compounds. The analogous compounds include polybrominated dibenzo-p-dioxin, polychlorinated bezofuran (P
CDF), polychlorinated biphenyls (PCBC) and their analogous compounds.
【００１９】特に、ポリ塩化ジベンゾ−ｐ−ジオキシン
（ＰＣＤＤ、ダイオキシン）のうち、四塩化ジベンゾ−
ｐ−ジオキシン（ＴＣＤＤ）には、最高毒性を示す２，
３，７，８−四塩化ジベンゾ−ｐ−ジオキシンが含まれ
る。Particularly, among polychlorinated dibenzo-p-dioxins (PCDD, dioxin), dibenzotetrachloride
p-Dioxin (TCDD) has the highest toxicity2,
3,7,8-tetrachlorodibenzo-p-dioxin is included.
【００２０】なお、本実施の形態においては、ポリ塩化
ジベンゾ−ｐ−ジオキシン（ＰＣＤＤ、ダイオキシン）
を中心に説明するが、これによって本発明の技術範囲が
限定されるものではない。In this embodiment, polychlorinated dibenzo-p-dioxin (PCDD, dioxin) is used.
However, this does not limit the technical scope of the present invention.
【００２１】一般ゴミ・廃棄物焼却炉、産業廃棄物焼却
炉、塩素系漂白工場、塩素系溶剤使用工場などを発生源
として、上記ダイオキシンを含有するガス（ダイオキシ
ン含有ガス）が排出される。こうしたダイオキシン含有
ガスは、ダイオキシンを遊離の形で含む外、ガス中の微
細固形物に付着乃至吸着された形などで含んでいる。こ
れらは、何れも本発明のダイオキシンの範囲に含まれ
る。The above dioxin-containing gas (dioxin-containing gas) is discharged from a general waste / waste incinerator, an industrial waste incinerator, a chlorine-based bleaching plant, a plant using a chlorine-based solvent, or the like. Such a dioxin-containing gas contains not only dioxin in a free form but also a form adhering to or adsorbed to fine solids in the gas. These are all included in the range of the dioxin of the present invention.
【００２２】[0022]
【発明の実施の形態】本発明による１群の方法は、ダイ
オキシン含有ガスを微粉乃至粉体状の活性炭またはコー
クスから成る吸着剤が投入された循環・分離用上置槽付
の流動床式吸着塔の下部に導入し、上記吸着剤を流動化
させ、さらに流動化された上記吸着剤を上昇管を通って
上記循環・分離用上置槽に押上げると共に含有するダイ
オキシンを吸着させ、次いで上記循環・分離用上置槽上
部の流動界面より上側からダイオキシンを吸着・除去さ
れたガスを分離・導出し、さらに気−固分離手段によっ
て同伴する固型分を除去・分離してダイオキシン除去ガ
スとし、上置循環・分離用上置槽内の吸着剤を上記流動
床式吸着塔へ下降させる循環手段によって下降させて上
記流動式吸着塔と上記循環・分離用上置槽間で吸着剤の
上昇・下降連続循環を形成し、またダイオキシンを吸着
した吸着剤の１部を上記流動床式吸着塔への補給用吸着
剤供給量とバランスさせつつ、上記循環・分離用上置槽
の流動界面より下側から取出し、取出されたダイオキシ
ンを吸着した吸着剤を燃焼炉または水熱酸化分離反応装
置に導入して、吸着されたダイオキシンと吸着剤の両者
を酸化分解するダイオキシン含有ガスの連続的処理方法
である。DETAILED DESCRIPTION OF THE INVENTION One group of processes according to the present invention is a fluidized bed adsorption of a dioxin-containing gas with a circulating / separating upper tank into which an adsorbent comprising fine or powdered activated carbon or coke is charged. Introduced to the lower part of the tower, fluidized the adsorbent, further pushed up the fluidized adsorbent to the circulation / separation upper tank through a riser to adsorb the contained dioxin, and then The gas from which dioxin has been adsorbed and removed from above the flow interface at the top of the upper circulation / separation tank is separated and led out, and the solid components entrained are removed and separated by gas-solid separation means to obtain dioxin-removed gas. The adsorbent in the upper circulation / separation upper tank is lowered by the circulating means for lowering the adsorbent to the fluidized bed adsorption tower, and the adsorbent rises between the fluidized adsorption tower and the circulation / separation upper tank.・ Descent continuous circulation And removing a part of the adsorbent adsorbing dioxin from below the flow interface of the circulation / separation upper tank while balancing the supply amount of the adsorbent for replenishment to the fluidized bed adsorption tower. A method for continuously treating a dioxin-containing gas in which an adsorbent having adsorbed dioxin taken out is introduced into a combustion furnace or a hydrothermal oxidation separation reactor to oxidatively decompose both the adsorbed dioxin and the adsorbent.
