JP3046309B1 - Method and apparatus for reducing dioxins in a garbage gasifier for char separation - Google Patents
Method and apparatus for reducing dioxins in a garbage gasifier for char separationInfo
- Publication number
- JP3046309B1 JP3046309B1 JP26510599A JP26510599A JP3046309B1 JP 3046309 B1 JP3046309 B1 JP 3046309B1 JP 26510599 A JP26510599 A JP 26510599A JP 26510599 A JP26510599 A JP 26510599A JP 3046309 B1 JP3046309 B1 JP 3046309B1
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- JP
- Japan
- Prior art keywords
- exhaust gas
- melting
- char
- gas
- melting furnace
- 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.)
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Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/20—Waste processing or separation
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- Chimneys And Flues (AREA)
- Gasification And Melting Of Waste (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
【要約】
【課題】 チャー分離方式ごみガス化溶融装置におい
て、飛灰中及び排ガス中のダイオキシン類の低減化を図
る。
【解決手段】 溶融炉３０と減温塔２１とを溶融炉排ガ
ス導管３６ａを介して直接接続して、溶融炉３０からの
排ガスの顕熱を回収することなく、ボイラ１６及び空気
予熱器１８を介さずに、溶融炉３０からの排ガスを減温
塔２１に直接導入し冷却する。To reduce dioxins in fly ash and exhaust gas in a char separation type refuse gasification / melting apparatus. SOLUTION: A melting furnace 30 and a cooling tower 21 are directly connected via a melting furnace exhaust gas conduit 36a, and the boiler 16 and the air preheater 18 are connected without recovering the sensible heat of the exhaust gas from the melting furnace 30. The exhaust gas from the melting furnace 30 is directly introduced into the cooling tower 21 and cooled without any intervention.
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、都市ごみ、産業廃
棄物、ごみ固形燃料（ＲＤＦ）等の固体可燃物（以下、
単にごみと総称する）をガス化炉でガス化（部分燃焼）
し、チャー（未燃炭素）及び灰を含む未燃ガス（熱分解
ガス）を固気分離器に導入して固気分離し、分離された
未燃ガスをボイラに導入し、分離されたチャー及び灰を
溶融炉に導入するチャー分離方式ごみガス化溶融装置に
おける飛灰中及び排ガス中のダイオキシン類の低減方法
及び装置に関するものである。The present invention relates to solid combustibles (hereinafter referred to as municipal solid waste, industrial waste, solid waste fuel (RDF), etc.).
(Collectively called garbage) is gasified in a gasifier (partial combustion)
Then, char (unburned carbon) and unburned gas (pyrolyzed gas) containing ash are introduced into a solid-gas separator to be separated into solid and gas, and the separated unburned gas is introduced into a boiler. The present invention relates to a method and an apparatus for reducing dioxins in fly ash and exhaust gas in a char separation type gasification and melting apparatus for introducing ash into a melting furnace.
【０００２】[0002]
【従来の技術】従来から、チャー分離方式ごみガス化溶
融装置は既に知られている（例えば、特許第２８９５４
６９号公報参照（とくに図１０））。図３は、従来のチ
ャー分離方式ごみガス化溶融装置の一例を示している。
流動層ガス化炉（部分燃焼炉）１０に投入されたごみ
は、低空気比（例えば、０．１５〜０．４、望ましくは
０．２〜０．３）で部分燃焼し、未燃ガス（熱分解ガ
ス）と、チャー（未燃炭素）を含む未燃灰とに熱分解さ
れる。未燃灰（チャー及び灰）を含む未燃ガスは、ガス
化炉１０のフリーボード１２から固気分離器、例えば、
サイクロン１４に導入され、未燃ガスと未燃灰とに分離
される。2. Description of the Related Art Conventionally, a garbage gasifying and melting apparatus using a char separation method is already known (for example, Japanese Patent No. 28954).
See No. 69 (especially FIG. 10). FIG. 3 shows an example of a conventional char separation type waste gasification and melting apparatus.
The refuse introduced into the fluidized-bed gasification furnace (partial combustion furnace) 10 partially burns at a low air ratio (for example, 0.15 to 0.4, desirably 0.2 to 0.3) and generates unburned gas. (Pyrolysis gas) and unburned ash containing char (unburned carbon). Unburned gas including unburned ash (char and ash) is separated from the freeboard 12 of the gasifier 10 by a solid-gas separator, for example,
It is introduced into the cyclone 14 and separated into unburned gas and unburned ash.
【０００３】分離された未燃ガスはボイラ１６に導入さ
れ燃焼して蒸気を発生させた後、ボイラ１６からの排ガ
スは空気予熱器１８に導入され空気を予熱して燃焼用空
気及び流動化空気とし、空気予熱器１８からの排ガスは
減温塔２０に導入され冷却される。そして、減温塔２０
で冷却された排ガス中に活性炭又は／及び石灰（例え
ば、消石灰）が添加された後、この排ガスはバグフィル
ター２３に導入され、排ガス中のダイオキシン類、塩化
水素・硫黄酸化物等の酸性ガス成分が除去される。２４
は過熱器、２６は過熱器又は蒸発器、２８は蒸発器であ
る。[0003] The separated unburned gas is introduced into a boiler 16 and burns to generate steam. The exhaust gas from the boiler 16 is introduced into an air preheater 18 to preheat the air to burn air and fluidized air. The exhaust gas from the air preheater 18 is introduced into the cooling tower 20 and cooled. And the cooling tower 20
After activated carbon and / or lime (for example, slaked lime) is added to the exhaust gas cooled in the above, the exhaust gas is introduced into the bag filter 23, and acid gas components such as dioxins, hydrogen chloride and sulfur oxide in the exhaust gas. Is removed. 24
Is a superheater, 26 is a superheater or evaporator, and 28 is an evaporator.
