JP3491783B2 - Fluidized bed incinerator with fluidized media circulation path - Google Patents
Fluidized bed incinerator with fluidized media circulation pathInfo
- Publication number
- JP3491783B2 JP3491783B2 JP16310795A JP16310795A JP3491783B2 JP 3491783 B2 JP3491783 B2 JP 3491783B2 JP 16310795 A JP16310795 A JP 16310795A JP 16310795 A JP16310795 A JP 16310795A JP 3491783 B2 JP3491783 B2 JP 3491783B2
- Authority
- JP
- Japan
- Prior art keywords
- fluidized
- medium
- fluidized bed
- bed incinerator
- heat exchanger
- 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.)
- Expired - Fee Related
Links
Landscapes
- Incineration Of Waste (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Description
【０００１】[0001]
【産業上の利用分野】本発明は、流動床焼却炉に係り、
特に、流動床式の廃棄物、都市ゴミ焼却炉において熱を
効率良く、簡易に回収できる流動媒体循環経路を有する
流動床焼却装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a fluidized bed incinerator,
In particular, the present invention relates to a fluidized bed incinerator having a fluidized medium circulation path capable of efficiently and easily recovering heat in a fluidized bed type waste and municipal waste incinerator.
【０００２】[0002]
【従来の技術】流動床式の廃棄物、都市ゴミ焼却炉にお
いて熱エネルギーを回収する方式として、通常ボイラが
採用され排熱の回収と有効利用がされている。一般的な
流動床式の都市ゴミ焼却炉を図２に示す。排ガス１７の
温度は通常８００〜９５０℃の間に保たれている。低い
場合はバーナ２２により助燃され、高い場合は水スプレ
ー２３により冷却される。また、流動層７の温度も６０
０〜７５０℃程度の間に保たれている。その理由は高す
ぎると流動媒体の溶融、分散ノズルの腐食、都市ゴミの
ガス化が活発に起きるため未燃物の増加が起こり、低す
ぎると都市ゴミのガス化が起きなくなり炉内に都市ゴミ
が堆積してしまうためである。そのために、炉床の温度
は低い場合、バーナ２２により助燃され、高い場合は水
スプレー２３により冷却される。排熱の回収効率を上げ
るという意味では、水スプレーは排ガスからの熱損失を
増加させ好ましくないので、有効的な熱の回収方法が待
たれていた。2. Description of the Related Art As a method for recovering heat energy in a fluidized bed waste and municipal waste incinerator, a boiler is usually adopted to recover and effectively use exhaust heat. Figure 2 shows a general fluidized bed type municipal waste incinerator. The temperature of the exhaust gas 17 is usually kept between 800 and 950 ° C. When it is low, it is assisted by the burner 22, and when it is high, it is cooled by the water spray 23. The temperature of the fluidized bed 7 is also 60
It is maintained between 0 and 750 ° C. The reason for this is that if it is too high, melting of the fluid medium, corrosion of the dispersion nozzle, and gasification of municipal waste occur vigorously, which increases the amount of unburned materials. Is accumulated. Therefore, when the temperature of the hearth is low, it is assisted by the burner 22, and when it is high, it is cooled by the water spray 23. In terms of increasing the efficiency of recovering exhaust heat, water spray increases heat loss from exhaust gas and is not preferable, so an effective method for recovering heat has been awaited.