【００２３】本発明による１群の装置は、ダイオキシン
含有ガスの連続的処理装置において、ダイオキシン含有
ガスよりダイオキシンを吸着・除去してダイオキシン除
去ガスとする流動床式吸着装置と生成するダイオキシン
を吸着した吸着剤を処理して吸着されたダイオキシンと
吸着剤の両者を酸化分解する酸化処理装置とを有し、上
記流動床式吸着装置が循環・分離用上置槽を有する流動
床式吸着塔と補給用吸着剤供給手段とダイオキシンを吸
着した吸着剤を取出す吸着剤取出手段と吸着剤を上記循
環・分離用上置槽から上記流動床式吸着塔へ下降させる
循環手段とを含み、上記流動床式吸着塔が微粉乃至粉体
状の吸着剤として活性炭またはコークスを投入されてお
り、ダイオキシン含有ガスが上記流動床式吸着塔下部に
導入されることによって上記吸着剤が流動化され、さら
に流動化された上記吸着剤が上昇管を通って上記循環・
分離用上置槽に押上げられ、この間に含有ダイオキシン
が吸着剤によって吸着・除去され、ダイオキシンを吸着
・除去されたガスが上記循環・分離用上置槽上部の流動
界面より上側より分離・導出され、さらに分離・導出ガ
スがダイオキシン除去ガスとして上記流動床式吸着装置
外へ導出されるように構成され、また上記循環・分離用
上置槽内の吸着剤が上記循環手段によって上記流動床式
吸着塔内に下降・導入され、上記流動床式吸着塔と上記
循環・分離用上置槽間で吸着剤が上昇・下降の循環を行
うように構成され、さらに上記循環・分離用上置槽内の
ダイオキシンを吸着した吸着剤が、上記補給用吸着剤供
給手段によって上記流動床式吸着塔に補給される吸着剤
量とバランスされつつ取出されるように構成され、上記
酸化処理装置は燃焼炉または水熱酸化分解反応装置を含
み、上記吸着剤取出手段によって導出されたダイオキシ
ンを吸着した吸着剤が上記酸化処理装置に導入されて、
吸着されたダイオキシンと吸着剤の両者が酸化分解され
るように構成されているダイオキシン含有ガスの連続処
理装置である。A group of apparatuses according to the present invention are a continuous processing apparatus for a dioxin-containing gas, in which a dioxin is adsorbed and removed from the dioxin-containing gas to obtain a dioxin-removed gas, and a dioxin produced is adsorbed. It has an oxidation treatment device that oxidizes and decomposes both adsorbent and dioxin adsorbed by treating the adsorbent, and the fluidized bed adsorber is replenished with a fluidized bed adsorption tower having an upper tank for circulation and separation. An adsorbent supply means, an adsorbent removal means for taking out the adsorbent adsorbing dioxin, and a circulation means for lowering the adsorbent from the circulation / separation upper tank to the fluidized bed adsorption tower, The adsorption tower is charged with activated carbon or coke as a fine or powdery adsorbent, and the dioxin-containing gas is introduced into the lower part of the fluidized bed adsorption tower. The sorbent is fluidized I, the circulating-further fluidized the adsorbent through the riser
It is pushed up to the upper separation tank, during which dioxin is adsorbed and removed by the adsorbent, and the gas from which dioxin has been adsorbed and removed is separated and led out from above the flow interface above the upper circulation and separation tank. Further, the separation / outflow gas is configured to be led out of the fluidized bed adsorber as a dioxin removal gas, and the adsorbent in the circulation / separation upper tank is discharged by the circulation means in the fluidized bed type. The adsorbent is lowered and introduced into the adsorption tower, and the adsorbent is configured to circulate up and down between the fluidized bed adsorption tower and the circulation / separation upper tank, and furthermore, the circulation / separation upper tank. The adsorbent having adsorbed dioxin therein is taken out while being balanced with the amount of adsorbent supplied to the fluidized bed adsorption tower by the supply adsorbent supply means, and the oxidation treatment apparatus is provided with Include furnace or hydrothermal oxidation decomposition reactor, the adsorbent having adsorbed dioxin derived by the adsorbent retriever is introduced into the oxidizing apparatus,
This is a continuous processing device for a dioxin-containing gas configured so that both the adsorbed dioxin and the adsorbent are oxidatively decomposed.
【００２４】上記の水熱酸化分解反応装置は水熱酸化分
解反応を用いるものであって、この水熱酸化分解反応
は、工業的技術として既に一部で用いられている。これ
らは、実用反応混合物系に応じた３００℃程度の温度で
水の化学反応性が急増乃至最大化しまた有機物に対する
溶解能が急増し、さらに高温では気一液界消失領域の超
臨界水条件、その間の亜臨界水条件が発生すること、及
びこの様な水熱条件で有機物や炭素質を酸化分解できる
ことを利用している。The above-mentioned hydrothermal oxidative decomposition reaction apparatus uses a hydrothermal oxidative decomposition reaction, and this hydrothermal oxidative decomposition reaction is already partially used as an industrial technique. In these, the chemical reactivity of water sharply increases or maximizes at a temperature of about 300 ° C. according to the practical reaction mixture system, and the dissolving ability for organic substances rapidly increases.At higher temperatures, supercritical water conditions in a gas-liquid boundary disappearance region, Utilizing the fact that a subcritical water condition is generated during that time, and that organic substances and carbonaceous materials can be oxidatively decomposed under such hydrothermal conditions.
【００２５】例えば、石炭は超臨界水分解によって分解
・液化され、アルカリ剤の存在はこの種の分解・液化を
触媒的に促進する。重質油は超臨界水分解によって軽質
油に分解され、アルカリ剤の存在はこの種の分解・改質
を触媒的に促進する。For example, coal is decomposed and liquefied by supercritical water decomposition, and the presence of an alkaline agent catalytically promotes this kind of decomposition and liquefaction. Heavy oil is decomposed into light oil by supercritical water cracking, and the presence of an alkaline agent catalytically promotes this kind of decomposition and reforming.
【００２６】一般に有機物は、酸化剤の存在下に水熱分
解すると水熱酸化分解され、例えば汚泥は２００℃で酸
化分解され、４００℃では自熱的に酸化分解され、二酸
化炭素と水になる。In general, organic matter is hydrothermally decomposed when hydrothermally decomposed in the presence of an oxidizing agent. For example, sludge is oxidatively decomposed at 200 ° C. and autothermally oxidatively decomposed at 400 ° C. to become carbon dioxide and water. .
【００２７】超臨界水酸化分解を含め、水熱酸化分解反
応の利点は、反応管理・バッチ反応化及び連続管型反応
化が容易であること、熱損失が小さく、熱管理が容易で
あること、熱回収が容易であること、追加燃料を要せず
反応進行が可能であること、高品質水の回収が可能であ
ること等の諸点であり、本発明はこれらの諸点を活用す
るものである。The advantages of hydrothermal oxidative decomposition, including supercritical hydroxylation, are that reaction management, batch reaction and continuous tube reaction are easy, heat loss is small, and heat management is easy. , Heat recovery is easy, the reaction can proceed without the need for additional fuel, and high-quality water can be recovered.The present invention makes use of these points. is there.