【０００４】サイクロン１４で分離された未燃灰（チャ
ー及び灰）は旋回溶融炉３０に導入されてチャーが燃焼
するとともに、灰が溶融してスラグとなる。３２は水タ
ンクである。流動層ガス化炉１０の底部から排出される
流動媒体（砂）、灰及び大塊不燃物の混合物は振動ふる
い等の分級機３４に導入され、大塊不燃物及び灰が系外
に抜き出され、砂は循環使用される。[0004] The unburned ash (char and ash) separated by the cyclone 14 is introduced into the swirling melting furnace 30 to burn the char, and the ash is melted to form slag. 32 is a water tank. The mixture of fluidized medium (sand), ash and large incombustibles discharged from the bottom of the fluidized bed gasifier 10 is introduced into a classifier 34 such as a vibrating sieve, and the large incombustibles and ash are extracted out of the system. And the sand is recycled.
【０００５】図３に示す従来のチャー分離方式ごみガス
化溶融装置においては、溶融炉３０からの高温（例え
ば、１３００〜１４００℃）の排ガスの顕熱を回収する
ために、溶融炉排ガス導管３６はボイラ１６に接続され
ている。この場合、溶融炉排ガス中には、ＣａＣｌ2、
ＫＣｌ、ＮａＣｌ等の塩化物を高濃度で含む飛灰、高濃
度の塩化水素が含まれるので、塩化物のコーチングや伝
熱管の腐蝕等が発生する。そこで、特に過熱器２４の高
温腐食を防止するために、溶融炉排ガス導管３６は過熱
器２４の下流側に接続されている。図３に示す従来のチ
ャー分離方式ごみガス化溶融装置は、つぎのような利点
を有している。 （１） 旋回溶融炉にチャーが定量供給されるので、安
定した溶融運転ができる。チャーの低位発熱量は、水分
が全て未燃ガス側に分離されるため通常２５００〜３０
００kcal／kg程度と比較的高く、炉の処理量がある程度
大きくなるとチャーの燃焼熱を利用して灰を溶融するこ
とができる。すなわち、自己熱溶融することができる。 （２） 溶融炉排ガス導管３６を過熱器２４の下流側に
接続することにより、過熱器まわりのガス中塩化水素濃
度が低くなり、過熱器出口蒸気温度を従来より高く設定
でき、発電効率が向上する。 （３） 総空気比が１．３程度と小さいので（ガス化炉
を用いずに通常の燃焼炉を用いる場合の総空気比は１．
８以上と大きい）、排ガス量が少なくなり、各機器、配
管を小型、コンパクトにすることができる。In the conventional char separation type waste gasification and melting apparatus shown in FIG. 3, in order to recover the sensible heat of the high temperature (for example, 1300 to 1400 ° C.) exhaust gas from the melting furnace 30, a melting furnace exhaust gas conduit 36 is provided. Is connected to the boiler 16. In this case, CaCl 2 ,
Since fly ash containing a high concentration of chlorides such as KCl and NaCl and high concentration of hydrogen chloride are contained, coating of chlorides and corrosion of heat transfer tubes and the like occur. Therefore, in order to prevent high-temperature corrosion of the superheater 24 in particular, the melting furnace exhaust gas conduit 36 is connected to the downstream side of the superheater 24. The conventional char separation type waste gasification and melting apparatus shown in FIG. 3 has the following advantages. (1) Since a fixed amount of char is supplied to the swirling melting furnace, stable melting operation can be performed. The lower calorific value of the char is usually 2,500 to 30, since all the water is separated to the unburned gas side.
It is relatively high at about 00 kcal / kg, and when the throughput of the furnace is increased to some extent, the ash can be melted using the combustion heat of the char. That is, self-heating can be performed. (2) By connecting the melting furnace exhaust gas conduit 36 to the downstream side of the superheater 24, the concentration of hydrogen chloride in the gas around the superheater is reduced, and the superheater outlet steam temperature can be set higher than before, thereby improving power generation efficiency. I do. (3) Since the total air ratio is as small as about 1.3 (the total air ratio when a normal combustion furnace is used without using a gasifier is 1.
8 or more), the amount of exhaust gas is reduced, and each device and piping can be made small and compact.