【０００３】通常の不燃物を含む流動床式の都市ゴミ焼
却炉において、都市ゴミ２１は炉内に投入後、一時に乾
燥→ガス化→燃焼というプロセスをたどる。流動床炉で
は、投入されたごみは流動砂によって解砕され、乾燥、
ガス化し、その後一部が砂中で、その他が燃焼室で燃焼
する。そして、この上部燃焼室には、二次空気２４が供
給される。焼却灰については、粒径の細かいものについ
ては灰と共に炉外に排ガス出口より飛散し、大型のもの
については不燃物排出装置２より、流動媒体と共に炉外
に排出される。流動媒体と不燃物は分級装置で分けられ
る。不燃物は系外に排出され、流動媒体は流動媒体エレ
ベータにより投入口迄持ち上げられ炉内に戻される。炉
床の流動状態を良好に保つため、流動媒体に対し、不燃
物の割合は３〜１０％程度に抑えることが好ましく、結
果として流動媒体循環量が多くなり、これからの熱損失
が問題であった。In a conventional fluidized bed type municipal waste incinerator containing incombustibles, after the municipal waste 21 is charged into the furnace, the process of drying → gasification → combustion is followed. In a fluidized bed furnace, the input waste is crushed by fluidized sand, dried,
It gasifies and then burns partially in the sand and in the combustion chamber. Then, the secondary air 24 is supplied to the upper combustion chamber. Regarding the incinerated ash, those having a small particle size are scattered out of the furnace together with the ash from the exhaust gas outlet, and those having a large particle size are discharged from the incombustibles discharging device 2 to the outside of the furnace together with the fluidized medium. The fluid medium and incombustibles are separated by a classifier. The incombustibles are discharged to the outside of the system, and the fluidized medium is lifted up to the inlet by the fluidized medium elevator and returned to the furnace. In order to keep the fluidized state of the hearth in a good state, it is preferable to keep the ratio of incombustibles to about 3 to 10% with respect to the fluidized medium, and as a result, the fluidized medium circulation amount increases and heat loss from this is a problem. It was
【０００４】また、流動層からの熱の回収技術としては
流動層の層内に伝熱管を挿入して熱を回収する方法があ
るが、層内で燃焼ガスに暴露されるため、酸性ガスによ
る腐食、摩耗が起きて伝熱管の寿命が比較的短く、また
伝熱管の交換に時間と多くの費用を要する。また、層内
に伝熱管を配することにより、廃棄物、都市ゴミ中に含
まれる不燃物が伝熱管に引っかかり等を生じ、流動層内
の移動に支障をきたすことが予想され、炉床中の不燃物
含有量を低くするため、流動媒体循環量が多くなり、こ
れからの熱損失は問題であった。As a technique for recovering heat from the fluidized bed, there is a method of recovering the heat by inserting a heat transfer tube into the bed of the fluidized bed. However, since the heat is exposed to the combustion gas in the bed, acid gas is used. Corrosion and wear occur, and the life of the heat transfer tube is relatively short, and replacement of the heat transfer tube requires a lot of time and money. Also, by arranging the heat transfer tubes in the bed, it is expected that waste materials and incombustible substances contained in municipal waste will be caught in the heat transfer tubes, which will hinder the movement in the fluidized bed. Since the content of non-combustible substances in (1) is reduced, the circulating amount of the fluidized medium is increased, and the heat loss from this is a problem.
【０００５】また、先に本発明者らは、分級装置と流動
媒体エレベータとの間に直列に熱交換器を置く方法を提
案（特願平３−３３４４９０号）したが、この方式にお
いても流動媒体循環量が多くなると熱交換器の必要伝熱
面積も増え、配置において熱交換器の設置面積が過大と
なり問題であった。また、熱交換器は定期的にメンテナ
ンスが必要となるが直列に接続されているため、熱交換
器のメンテナンス時及び故障時、流動床焼却プラント全
体の運転を中止しなければならない問題があった。ま
た、直列のため、流動媒体循環量と熱回収量は各々任意
に操作することは難しかった。The present inventors have previously proposed a method of placing a heat exchanger in series between a classifier and a fluid medium elevator (Japanese Patent Application No. 3-334490). When the medium circulation amount increases, the heat transfer area required for the heat exchanger also increases, and the installation area of the heat exchanger becomes excessively large in the layout, which is a problem. Further, the heat exchangers require periodic maintenance, but since they are connected in series, there was a problem that the operation of the entire fluidized bed incineration plant had to be stopped when the heat exchangers were maintained or failed. . Further, since they are in series, it was difficult to arbitrarily control the circulating amount of the fluidized medium and the heat recovery amount.
【０００６】[0006]
【発明が解決しようとする課題】そこで、本発明は、上
記のような問題点を解決し、炉床中の不燃物含有量及
び、炉床温度の制御と熱の回収を任意にでき、伝熱管の
トラブルや不燃物の排出トラブルがなく、プラント全体
の運転に影響を与えずかつ、プラントの配置に支障を与
えない設置面積で、簡易に効率よく熱回収が行える流動
媒体循環経路を有する流動床焼却装置を提供することを
課題とする。SUMMARY OF THE INVENTION Therefore, the present invention solves the above-mentioned problems, controls the content of incombustibles in the hearth, the hearth temperature, and the heat recovery as desired. There is no trouble of heat pipes or discharge of incombustibles, it does not affect the operation of the entire plant, and it does not hinder the layout of the plant. An object is to provide a floor incinerator.