【００２８】即ち、水熱分解反応とは、高温高圧水条件
下の分解反応であって、超臨界水酸化分解、亜臨界水酸
化分解、その他の水熱酸化分解などの水熱科学的酸化分
解反応が含まれ、酸化剤、アルカリ剤などの分解剤を添
加使用することによって、その分解剤の科学的性質に応
じた反応が促進される。このような分解剤としては、酸
素、空気、過酸化水素、オゾン、オゾン水、などの酸化
剤などが含まれる。That is, the hydrothermal decomposition reaction is a decomposition reaction under high-temperature and high-pressure water conditions, and includes hydrothermal scientific oxidative decomposition such as supercritical oxidative decomposition, subcritical oxidative decomposition, and other hydrothermal oxidative decomposition. A reaction is included, and by adding and using a decomposing agent such as an oxidizing agent and an alkali agent, a reaction according to the scientific properties of the decomposing agent is promoted. Such decomposing agents include oxidizing agents such as oxygen, air, hydrogen peroxide, ozone, ozone water, and the like.
【００２９】そして、分解剤として例えば酸化剤を用い
てダイオキシンを超臨界水酸化分解すると、まず４００
℃程度でベンセン、フェノール、クロロベナセン、クロ
ロフェノール、塩化水素などに分解し、さらに高温にす
ると低級炭化水素（Ｃ1 〜Ｃ2 程度）、二酸化炭素、
水、塩化分解と加水分解と特異な合成的反応とが並行的
に複合したものである。Then, when dioxin is supercritically hydrolyzed and decomposed using, for example, an oxidizing agent as a decomposing agent, first, 400
Decomposes into benzene, phenol, chlorobenacene, chlorophenol, hydrogen chloride, etc. at about ℃, and lower temperature to lower hydrocarbons (about C 1 -C 2 ), carbon dioxide,
It is a complex of water, chlorination, hydrolysis and a unique synthetic reaction in parallel.
【００３０】実施例：以下に本発明の好適実施形態を図
１および図２により説明する。Embodiment: A preferred embodiment of the present invention will be described below with reference to FIGS.
【００３１】（１）ダイオキシン吸着装置 本発明のダイオキシン吸着装置の具体例は、微粉活性炭
または微粉コークスを吸着剤とし、上記吸着剤を被処理
ガスであるダイオキシン含有ガスによって流動せしめる
ようにした流動床式吸着塔１を含み、上記流動床式吸着
塔１は循環・分離用上置槽２が設けられている。(1) Dioxin Adsorbing Apparatus A specific example of the dioxin adsorbing apparatus of the present invention is a fluidized bed in which fine activated carbon or fine coke is used as an adsorbent and the adsorbent is caused to flow by a dioxin-containing gas which is a gas to be treated. The fluidized bed type adsorption tower 1 includes an upper tank 2 for circulation / separation.
【００３２】上記流動床式吸着塔１は流動化された吸着
剤を上記循環・分離用上置槽２に押上げる上昇管と、上
記循環・分離用上置槽２の流動界面の下側から上記流動
床式吸着塔１の流動界面の下側へ吸着剤の１部を取入用
の循環手段２１の下降管とによって連続され、このよう
な構成によって吸着剤は両者（１，２）間を循環せしめ
られる。The fluidized bed type adsorption tower 1 is provided with a rising pipe for pushing up the fluidized adsorbent to the circulation / separation upper tank 2, and from the lower side of the flow interface of the circulation / separation upper tank 2. A part of the adsorbent is connected to the lower side of the fluid interface of the fluidized bed adsorption tower 1 by a downcomer of a circulating means 21 for taking in the adsorbent. Is circulated.
【００３３】即ち、上記流動床式吸着塔１は上記のよう
にライダ２より吸着剤の１部を取入れる。That is, the fluidized bed adsorption tower 1 takes in a part of the adsorbent from the lid 2 as described above.
【００３４】循環手段２１と、ダイオキシンを吸着除去
されたガスを連続的に分解・排出するガスの排出手段２
２と、ダイオキシンを吸着した吸着剤の１部を連続的に
取出す吸着剤取出手段２３とを具備する循環・分離用上
置槽２と上記の吸着剤の取出手段２３とバランスをとり
つつ吸着剤を連続的に補給する補給用吸着剤供給手段３
とを具備している。（補給用の吸着剤槽３１を含む）な
お、上記ガスの排出手段２２は、フィルタ２４と連続す
るようにされ、ガスの排出手段２２を出たガスがフィル
タ２４で濾過されてダイオキシン除去ガスとして系外へ
導出され、一方で上記フィルタ２４で分離された吸着剤
は、上記吸着剤の取出手段２３によって取出された吸着
剤と合わせて酸化処理装置４で酸化処理されるように構
成される。Circulating means 21 and gas discharging means 2 for continuously decomposing and discharging the gas from which dioxin has been adsorbed and removed
2 and a circulating / separating upper tank 2 having adsorbent removing means 23 for continuously taking out a part of the adsorbent adsorbing dioxin and the adsorbent while balancing the adsorbent removing means 23 described above. Adsorbent supply means 3 for continuously replenishing water
Is provided. (Including the replenishing adsorbent tank 31) The gas discharging means 22 is connected to the filter 24, and the gas exiting the gas discharging means 22 is filtered by the filter 24 to be used as a dioxin removing gas. The adsorbent led out of the system and separated by the filter 24 on the other hand is configured to be oxidized by the oxidation treatment device 4 together with the adsorbent taken out by the adsorbent take-out means 23.