【０００６】[0006]
【発明が解決しようとする課題】しかし、図３に示す従
来のチャー分離方式ごみガス化溶融装置の構成では、ボ
イラ１６の低温部及び空気予熱器１８内が、ダイオキシ
ン類の合成温度として知られている６００〜２００℃
（とくに５００〜３００℃）の温度域となり、かつ、溶
融炉排ガスに含まれていた飛灰中にＣａＣｌ2、ＫＣ
ｌ、ＮａＣｌ等の塩化物が高濃度で、しかも溶融して付
着性が高い状態で通過するので、ボイラ１６の低温部及
び空気予熱器１８内の伝熱管や壁面等に塩化物が、未燃
物やダイオキシン類生成の触媒となるといわれている
銅、鉄等の粉末とともに付着・堆積する。この付着物と
塩化水素を含む排ガスとが十分長時間にわたり接触して
ダイオキシン類が生成されていることは、この温度域に
おいて炉出口のダイオキシン類濃度が数倍から数十倍に
なることから、容易に類推され、半ば公知の事実となっ
ている。すなわち、ダイオキシン類は排ガス中で瞬間的
に合成されるのではなく、排ガスと灰とが接触して灰中
で比較的長い時間をかけて生成されているとの知見は広
く知れわたっている。However, in the configuration of the conventional char separation type waste gasification and melting apparatus shown in FIG. 3, the low temperature section of the boiler 16 and the inside of the air preheater 18 are known as the synthesis temperature of dioxins. 600-200 ° C
(Especially 500 to 300 ° C) and CaCl 2 , KC
Since the chlorides such as 1 and NaCl have a high concentration and are melted and pass through in a state of high adhesion, the chlorides are unburned in the low-temperature portion of the boiler 16 and the heat transfer tubes and wall surfaces in the air preheater 18. It adheres and accumulates together with powders of copper, iron, etc., which are said to be catalysts for the production of substances and dioxins. The fact that dioxins are produced by the contact between the deposits and the exhaust gas containing hydrogen chloride for a sufficiently long time, because the concentration of dioxins at the furnace outlet in this temperature range becomes several times to several tens times, It is easily inferred and is a known fact. That is, it is widely known that dioxins are not instantaneously synthesized in exhaust gas, but are generated over a relatively long time in ash due to contact between exhaust gas and ash.
【０００７】本発明は上記の知見に基づきなされたもの
で、本発明の目的は、溶融炉排ガスをボイラ及び空気予
熱器をバイパスさせて、減温塔に直接導入することによ
り、ＨＣｌ濃度が高く、かつ塩化物を高濃度で含む飛灰
を含有する溶融炉排ガスを減温塔でダイオキシン類の合
成温度以下に急冷して、ＨＣｌ濃度が高く、かつ塩化物
を高濃度で含む飛灰を含有する溶融炉排ガスラインでの
ダイオキシン類生成を抑制した飛灰中及び排ガス中のダ
イオキシン類を低減することができる方法及び装置を提
供することにある。[0007] The present invention has been made based on the above-described findings, and an object of the present invention is to introduce a molten furnace exhaust gas directly into a cooling tower by bypassing a boiler and an air preheater, thereby increasing the HCl concentration. In addition, the melting furnace exhaust gas containing fly ash containing a high concentration of chloride is quenched to a temperature lower than the synthesis temperature of dioxins in a cooling tower to contain fly ash having a high HCl concentration and a high chloride concentration. It is an object of the present invention to provide a method and an apparatus capable of reducing dioxins in fly ash and exhaust gas while suppressing generation of dioxins in a melting furnace exhaust gas line.
【０００８】[0008]
【課題を解決するための手段】上記の目的を達成するた
めに、本発明のチャー分離方式ごみガス化溶融装置にお
けるダイオキシン類の低減方法は、ごみをガス化炉に供
給してガス化させ、チャー及び灰を含む未燃ガスをフリ
ーボードから固気分離器に導入して固気分離し、固気分
離された未燃ガスをボイラに導入し燃焼させて蒸気を発
生させた後、ボイラからの排ガスを空気予熱器に導入し
て空気を予熱し、空気予熱器からの排ガスを減温塔に導
入して冷却し、一方、固気分離されたチャー及び灰を溶
融炉に導入しチャーを燃焼させるとともに灰を溶融して
スラグとするチャー分離方式ごみガス化溶融装置におい
て、溶融炉からの排ガスの顕熱を回収することなく、ボ
イラ及び空気予熱器を介さずに、溶融炉からの排ガスを
減温塔に直接導入し冷却するように構成されている（図
１、図２参照）。In order to achieve the above object, a method for reducing dioxins in a char separation type refuse gasification and melting apparatus according to the present invention is to supply refuse to a gasification furnace to gasify the refuse. The unburned gas containing char and ash is introduced from the free board into the solid-gas separator to separate it into solid and gas, and the solid-gas separated unburned gas is introduced into the boiler and burned to generate steam. The exhaust gas is introduced into the air preheater to preheat the air, and the exhaust gas from the air preheater is introduced into the cooling tower and cooled, while the char and ash separated into solid and gas are introduced into the melting furnace to burn the char In the char separation type refuse gasification and melting equipment that melts the ash and turns it into slag, without collecting the sensible heat of the exhaust gas from the melting furnace, the exhaust gas from the melting furnace is not passed through the boiler and air preheater. Directly introduced into cooling tower Is configured to cool (see FIGS. 1 and 2).
【０００９】本発明のチャー分離方式ごみガス化溶融装
置におけるダイオキシン類の低減装置は、ごみを還元雰
囲気でガス化処理するガス化炉と、このガス化炉のフリ
ーボード部に接続された固気分離器と、この固気分離器
の後流に未燃ガス導管を介して接続されたボイラと、こ
のボイラに排ガス導管を介して接続された空気予熱器
と、この空気予熱器に排ガス導管を介して接続された減
温塔と、前記固気分離器の下部にチャー・灰搬送手段を
介して接続された溶融炉とを備えたチャー分離方式ごみ
ガス化溶融装置において、溶融炉と減温塔とが溶融炉排
ガス導管を介して直接接続されていることを特徴として
いる（図１、図２参照）。上記の構成において、ガス化
炉を流動層ガス化炉とし、溶融炉を旋回溶融炉とするこ
とが好ましい。An apparatus for reducing dioxins in a char separation type refuse gasification / melting apparatus according to the present invention comprises a gasification furnace for gasifying refuse in a reducing atmosphere, and a solid gas connected to a free board portion of the gasification furnace. A separator, a boiler connected to the wake of the solid-gas separator via an unburned gas conduit, an air preheater connected to the boiler via an exhaust gas conduit, and an exhaust gas conduit connected to the air preheater. And a melting furnace connected to the lower part of the solid-gas separator via a char / ash conveying means. It is characterized in that the tower and the tower are directly connected via a melting furnace exhaust gas conduit (see FIGS. 1 and 2). In the above configuration, it is preferable that the gasification furnace be a fluidized bed gasification furnace and the melting furnace be a swirling melting furnace.
【００１０】[0010]
【発明の実施の形態】以下、本発明の実施の形態につい
て説明するが、本発明は下記の実施の形態に何ら限定さ
れるものではなく、適宜変更して実施することができる
ものである。図１は、本発明の実施の第１形態によるチ
ャー分離方式ごみガス化溶融装置におけるダイオキシン
類の低減装置を示している。本実施形態では、ガス化炉
として流動層ガス化炉、溶融炉として旋回溶融炉を用い
る場合を示しているが、他の形式のガス化炉、溶融炉を
用いることも可能である。DESCRIPTION OF THE PREFERRED EMBODIMENTS Embodiments of the present invention will be described below, but the present invention is not limited to the following embodiments and can be implemented with appropriate modifications. FIG. 1 shows an apparatus for reducing dioxins in a char separation type waste gasification and melting apparatus according to a first embodiment of the present invention. In the present embodiment, a case where a fluidized-bed gasification furnace is used as a gasification furnace and a swirling melting furnace is used as a melting furnace, but other types of gasification furnaces and melting furnaces can be used.
【００１１】１０は流動層ガス化炉で、このガス化炉１
０のフリーボード１２に固気分離器、例えば、サイクロ
ン１４が接続されている。流動層ガス化炉１０は、図１
では散気管タイプのものを示しているが、空気分散板タ
イプのものを用いることも、勿論可能である。サイクロ
ン１４の上部（後流）には未燃ガス導管３８を介してボ
イラ１６が接続され、このボイラ１６に排ガス導管４０
を介して空気予熱器１８が接続され、この空気予熱器１
８に排ガス導管４２を介して２次減温塔２２が接続され
ている。Reference numeral 10 denotes a fluidized-bed gasification furnace.
The solid-gas separator, for example, a cyclone 14 is connected to the free board 12. The fluidized-bed gasifier 10 is shown in FIG.
Although a diffuser type is shown in FIG. 1, it is of course possible to use an air distribution plate type. The boiler 16 is connected to the upper part (the downstream side) of the cyclone 14 via an unburned gas conduit 38, and the boiler 16 is connected to an exhaust gas conduit 40.
The air preheater 18 is connected via the
The secondary cooling tower 22 is connected to 8 via an exhaust gas conduit 42.
【００１２】また、サイクロン１４の下部にはチャー・
灰搬送手段４４、例えば、ロータリフィーダ等の排出機
を備えた配管を介して旋回溶融炉３０が接続されてい
る。この旋回溶融炉３０は、チャー及び灰、燃焼用空
気、必要に応じて補助燃料を供給して予燃焼させる予燃
焼部４６と、この予燃焼部４６が接線方向に連結された
略円筒形の旋回溶融部４８と、この旋回溶融部４８に連
結された再燃焼部５０と、旋回溶融部４８の下面にスラ
グ流下口を介して連結されたスラグ冷却用の水タンク３
２とからなっている。[0012] In the lower part of the cyclone 14 is a char.
The swirling melting furnace 30 is connected to the ash conveying means 44 via a pipe provided with a discharger such as a rotary feeder. The swirling melting furnace 30 includes a pre-combustion unit 46 that supplies char and ash, combustion air, and auxiliary fuel as needed to pre-combust, and a substantially cylindrical shape in which the pre-combustion unit 46 is tangentially connected. A swirling / melting unit 48, a reburning unit 50 connected to the swirling / melting unit 48, and a slag cooling water tank 3 connected to a lower surface of the swirling / melting unit 48 via a slag flow outlet.
It consists of two.
【００１３】旋回溶融炉３０の再燃焼部５０と１次減温
塔２１とは、溶融炉排ガス導管３６ａを介して直接接続
されている。図１においては、１次減温塔排ガス導管３
７が、空気予熱器１８からの排ガス導管４２と合流して
２次減温塔２２に接続される場合を、一例として示して
いる。The reburning section 50 of the swirling melting furnace 30 is directly connected to the primary cooling tower 21 via a melting furnace exhaust gas conduit 36a. In FIG. 1, the primary cooling tower exhaust gas conduit 3
7 shows, as an example, a case where the fuel cell 7 is joined to the exhaust gas conduit 42 from the air preheater 18 and connected to the secondary cooling tower 22.