【００３５】（２）吸着剤の酸化処理装置 本発明の酸化処理装置の１群の具体例は、上記吸着剤の
取出手段２３およびフィルタ２４から供給されるダイオ
キシンを吸着した吸着剤（微粉活性炭または微粉コーク
ス）を燃焼する燃焼炉あるいは水熱酸化する水熱酸化反
応装置４Ａであって吸着剤を構成する炭素を酸化して炭
酸ガス類とすると共にダイオキシンを無害化する。(2) Apparatus for oxidizing adsorbent A specific example of a group of the oxidizing apparatus of the present invention is an adsorbent (fine-powder activated carbon or fine activated carbon) adsorbing dioxin supplied from the adsorbent extracting means 23 and the filter 24. A combustion furnace for burning fine coke) or a hydrothermal oxidation reactor 4A for hydrothermal oxidation, which oxidizes carbon constituting the adsorbent to carbon dioxide and detoxifies dioxin.
【００３６】以下に上記水熱酸化分解反応装置の１例を
説明する（図２参照）。Hereinafter, an example of the hydrothermal oxidative decomposition reaction apparatus will be described (see FIG. 2).
【００３７】本発明の水熱酸化分解反応装置４Ａの具体
例は、上記吸着剤の取出手段２３および上記フィルタ２
４から供給されるダイオキシン吸着活性炭あるいはダイ
オキシン吸着コークスの微粉体を、酸化剤などの分解剤
の存在下に水熱酸化分解する管型水熱酸化分解反応器４
１を含み、上記管型水熱酸化分解反応器４１は、これに
上記の微粉体と水とにより吸着剤−水スラリを製造する
スラリ化手段４２と、得られた吸着剤−水スラリに分解
剤（酸化剤など）を混合して上記水熱酸化分解反応器４
１に供給する反応混合物の供給手段４３と、水熱酸化分
解反応を受けた反応終了混合物を気−液分離する分離手
段４４（上記分離手段４４は、高圧分離器と低圧分離器
に分けて多段化してもよい）とを具備するようにされ
る。The specific example of the hydrothermal oxidative decomposition reaction apparatus 4A of the present invention includes the adsorbent extracting means 23 and the filter 2
4. A tubular hydrothermal oxidative decomposition reactor 4 for hydrothermal oxidative decomposition of fine powder of dioxin-adsorbed activated carbon or dioxin-adsorbed coke supplied from 4 in the presence of a decomposing agent such as an oxidant.
The above-mentioned tubular hydrothermal oxidative decomposition reactor 41 comprises a slurrying means 42 for producing an adsorbent-water slurry from the fine powder and water, and a decomposition into the obtained adsorbent-water slurry. A hydrothermal oxidative decomposition reactor 4
1 and a separating means 44 for gas-liquid separation of the reaction-completed mixture subjected to the hydrothermal oxidative decomposition reaction (the separating means 44 is divided into a high-pressure separator and a low-pressure separator, May be included).
【００３８】なお、上記スラリ化手段４２で用いられる
水の少なくとも１部は、上記分離手段４４で分離回収さ
れる回収水が循環使用されるように配管・連続され、ま
た上記スラリ化手段４２を出た吸着剤−水スラリが上記
管型水熱酸化分解反応器４１を出た反応終了混合物と熱
交換するように熱交換器４５を組込んで配管・連続さ
れ、さらにまた上記管型水熱酸化分解反応器４１の反応
熱が蒸気として回収される熱回収手段４６が設けられて
いる。At least a part of the water used in the slurrying means 42 is connected to a pipe so that the recovered water separated and recovered by the separating means 44 is circulated and used. The adsorbent-water slurry is piped and connected by incorporating a heat exchanger 45 so as to exchange heat with the reaction-terminated mixture exiting the tubular hydrothermal oxidative decomposition reactor 41. Heat recovery means 46 is provided for recovering the reaction heat of the oxidative decomposition reactor 41 as steam.
【００３９】（３）吸着剤、吸着条件、酸化処理条件 本発明のダイオキシン処理システムの具体的構成例は上
記の流動床式吸着塔１と循環・分離用上置槽２と吸着剤
補給手段３と酸化処理装置４とを上記のように構成した
ものである。(3) Adsorbent, adsorption conditions, and oxidation treatment conditions Specific examples of the dioxin treatment system of the present invention include the above-described fluidized bed adsorption tower 1, upper circulation / separation tank 2, and adsorbent replenisher 3. And the oxidation treatment device 4 are configured as described above.
【００４０】以下、全体システムなどについてさらに詳
述する。Hereinafter, the overall system will be described in more detail.
【００４１】吸着剤：本発明の流動床式吸着塔１におい
て、投入された吸着剤は導入された焼却炉（等）由来の
ダイオキシン含有ガスによって流動化されて流動床を形
成する。従って、吸着剤は吸着剤としての機能に流動床
の媒体としての機能を兼備する。微粉の活性炭またはコ
ークスが用いられる。殊にコークスの場合には多孔質の
ものが選択される。何れにせよ粒径が３００〜４００ミ
クロン程度以下の比表面積の大きいものが好適である。Adsorbent: In the fluidized bed type adsorption tower 1 of the present invention, the introduced adsorbent is fluidized by the introduced dioxin-containing gas from the incinerator (or the like) to form a fluidized bed. Therefore, the adsorbent has the function as the medium of the fluidized bed in addition to the function as the adsorbent. Fine powdered activated carbon or coke is used. Particularly in the case of coke, a porous one is selected. In any case, those having a large specific surface area with a particle size of about 300 to 400 microns or less are suitable.