【００１４】つぎに、図１に示す装置の作用について説
明する。流動層ガス化炉（部分燃焼炉）１０に投入され
たごみは、低空気比（例えば、０．１５〜０．４、望ま
しくは０．２〜０．３）で部分燃焼し、未燃ガス（熱分
解ガス）と、チャー（未燃炭素）を含む未燃灰とに熱分
解される。未燃灰（チャー及び灰）を含む未燃ガスは、
ガス化炉１０のフリーボード１２からサイクロン１４に
導入され、未燃ガスと未燃灰とに分離される。この時、
ごみ中の塩素分の大部分（例えば、７０〜８０wt％）は
ＣａＣｌ2、ＫＣｌ、ＮａＣｌ等の塩化物となって灰中
に含まれサイクロン１４下部から分離される。サイクロ
ン１４上部から分離される未燃ガス中には、ごみ中の塩
素分の残部（例えば、２０〜３０wt％）が、飛灰中の塩
化物、及びＨＣｌガスとして含まれる。Next, the operation of the apparatus shown in FIG. 1 will be described. The refuse introduced into the fluidized-bed gasification furnace (partial combustion furnace) 10 partially burns at a low air ratio (for example, 0.15 to 0.4, desirably 0.2 to 0.3) and generates unburned gas. (Pyrolysis gas) and unburned ash containing char (unburned carbon). Unburned gas containing unburned ash (char and ash)
The gas is introduced into the cyclone 14 from the free board 12 of the gasifier 10 and separated into unburned gas and unburned ash. At this time,
Most of the chlorine content in the refuse (for example, 70 to 80 wt%) is converted into chlorides such as CaCl 2 , KCl, and NaCl, contained in the ash, and separated from the lower part of the cyclone 14. In the unburned gas separated from the upper part of the cyclone 14, the remaining chlorine (eg, 20 to 30% by weight) in the refuse is included as chloride in the fly ash and HCl gas.
【００１５】分離された未燃ガスは、未燃ガス導管３８
を通ってボイラ１６に導入され燃焼して蒸気を発生させ
た後、ボイラ１６からの排ガスは、排ガス導管４０を通
って空気予熱器１８に導入され空気を予熱して燃焼用空
気及び流動化空気とし、空気予熱器１８からの排ガス
は、排ガス導管４２を通って２次減温塔２２に導入され
冷却される。そして、２次減温塔２２で冷却された排ガ
ス中に活性炭又は／及び石灰（例えば、消石灰）が添加
された後、この排ガスはバグフィルター２３に導入さ
れ、排ガス中のダイオキシン類、塩化水素・硫黄酸化物
等の酸性ガス成分が除去される。２４は過熱器、２６は
過熱器又は蒸発器、２８は蒸発器である。なお、空気予
熱器１８で予熱された空気の一部は、流動化空気として
流動層ガス化炉１０の散気管へ供給され、予熱された空
気の残部は、燃焼用空気として旋回溶融炉３０の予燃焼
部４６、再燃焼部５０及びボイラ１６へ供給される。ま
た、流動層ガス化炉１０の底部から排出される流動媒体
（砂）、灰及び大塊不燃物の混合物は振動ふるい等の分
級機３４に導入され、大塊不燃物及び灰が系外に抜き出
され、砂は循環使用される。The separated unburned gas is supplied to an unburned gas conduit 38.
After passing through the boiler 16 and burning to generate steam, the exhaust gas from the boiler 16 is introduced into an air preheater 18 through an exhaust gas conduit 40 to preheat the air to generate combustion air and fluidized air. The exhaust gas from the air preheater 18 is introduced into the secondary cooling tower 22 through the exhaust gas conduit 42 and is cooled. Then, after activated carbon and / or lime (for example, slaked lime) is added to the exhaust gas cooled in the secondary cooling tower 22, the exhaust gas is introduced into the bag filter 23, and dioxins, hydrogen chloride, Acid gas components such as sulfur oxides are removed. 24 is a superheater, 26 is a superheater or evaporator, and 28 is an evaporator. A part of the air preheated by the air preheater 18 is supplied as fluidized air to the diffuser pipe of the fluidized bed gasifier 10, and the rest of the preheated air is supplied to the swirling melting furnace 30 as combustion air. It is supplied to the pre-combustion unit 46, the re-combustion unit 50, and the boiler 16. The mixture of the fluid medium (sand), the ash and the large incombustible material discharged from the bottom of the fluidized bed gasifier 10 is introduced into a classifier 34 such as a vibrating sieve, and the large incombustible material and the ash are removed from the system. It is extracted and the sand is recycled.