【００４２】吸着条件：本発明の流動床吸着塔１におい
てダイオキシン含有ガスの吸着は連続式で行われ、上記
吸着剤補給手段３より吸着剤は必要なバランスを採って
連続的に補給され、一方で上記吸着剤の取出手段２３お
よびフィルタ２４よりダイオキシンを吸着した吸着剤の
１部が連続的に導出される。さらに、上記のような連続
的吸着を円滑に実現する為に、上記流動床式吸着塔１に
循環・分離用上置槽２が組合されて設置され、流動状態
の吸着剤は上記流動床式吸着塔１から押上げられて上記
循環・分離用上置槽２に至り、次いで上記循環・分離用
上置槽２より上記循環手段２１によって上記流動床式吸
着塔１へ至る循環を行うように構成されている。吸着温
度としては、吸着剤として活性炭を用いる場合には２０
０℃以下とするのが良く、吸着剤としてコークスを用い
る場合には２００℃〜４５０℃とするのが良い。Adsorption conditions: Dioxin-containing gas is adsorbed continuously in the fluidized bed adsorption tower 1 of the present invention, and the adsorbent is continuously replenished by the adsorbent replenishing means 3 with a necessary balance. Thus, a part of the adsorbent that has adsorbed dioxin is continuously discharged from the adsorbent removing means 23 and the filter 24. Further, in order to smoothly realize the continuous adsorption as described above, an upper circulating / separating tank 2 is installed in combination with the fluidized bed type adsorption tower 1, and the adsorbent in a fluidized state is mixed with the fluidized bed type adsorber. The water is pushed up from the adsorption tower 1 to reach the circulation / separation upper tank 2, and then circulated from the circulation / separation upper tank 2 to the fluidized bed adsorption tower 1 by the circulation means 21. It is configured. The adsorption temperature is 20 when activated carbon is used as the adsorbent.
The temperature is preferably set to 0 ° C. or lower. When coke is used as the adsorbent, the temperature is preferably set to 200 ° C. to 450 ° C.
【００４３】酸化処理条件：本発明の酸化処理装置４に
おいて、上記吸着剤の取出手段２３より導出される設計
量のダイオキシンを吸着した吸着剤と上記フィルタ２４
で分離されたダイオキシンを吸着した吸着剤とは合せて
酸化処理される。この場合、吸着剤の主体である活性炭
またはコークスの酸化処理と、これに吸着されたダイオ
キシンの酸化処理とが平行して行なわれる。酸化処理装
置４としては高温燃焼炉または水熱酸化分解反応装置が
用いられるが、上記高温燃焼炉の温度条件としては８０
０℃程度以上とするのがよい。上記水熱酸化反応装置と
しては、超臨界水酸化分解反応装置、亜臨界水酸化分解
反応装置（以上の場合の反応温度は４００℃〜７００℃
とするのが良い）およびその他の水熱酸化反応装置（８
００℃以下とするのが良い）が含まれる。Oxidation treatment conditions: In the oxidation treatment apparatus 4 of the present invention, the adsorbent adsorbing the designed amount of dioxin derived from the adsorbent removal means 23 and the filter 24
Is oxidized together with the adsorbent that has adsorbed the dioxins separated in step (1). In this case, the oxidation treatment of activated carbon or coke, which is the main component of the adsorbent, and the oxidation treatment of dioxin adsorbed thereon are performed in parallel. A high-temperature combustion furnace or a hydrothermal oxidative decomposition reaction apparatus is used as the oxidation treatment apparatus 4.
The temperature is preferably about 0 ° C. or higher. Examples of the hydrothermal oxidation reactor include a supercritical hydroxylation decomposition reactor and a subcritical hydroxylation decomposition reactor (the reaction temperature in the above case is 400 ° C. to 700 ° C.).
And other hydrothermal oxidation reactors (8
The temperature is preferably set to 00 ° C. or less).
【００４４】（４）全体システム 燃焼炉などから導出されたダイオキシン含有ガスは直接
または間接に上記流動床式吸着塔１の下部より連続的に
導入され、投入されている吸着剤を流動化しつつ各種の
状態で含有するダイオキシンを吸着剤によって除去さ
れ、且つ流動状態の吸着剤を上記循環・分離用上置槽２
へ押上げ結果的に上記循環手段２１による下降流と組合
せた吸着剤の循環運動を生起させつつ上記排出手段２２
および上記フィルタ２４を通ってダイオキシン除去ガス
として系外へ導出される。上記ダイオキシン除去ガスは
ダイオキシン含量が分析限界以下であるガス乃至目的に
応じてダイオキシン含量を充分低下せしめられたガスを
意味する。(4) Overall System Dioxin-containing gas derived from a combustion furnace or the like is directly or indirectly continuously introduced from the lower portion of the fluidized bed type adsorption tower 1, and various types of fluid are introduced while fluidizing the introduced adsorbent. The adsorbent removes the dioxin contained in the above-mentioned state, and removes the adsorbent in a fluid state from the circulation / separation upper tank 2.
As a result, the circulating movement of the adsorbent combined with the downward flow by the circulating means 21 is generated while the discharging means 22
And it is led out of the system as a dioxin removal gas through the filter 24. The dioxin removing gas means a gas having a dioxin content below the analysis limit or a gas having a sufficiently reduced dioxin content according to the purpose.
【００４５】上記流動床式吸着塔１における吸着剤は、
導入されたダイオキシン含有ガスによって流動化され、
上記循環・分離用上置槽２へ押上げる上昇流と上記循環
手段２１によってもたらされる下降流とで形成される循
環運動と、上記吸着剤の取出手段２３と上記フィルタ２
４とによる排出とこれとバランスする上記補給用吸着剤
供給手段３（吸着剤槽３１を含む）による供給とによっ
て形成される供給−排出運動を並行して行いつつダイオ
キシンを吸着し、次いで上記酸化処理装置４に導入され
る。The adsorbent in the fluidized bed adsorption tower 1 is as follows:
Fluidized by the introduced dioxin-containing gas,
A circulating motion formed by an ascending flow pushed up to the circulating / separating upper tank 2 and a descending flow provided by the circulating means 21; the adsorbent extracting means 23 and the filter 2;
4, the dioxin is adsorbed while the supply-discharge movement formed by the discharge by the supply adsorbent 4 and the supply by the replenishment adsorbent supply means 3 (including the adsorbent tank 31) is performed in parallel, and then the oxidation is performed. It is introduced into the processing device 4.
【００４６】上記酸化処理装置４に導入された吸着剤は
それ自身と上記流動床式吸着塔１において吸着乃至付着
等したダイオキシンと共に酸化分解処理される。The adsorbent introduced into the oxidizing apparatus 4 is subjected to oxidative decomposition together with the adsorbent itself and dioxin adsorbed or adhered in the fluidized bed type adsorption tower 1.