【００１６】サイクロン１４で分離された未燃灰（チャ
ー及び灰）は旋回溶融炉３０の予燃焼部４６に、燃焼用
空気、必要に応じて補助燃料とともに供給され、ここで
チャーの大部分は燃焼する。予燃焼部４６からの予燃焼
ガスは略円筒形の旋回溶融部４８に接線方向に導入さ
れ、残りのチャーの一部が周壁に付着して捕捉され、燃
焼する。また、灰の大部分（例えば、８０〜９０wt％）
は溶融してスラグとなり旋回溶融部４８から水タンク３
２内に落下し冷却されて水冷スラグとなって、コンベア
等の排出機により取り出される。旋回溶融部４８からの
排ガスは再燃焼部５０に導入され、ここで燃焼に必要な
空気が追加供給されて完全燃焼が図られる。The unburned ash (char and ash) separated in the cyclone 14 is supplied to a pre-combustion section 46 of the swirling melting furnace 30 together with combustion air and, if necessary, auxiliary fuel, where most of the char is formed. Burn. The pre-combustion gas from the pre-combustion section 46 is tangentially introduced into the substantially cylindrical swirl / melting section 48, and a part of the remaining char adheres to the peripheral wall and is captured and burns. Most of the ash (for example, 80 to 90 wt%)
Melts into slag and turns into the water tank 3
It falls into 2 and is cooled to become a water-cooled slag, which is taken out by a discharger such as a conveyor. Exhaust gas from the swirling / melting unit 48 is introduced into the reburning unit 50, where air necessary for combustion is additionally supplied to complete combustion.
【００１７】旋回溶融炉３０の旋回溶融部４８内は高温
（例えば、１３００〜１４００℃）であるので、灰中に
含まれているＣａＣｌ2、ＫＣｌ、ＮａＣｌ等の塩化物
は分解して、塩素分はＨＣｌガスとなって排ガス中に移
行する。したがって、スラグ中には塩素分は含まれない
か、又は微量の塩素分が含まれることになる。上記のよ
うに、溶融炉排ガス中には高濃度のＨＣｌが含まれてお
り、さらに、スラグ化しなかった灰（旋回溶融部４８に
導入された灰の、例えば、１０〜２０wt％）が飛灰とな
って含まれている。ガス温度が低下するとＨＣｌと飛灰
中のＣａ、Ｋ、Ｎａ等が反応し、ＣａＣｌ2、ＫＣｌ、
ＮａＣｌ等の塩化物が生成する。Since the inside of the swirling melting section 48 of the swirling melting furnace 30 is at a high temperature (for example, 1300 to 1400 ° C.), chlorides such as CaCl 2 , KCl, and NaCl contained in the ash are decomposed to chlorine. The portion becomes HCl gas and moves into the exhaust gas. Therefore, the slag contains no chlorine or a trace amount of chlorine. As described above, high-concentration HCl is contained in the exhaust gas of the melting furnace, and ash that has not been slagged (for example, 10 to 20% by weight of the ash introduced into the swirling melting section 48) is fly ash. Included. When the gas temperature decreases, HCl reacts with Ca, K, Na and the like in fly ash, and CaCl 2 , KCl,
Chloride such as NaCl is produced.
【００１８】高濃度のＨＣｌ、及び高濃度の塩化物を含
む飛灰を含有する溶融炉排ガスを、溶融炉排ガス導管３
６ａを通して１次減温塔２１へ直接導入し、散水等の手
段により、溶融炉排ガスを急冷して塩化物が溶融して付
着性が高く、かつ、ダイオキシン類の生成温度となる６
００〜２００℃（とくに５００〜３００℃）の温度域を
急速に通過させる。このようにすることにより、ＨＣｌ
濃度が高く、かつ塩化物を高濃度で含む飛灰を含有する
溶融炉排ガス処理系統でのダイオキシン類生成を効果的
に抑制することができる。このため、１次減温塔２１で
捕捉されたダスト（飛灰）、バグフィルター２３で捕捉
されたダスト（飛灰を含む）中のダイオキシン類を低減
させることができ、かつ、バグフィルター２３からの排
ガス中のダイオキシン類を低減させることができる。な
お、本実施形態では、減温塔を２基用いる場合について
説明しているが、１基又は３基以上とすることも可能で
ある。The melting furnace exhaust gas containing high concentration HCl and fly ash containing high concentration chloride is supplied to the melting furnace exhaust gas conduit 3.
6a, the mixture is directly introduced into the primary cooling tower 21 and the exhaust gas from the melting furnace is quenched by means such as water sprinkling, so that the chlorides are melted and the adhesion is high, and the temperature at which the dioxins are formed is reached.
Rapidly pass through a temperature range of 00 to 200 ° C (particularly 500 to 300 ° C). By doing so, HCl
It is possible to effectively suppress the generation of dioxins in a melting furnace exhaust gas treatment system containing a fly ash having a high concentration and containing a high concentration of chloride. Therefore, dioxins in dust (fly ash) captured by the primary cooling tower 21 and dust (including fly ash) captured by the bag filter 23 can be reduced. Dioxins in the exhaust gas can be reduced. In the present embodiment, the case where two cooling towers are used is described, but one or three or more cooling towers can be used.
【００１９】図２は、本発明の実施の第２形態によるチ
ャー分離方式ごみガス化溶融装置におけるダイオキシン
類の低減装置を示している。本実施形態は、１次減温塔
排ガス導管３７を空気予熱器１８からの排ガス導管４２
に合流させることなく、１次減温塔排ガス導管３７を２
次減温塔２２の上部に直接接続したものである。他の構
成及び作用は、実施の第１形態の場合と同様である。FIG. 2 shows an apparatus for reducing dioxins in a char separation type refuse gasification and melting apparatus according to a second embodiment of the present invention. In the present embodiment, the primary degassing tower exhaust gas conduit 37 is connected to the exhaust gas conduit 42 from the air preheater 18.