【００４７】[0047]
【発明の効果】ダイオキシン含有ガスを吸着処理してダ
イオキシン除去ガスとすると共に、吸着されたダイオキ
シンと吸着剤とを酸化分解するダイオキシン含有ガスの
連続的処理方法及び連続処理装置を提供する。According to the present invention, there is provided a method and apparatus for continuously treating a dioxin-containing gas, wherein the dioxin-containing gas is subjected to an adsorption treatment to obtain a dioxin-removed gas, and the adsorbent is oxidatively decomposed.
【図１】本発明の方法及び装置の一例の概要を示す概略
説明図。FIG. 1 is a schematic explanatory view showing an outline of an example of a method and an apparatus of the present invention.
【図２】本発明に用いられる水熱酸化分解装置の一例の
概要を示す概略説明図。FIG. 2 is a schematic explanatory view showing an outline of an example of a hydrothermal oxidative decomposition device used in the present invention.
１ 流動床式吸着塔 ２ 循環・分離用上置槽 ３ 補給用吸着剤供給手段 ４ 酸化処理装置（４Ａ水熱酸化分解反応装置） ２１ 循環手段 ２２ 排出手段 ２３ 取出手段 ２４ フィルタ ３１ 吸着剤槽 ４１ 管型水熱酸化分解反応器 ４２ スラリ化手段 ４３ 供給手段 ４４ 分離手段 ４５ 熱交換器 ４６ 熱交換手段 REFERENCE SIGNS LIST 1 fluidized bed adsorption tower 2 circulating / separating upper tank 3 replenishing adsorbent supply means 4 oxidation treatment apparatus (4A hydrothermal oxidative decomposition reaction apparatus) 21 circulation means 22 discharge means 23 removal means 24 filter 31 adsorbent tank 41 Tubular hydrothermal oxidative decomposition reactor 42 Slurry means 43 Supply means 44 Separation means 45 Heat exchanger 46 Heat exchange means
Claims (4)
またはコークスから成る吸着剤を投入された流動床式吸
着塔の下部に導入し、吸着剤を流動化させると共にこれ
が含有するダイオキシンを吸着剤に吸着させつつ上昇さ
せ、次いで上記流動床式吸着塔の上部よりダイオキシン
を吸着・除去されたガスとして分離・導出し、さらに気
−固分離手段によって同伴する固型分を除去・分離して
ダイオキシン除去ガスとし、上記のようにして形成され
たダイオキシンを吸着した吸着剤の１部を補給・供給さ
れる吸着剤とバランスさせつつ取出し、取出されたダイ
オキシンを吸着した吸着剤を燃焼炉または水熱酸化分解
反応装置に導入して吸着されたダイオキシンと吸着剤の
両者を酸化分解するダイオキシン含有ガスの連続的処理
方法。1. A dioxin-containing gas is introduced into a lower portion of a fluidized bed adsorption tower into which an adsorbent made of powdered activated carbon or coke has been charged, and the adsorbent is fluidized and the dioxin contained therein is used as an adsorbent. It is lifted while being adsorbed, and then dioxin is separated and led out from the upper part of the fluidized bed type adsorption tower as a gas adsorbed and removed, and the solid components entrained by gas-solid separation means are removed and separated to remove dioxin. As a gas, a part of the adsorbent adsorbing dioxin formed as described above is taken out while balancing with the supplied / supplied adsorbent, and the adsorbent adsorbing the dioxin taken out is burned in a combustion furnace or hydrothermal oxidation. A continuous treatment method for a dioxin-containing gas that oxidizes and decomposes both the adsorbent and the adsorbed dioxin introduced into the decomposition reactor.
またはコークスから成る吸着剤が投入された循環・分離
用上置槽付の流動床式吸着塔の下部に導入し、上記吸着
剤を流動化させ、さらに流動化された上記吸着剤を上昇
管を通って上記循環・分離用上置槽に押上げると共に含
有するダイオキシンを吸着させ、次いで上記循環・分離
用上置槽上部の流動界面より上側からダイオキシンを吸
着・除去されたガスを分離・導出し、さらに気−固分離
手段によって同伴する固型分を除去・分離してダイオキ
シン除去ガスとし、上置循環・分離用上置槽内の吸着剤
を上記流動床式吸着塔へ下降させる循環手段によって下
降させて上記流動式吸着塔と上記循環・分離用上置槽間
で吸着剤の上昇・下降連続循環を形成し、またダイオキ
シンを吸着した吸着剤の１部を、上記流動床式吸着塔へ
の補給用吸着剤供給量とバランスさせつつ、上記循環・
分離用上置槽の流動界面より下側から取出し、取出され
たダイオキシンを吸着した吸着剤を燃焼炉または水熱酸
化分解反応装置に導入して吸着されたダイオキシンと吸
着剤の両者を酸化分解するダイオキシン含有ガスの連続
的処理方法。2. A dioxin-containing gas is introduced into the lower part of a fluidized bed adsorption tower having an upper circulating / separating tank into which an adsorbent composed of powdered activated carbon or coke is charged, and the adsorbent is fluidized. Further, the fluidized adsorbent is pushed up through the riser tube to the circulation / separation upper tank, and the contained dioxin is adsorbed. The gas from which dioxin has been adsorbed and removed is separated and led out, and the solid components entrained by gas-solid separation means are removed and separated into dioxin-removed gas, which is adsorbed in the upper tank for upper circulation / separation. The adsorbent is lowered by the circulating means for lowering the adsorbent to the fluidized bed adsorption tower to form an ascending and descending continuous circulation of the adsorbent between the fluidized adsorption tower and the circulation / separation upper tank, and adsorbs dioxin. adsorption While a part of the adsorbent is balanced with the supply amount of the replenishing adsorbent to the fluidized bed adsorption tower,
Take out from below the flow interface of the upper separation tank, and adsorb the adsorbed dioxin into the combustion furnace or hydrothermal oxidative decomposition reactor to oxidize and decompose both adsorbed dioxin and adsorbent A continuous treatment method for dioxin-containing gas.
において、ダイオキシン含有ガスよりダイオキシンを吸
着・除去してダイオキシン除去ガスとする流動床式吸着
装置と生成するダイオキシンを吸着した吸着剤を処理し
て吸着されたダイオキシンと吸着剤の両者を酸化分解す
る酸化処理装置とを有し、上記流動床式吸着装置が流動
床式吸着塔と補給用の吸着剤を供給する補給用吸着剤供
給手段とダイオキシンを吸着した吸着剤を取出す吸着剤
取出手段とを具備し、上記流動床式吸着塔が粉体状の吸
着剤として活性炭またはコークスを投入されており、ダ
イオキシン含有ガスが上記流動床式吸着塔下部に導入さ
れて、上部に向って流れる間に上記吸着剤はダイオキシ
ン含有ガスの上昇流によって流動化されると共にダイオ
キシン含有ガス中のダイオキシンを吸着し、ダイオキシ
ンを吸着・除去されたガスは上記流動床式吸着塔上部を
経て流動床式吸着装置外へダイオキシン除去ガスとして
分離・導出され、またダイオキシンを吸着した吸着剤の
１部が上記吸着剤取出手段によって上記補給用吸着剤供
給手段の供給量とバランスさせつつ取出されるように構
成され、また上記酸化処理装置が燃焼炉また水熱酸化分
解反応装置を具備し、上記吸着剤取出手段によって取出
されたダイオキシンを吸着した吸着剤を上記酸化処理装
置に導入することによってダイオキシンと吸着剤との両
者を酸化分解するように構成されているダイオキシン含
有ガスの連続処理装置。3. A continuous treatment apparatus for a dioxin-containing gas, wherein a dioxin is adsorbed and removed from the dioxin-containing gas to obtain a dioxin-removing gas, and a fluidized bed adsorber is used to treat the adsorbent that adsorbs the generated dioxin. An oxidation treatment device that oxidizes and decomposes both the dioxin and the adsorbent, wherein the fluidized bed adsorption device comprises a fluidized bed adsorption tower, a replenishing adsorbent supply means for supplying a replenishing adsorbent, and dioxin. Adsorbent removal means for taking out the adsorbed adsorbent, wherein the fluidized bed adsorption tower is charged with activated carbon or coke as a powdery adsorbent, and a dioxin-containing gas is provided at the lower part of the fluidized bed adsorption tower. While being introduced and flowing upward, the adsorbent is fluidized by the ascending flow of the dioxin-containing gas, and The dioxin-adsorbed gas from which dioxin has been adsorbed / removed is separated and led out as dioxin-removed gas outside the fluidized bed adsorber through the upper part of the fluidized bed adsorption tower, and a part of the adsorbent that has adsorbed dioxin is removed. The adsorbent removal means is configured to be taken out while balancing the supply amount of the replenishment adsorbent supply means, and the oxidation treatment device includes a combustion furnace or a hydrothermal oxidative decomposition reaction device, A continuous processing device for a dioxin-containing gas, wherein the dioxin and the adsorbent are oxidatively decomposed by introducing the adsorbent having adsorbed dioxin extracted by the extracting means into the oxidation treatment device.
おいて、ダイオキシン含有ガスよりダイオキシンを吸着
・除去してダイオキシン除去ガスとする流動床式吸着装
置と生成するダイオキシンを吸着した吸着剤を処理して
吸着されたダイオキシンと吸着剤の両者を酸化分解する
酸化処理装置とを有し、上記流動床式吸着装置が循環・
分離用上置槽を有する流動床式吸着塔と補給用吸着剤供
給手段とダイオキシンを吸着した吸着剤を取出す吸着剤
取出手段と吸着剤を上記循環・分離用上置槽から上記流
動床式吸着塔へ下降させる循環手段とを具備し、上記流
動床式吸着塔が粉体状の吸着剤として活性炭またはコー
クスを投入されて居り、ダイオキシン含有ガスが上記流
動床式吸着塔下部に導入されることによって上記吸着剤
が流動化されさらに流動化された上記吸着剤が上昇管を
通って上記循環・分離用上置槽に押上げられ、この間に
含有ダイオキシンが吸着剤によって吸着・除去され、ダ
イオキシンを吸着・除去されたガスが上記循環・分離用
上置槽上部の流動界面より上側より分離・導出され、さ
らに分離・導出されたガスがダイオキシン除去ガスとし
て上記流動床式吸着装置外へ導出されるように構成さ
れ、また上記循環・分離用上置槽内の吸着剤が上記循環
手段によって上記流動床式吸着塔内に下降・導入され、
上記流動床式吸着塔と上記循環・分離用上置槽間で吸着
剤が上昇・下降の循環を行うように構成され、さらに上
記循環・分離用上置槽内のダイオキシンを吸着した吸着
剤が、上記補給用吸着剤供給手段によって上記流動床式
吸着塔に補給される吸着剤量とバランスされつつ取出さ
れるように構成され、上記酸化処理装置が燃焼炉または
水熱酸化分解反応装置を有し、上記吸着剤取出手段によ
って導出されたダイオキシンを吸着した吸着剤が上記酸
化処理装置に導入されて、吸着されたダイオキシンと吸
着剤の両者が酸化分解されるように構成されているダイ
オキシン含有ガスの連続処理装置。4. A continuous treatment apparatus for a dioxin-containing gas, wherein a fluidized bed-type adsorption apparatus for adsorbing and removing dioxin from the dioxin-containing gas to produce a dioxin-removing gas and an adsorbent for adsorbing the generated dioxin are treated and adsorbed. An oxidation treatment device that oxidizes and decomposes both the dioxin and the adsorbent.