Without being connected to the primary cooling tower exhaust gas conduit 37
It is directly connected to the upper part of the next cooling tower 22. Other configurations and operations are the same as those in the first embodiment.
【００２０】[0020]
【発明の効果】本発明は上記のように構成されているの
で、つぎのような効果を奏する。 （１） ＨＣｌ濃度が高く、かつ、ＣａＣｌ2、ＫＣ
ｌ、ＮａＣｌ等の塩化物を高濃度で含む飛灰を含有する
溶融炉排ガスを、ボイラ及び空気予熱器をバイパスさせ
て、減温塔に直接導入し冷却するように構成されている
ので、灰中の塩化物濃度が大きく、付着性の高い溶融飛
灰が、ボイラ及び空気予熱器内の伝熱管や壁面等に付着
・堆積してダイオキシン類が合成され易い環境（雰囲
気）をつくることがなく、このため、飛灰中及び排ガス
中のダイオキシン類の低減化を図ることができる。 （２） 上記（１）のように、ボイラ及び空気予熱器内
の塩化物のコーチングが抑制されるので、装置の閉塞や
熱回収量の低下のトラブルが軽減され、安定な運転を継
続することができる。 （３） 上記（１）のように、溶融炉排ガスを、ボイラ
及び空気予熱器を介さずに、減温塔に直接導入している
ので、ボイラ及び空気予熱器の塩化水素による腐蝕の低
減を図ることができる。As described above, the present invention has the following effects. (1) High HCl concentration, CaCl 2 , KC
1, the melting furnace exhaust gas containing fly ash containing a high concentration of chlorides such as NaCl is directly introduced into the cooling tower and cooled by bypassing the boiler and the air preheater. Chloride concentration in the inside is high, and high-melting fly ash adheres and accumulates on heat transfer tubes and wall surfaces in boilers and air preheaters without creating an environment (atmosphere) where dioxins are easily synthesized. Therefore, dioxins in fly ash and exhaust gas can be reduced. (2) As described in (1) above, since the coating of chloride in the boiler and the air preheater is suppressed, troubles such as clogging of the device and reduction in the amount of heat recovery are reduced, and stable operation is continued. Can be. (3) As described in (1) above, since the melting furnace exhaust gas is directly introduced into the cooling tower without passing through the boiler and the air preheater, the corrosion of the boiler and the air preheater due to hydrogen chloride can be reduced. Can be planned.
【図１】本発明の実施の第１形態によるチャー分離方式
ごみガス化溶融装置におけるダイオキシン類の低減装置
の系統的概略構成図である。FIG. 1 is a systematic schematic configuration diagram of a dioxin reducing device in a char separation type waste gasification / melting device according to a first embodiment of the present invention.
【図２】本発明の実施の第２形態によるチャー分離方式
ごみガス化溶融装置におけるダイオキシン類の低減装置
の系統的概略構成図である。FIG. 2 is a systematic schematic configuration diagram of an apparatus for reducing dioxins in a char separation type waste gasification / melting apparatus according to a second embodiment of the present invention.
【図３】従来のチャー分離方式ごみガス化溶融装置の一
例を示す系統的概略構成図である。FIG. 3 is a systematic schematic configuration diagram showing an example of a conventional char separation type waste gasification and melting apparatus.
１０ 流動層ガス化炉 １２ フリーボード １４ サイクロン １６ ボイラ １８ 空気予熱器 ２０ 減温塔 ２１ １次減温塔 ２２ ２次減温塔 ２３ バグフィルター ２４ 過熱器 ２６ 過熱器又は蒸発器 ２８ 蒸発器 ３０ 旋回溶融炉 ３２ 水タンク ３４ 分級機 ３６、３６ａ 溶融炉排ガス導管 ３７ １次減温塔排ガス導管 ３８ 未燃ガス導管 ４０ ボイラからの排ガス導管 ４２ 空気予熱器からの排ガス導管 ４４ チャー・灰搬送手段 ４６ 予燃焼部 ４８ 旋回溶融部 ５０ 再燃焼部 DESCRIPTION OF SYMBOLS 10 Fluidized-bed gasification furnace 12 Free board 14 Cyclone 16 Boiler 18 Air preheater 20 Temperature reducing tower 21 Primary temperature reducing tower 22 Secondary temperature reducing tower 23 Bag filter 24 Superheater 26 Superheater or evaporator 28 Evaporator 30 Rotation Melting furnace 32 Water tank 34 Classifier 36, 36a Melting furnace exhaust gas conduit 37 Primary cooling tower exhaust gas conduit 38 Unburned gas conduit 40 Exhaust gas conduit from boiler 42 Exhaust gas conduit from air preheater 44 Char / ash conveying means 46 Combustion part 48 Swirling melting part 50 Reburning part
───────────────────────────────────────────────────── フロントページの続き (72)発明者 熊谷 親徳 兵庫県明石市川崎町１番１号 川崎重工 業株式会社 明石工場内 (72)発明者 片畑 正 兵庫県明石市川崎町１番１号 川崎重工 業株式会社 明石工場内 (56)参考文献 特開 平11−132430（ＪＰ，Ａ) 特開 平10−230239（ＪＰ，Ａ) 特開 平10−232007（ＪＰ，Ａ) 特開 平８−219436（ＪＰ，Ａ) (58)調査した分野(Int.Cl.7，ＤＢ名) F23J 15/06 F23G 5/00 115 F23G 5/00 ZAB F23G 5/027 ZAB F23G 5/030 ZAB ──────────────────────────────────────────────────続 き Continuing on the front page (72) Inventor Chitoku Kumagai 1-1, Kawasaki-cho, Akashi-shi, Hyogo Kawasaki Heavy Industries, Ltd. Akashi Plant (72) Inventor Tadashi Katahata 1-1, Kawasaki-cho, Akashi-shi, Hyogo (56) References JP-A-11-132430 (JP, A) JP-A-10-230239 (JP, A) JP-A-10-232007 (JP, A) JP-A-8 −219436 (JP, A) (58) Fields investigated (Int. Cl. 7 , DB name) F23J 15/06 F23G 5/00 115 F23G 5/00 ZAB F23G 5/027 ZAB F23G 5/030 ZAB