A fluidized bed adsorption tower having an upper separation tank, a supply adsorbent supply means, an adsorbent removal means for removing adsorbent adsorbing dioxin, and an adsorbent from the circulation / separation upper tank to the fluidized bed adsorption Circulating means for lowering to the tower, wherein the fluidized bed adsorption tower is charged with activated carbon or coke as a powdery adsorbent, and the dioxin-containing gas is introduced into the lower part of the fluidized bed adsorption tower The adsorbent is fluidized by the above, and the fluidized adsorbent is pushed up through the riser to the circulation / separation upper tank, during which the contained dioxin is adsorbed and removed by the adsorbent, and the dioxin is removed. The adsorbed and removed gas is separated and led out from above the flow interface above the circulation / separation upper tank, and the separated and led gas is used as the dioxin-removed gas in the fluidized bed absorption tank. Is configured to be derived to the outside of the apparatus, also sorbent in 置槽 on for the circulating-separated is lowered, introduced into the fluidized bed adsorption tower by the circulating means,
The adsorbent is configured to perform upward and downward circulation between the fluidized bed adsorption tower and the circulation / separation upper tank, and the adsorbent that has adsorbed dioxin in the circulation / separation upper tank is further provided. The replenishment adsorbent supply means is configured to be taken out while being balanced with the amount of adsorbent replenished to the fluidized bed adsorption tower, and the oxidation treatment device has a combustion furnace or a hydrothermal oxidative decomposition reaction device. A dioxin-containing gas configured so that the adsorbent that has adsorbed the dioxin derived by the adsorbent removal means is introduced into the oxidation treatment apparatus, and both the adsorbed dioxin and the adsorbent are oxidatively decomposed. Continuous processing equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP10081399A JPH11276856A (en) | 1998-03-27 | 1998-03-27 | Treatment of dioxin-containing gas and device therefor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP10081399A JPH11276856A (en) | 1998-03-27 | 1998-03-27 | Treatment of dioxin-containing gas and device therefor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH11276856A true JPH11276856A (en) | 1999-10-12 |
Family
ID=13745244
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP10081399A Pending JPH11276856A (en) | 1998-03-27 | 1998-03-27 | Treatment of dioxin-containing gas and device therefor |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH11276856A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113955787A (en) * | 2021-08-31 | 2022-01-21 | 江西盖亚环保科技有限公司 | Process for removing dioxin in fly ash |
-
1998
- 1998-03-27 JP JP10081399A patent/JPH11276856A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113955787A (en) * | 2021-08-31 | 2022-01-21 | 江西盖亚环保科技有限公司 | Process for removing dioxin in fly ash |
| CN113955787B (en) * | 2021-08-31 | 2023-10-13 | 江西盖亚环保科技有限公司 | Process for removing dioxin from fly ash |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP0813438B1 (en) | Feed processing employing dispersed molten droplets | |
| JP4243295B2 (en) | Low-temperature catalytic gasification apparatus and method for biomass refined fuel | |
| US7157167B1 (en) | Thermocatalytic process for CO2-free production of hydrogen and carbon from hydrocarbons | |
| TW412434B (en) | Process of removing mercury, mercury compounds, and polyhalogenated hydrocarbons from oxygen-containing exhaust gases produced by the combustion of garbage, industrial waste materials, and sewage sludge | |
| US6084147A (en) | Pyrolytic decomposition of organic wastes | |
| TWI407999B (en) | Activated regenerator for activated carbon, and gas purifying method and apparatus using the same | |
| JP2007196215A (en) | Adsorbent for removing trace harmful air pollutant in combustion flue gas and its manufacturing method | |
| KR20020020931A (en) | Process and apparatus for production of hydrogen by gasification of combustible material and method for electric power generation using fuel cell and electric power generation system using fuel cell | |
| CN107261788A (en) | The removal methods and device of a kind of high-temperature flue gas Zhong bioxin | |
| US5405812A (en) | Method and arrangement for purifying a carbon-containing adsorption medium | |
| FI74753B (en) | FOERFARANDE OCH ANORDNING FOER TILLVARATAGANDE AV ENERGI OCH KEMISKA PRODUKTER UR ANVAEND SELLULOSALUT. | |
| EP1195353A1 (en) | Method and apparatus for production of hydrogen by gasification of combusible material | |
| JP5403574B2 (en) | Gasification system using activated carbon extracted from a tar absorption tower. | |
| JPH11276856A (en) | Treatment of dioxin-containing gas and device therefor | |
| JP3565972B2 (en) | Wet oxidation method of waste soda | |
| JP2008029967A (en) | Method and apparatus for treating contaminants | |
| US7052661B1 (en) | Method for abatement of mercury emissions from combustion gases | |
| JP2011105890A (en) | Circulating fluidized bed gasification reactor | |
| JP4734649B2 (en) | Decomposition processing apparatus and decomposition processing method of hardly decomposable organic compound | |
| JP2007099827A (en) | Fuel gas refining system | |
| JPH11290639A (en) | Method and apparatus for continuous treatment of dioxins-containing gas | |
| JPH11276855A (en) | Treatment of dioxin-containing gas and device therefor | |
| JPH11226356A (en) | Method and apparatus for treating dioxin | |
| JP2018058002A (en) | Gas treatment apparatus and gas treatment method | |
| JP2000274622A (en) | Processing method for waste containing high concentration dioxins |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20060516 |
|
| A521 | Written amendment |
Free format text: JAPANESE INTERMEDIATE CODE: A523 Effective date: 20060814 |
|
| TRDD | Decision of grant or rejection written | ||
| A01 | Written decision to grant a patent or to grant a registration (utility model) |
Free format text: JAPANESE INTERMEDIATE CODE: A01 Effective date: 20061107 |
|
| A61 | First payment of annual fees (during grant procedure) |
Free format text: JAPANESE INTERMEDIATE CODE: A61 Effective date: 20061114 |
|
| R150 | Certificate of patent (=grant) or registration of utility model |
Free format text: JAPANESE INTERMEDIATE CODE: R150 |
|
| LAPS | Cancellation because of no payment of annual fees |