Claims (3)
チャー及び灰を含む未燃ガスをフリーボードから固気分
離器に導入して固気分離し、固気分離された未燃ガスを
ボイラに導入し燃焼させて蒸気を発生させた後、ボイラ
からの排ガスを空気予熱器に導入して空気を予熱し、空
気予熱器からの排ガスを減温塔に導入して冷却し、一
方、固気分離されたチャー及び灰を溶融炉に導入しチャ
ーを燃焼させるとともに灰を溶融してスラグとするチャ
ー分離方式ごみガス化溶融装置において、 溶融炉からの排ガスを減温塔に直接導入し冷却すること
を特徴とするチャー分離方式ごみガス化溶融装置におけ
るダイオキシン類の低減方法。Claims: 1. Waste is supplied to a gasification furnace to be gasified,
The unburned gas containing char and ash is introduced from the free board into the solid-gas separator to separate it into solid and gas, and the solid-gas separated unburned gas is introduced into the boiler and burned to generate steam. The exhaust gas is introduced into the air preheater to preheat the air, and the exhaust gas from the air preheater is introduced into the cooling tower and cooled, while the char and ash separated into solid and gas are introduced into the melting furnace to burn the char A dioxin in a char separation-type gasification / melting system, in which exhaust gas from a melting furnace is directly introduced into a cooling tower and cooled by a char separation-type refuse gasification / melting device that makes slag by melting ash. How to reduce the kind.
化炉と、このガス化炉のフリーボード部に接続された固
気分離器と、この固気分離器の後流に未燃ガス導管を介
して接続されたボイラと、このボイラに排ガス導管を介
して接続された空気予熱器と、この空気予熱器に排ガス
導管を介して接続された減温塔と、前記固気分離器の下
部にチャー・灰搬送手段を介して接続された溶融炉とを
備えたチャー分離方式ごみガス化溶融装置において、 溶融炉と減温塔とが溶融炉排ガス導管を介して直接接続
されていることを特徴とするチャー分離方式ごみガス化
溶融装置におけるダイオキシン類の低減装置。2. A gasifier for gasifying garbage in a reducing atmosphere, a solid-gas separator connected to a free board part of the gasifier, and an unburned gas conduit downstream of the solid-gas separator. A boiler connected to the boiler, an air preheater connected to the boiler via an exhaust gas conduit, a cooling tower connected to the air preheater via an exhaust gas conduit, and a lower part of the solid-gas separator In a char separation type waste gasification / melting unit equipped with a melting furnace connected to the ash transfer means via a char / ash transfer means, the melting furnace and the cooling tower are connected directly via a melting furnace exhaust gas conduit. Characteristic device for reducing dioxins in char separation type waste gasification and melting equipment.
炉が旋回溶融炉である請求項２記載のチャー分離方式ご
みガス化溶融装置におけるダイオキシン類の低減装置。3. The apparatus for reducing dioxins in a char separation type refuse gasification and melting apparatus according to claim 2, wherein the gasification furnace is a fluidized bed gasification furnace and the melting furnace is a rotary melting furnace.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP26510599A JP3046309B1 (en) | 1999-09-20 | 1999-09-20 | Method and apparatus for reducing dioxins in a garbage gasifier for char separation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP26510599A JP3046309B1 (en) | 1999-09-20 | 1999-09-20 | Method and apparatus for reducing dioxins in a garbage gasifier for char separation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP3046309B1 true JP3046309B1 (en) | 2000-05-29 |
| JP2001090936A JP2001090936A (en) | 2001-04-03 |
Family
ID=17412684
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP26510599A Expired - Fee Related JP3046309B1 (en) | 1999-09-20 | 1999-09-20 | Method and apparatus for reducing dioxins in a garbage gasifier for char separation |
Country Status (1)
| Country | Link |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112834049A (en) * | 2021-01-13 | 2021-05-25 | 中冶长天国际工程有限责任公司 | Method and system for secondary detection and secondary treatment of high-temperature activated carbon |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112834049A (en) * | 2021-01-13 | 2021-05-25 | 中冶长天国际工程有限责任公司 | Method and system for secondary detection and secondary treatment of high-temperature activated carbon |
| CN112834049B (en) * | 2021-01-13 | 2024-05-03 | 中冶长天国际工程有限责任公司 | Method and system for secondary detection and secondary treatment of high-temperature activated carbon |
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