【０００７】[0007]
【課題を解決するための手段】上記課題を解決するため
に、本発明では、下部に不燃物排出装置を有し、上部に
流動媒体投入口を有する流動床焼却炉と、前記不燃物排
出装置より排出される流動媒体と不燃物とを分ける分級
装置と、分けられた流動媒体を前記流動媒体投入口に持
ち上げる流動媒体循環エレベータとを有し、それらを流
動媒体循環経路で接続した流動床焼却装置において、前
記流動媒体循環経路に流動媒体エレベータと並列に流動
媒体を熱源とする熱交換器を設けたこととしたものであ
る。In order to solve the above-mentioned problems, according to the present invention, a fluidized bed incinerator having a non-combustible substance discharging device at a lower portion and a fluid medium charging port at an upper portion, and the non-combustible substance discharging device. A fluidized bed incinerator having a classifying device that separates the fluid medium and the incombustible substance that are more discharged, and a fluid medium circulation elevator that lifts the separated fluid medium to the fluid medium inlet, and connects them by a fluid medium circulation path. In the apparatus, a heat exchanger using a fluid medium as a heat source is provided in parallel with the fluid medium elevator in the fluid medium circulation path.
【０００８】前記装置において、熱交換器は、流動媒体
エレベータの高さを利用して流動媒体を落下させること
による受熱体の運動を利用して構成されており、前記流
動床焼却炉の後段に設けられたボイラの缶水を、該熱交
換器の受熱体として用いて、該缶水を前記熱交換器下部
より導入し、受熱後、熱交換器上部より抜き出して、ボ
イラ及びボイラ加熱器に戻す構成とするのがよい。ま
た、前記熱交換器の流動媒体出口は、分級装置から流動
媒体エレベータに通じる流動媒体循環経路に接続され、
熱交換後の流動媒体と焼却炉より排出された流動媒体と
を混合して、流動媒体の温度調節を行うことができる。
さらに、前記流動媒体循環経路には、流動床焼却炉への
流動媒体循環量と熱交換器への流動媒体量とを調節し
て、流動床焼却炉の炉床中の不燃物含有量及び、炉床温
度を制御する制御機構を設けることもできる。In the above apparatus, the heat exchanger is constructed by utilizing the motion of the heat receiving body by dropping the fluidized medium by utilizing the height of the fluidized medium elevator, and the heat exchanger is provided in the latter stage of the fluidized bed incinerator. The boiler can water provided is used as a heat receiving body of the heat exchanger, the can water is introduced from the lower part of the heat exchanger, and after receiving heat, it is withdrawn from the upper part of the heat exchanger to a boiler and a boiler heater. It is better to set it back. Further, the fluidized medium outlet of the heat exchanger is connected to a fluidized medium circulation path leading from the classifying device to the fluidized medium elevator,
The temperature of the fluidized medium can be adjusted by mixing the fluidized medium after heat exchange with the fluidized medium discharged from the incinerator.
Further, in the fluidized medium circulation path, the fluidized medium circulation amount to the fluidized bed incinerator and the fluidized medium amount to the heat exchanger are adjusted, and the incombustible content in the hearth of the fluidized bed incinerator, and A control mechanism for controlling the hearth temperature may be provided.
【０００９】[0009]
【作用】流動床焼却炉においては、下部の排出口から上
部の投入口まで高度差があるため、流動媒体エレベータ
は主にバケットエレベーターが使用される。本発明で
は、該流動媒体エレベータの頂部排出口より出た流動媒
体は設定した比率で分配され、一部は焼却炉に戻され、
残りは熱交換器に投入される。熱交換器は流動媒体エレ
ベータと並列に設置されているため、相当な高さを持つ
円柱形又は四角柱の形をなす。よって、熱交換器に投入
された流動媒体は熱交換器内を自由落下する。一方、熱
交換器内には熱交換チューブが底部より頂部に向けて設
置され、流動床焼却炉の後段に設置されたボイラの缶水
が前記熱交換チューブの底部注入口より注入される。缶
水は流動媒体より受熱し、熱水より蒸気になり、前記熱
交換チューブ内を上昇する。In a fluidized bed incinerator, a bucket elevator is mainly used as the fluidized medium elevator because there is a height difference from the lower outlet to the upper inlet. In the present invention, the fluidized medium coming out of the top outlet of the fluidized medium elevator is distributed at a set ratio, a part of which is returned to the incinerator,
The rest is put into the heat exchanger. Since the heat exchanger is installed in parallel with the fluidized medium elevator, it has the shape of a cylinder or a square pole having a considerable height. Therefore, the fluidized medium introduced into the heat exchanger falls freely in the heat exchanger. On the other hand, a heat exchange tube is installed in the heat exchanger from the bottom toward the top, and can water of a boiler installed in the latter stage of the fluidized bed incinerator is injected from the bottom injection port of the heat exchange tube. The can water receives heat from the fluid medium, becomes steam from hot water, and rises in the heat exchange tube.
【００１０】よって、流動媒体の下向きの落下運動と缶
水の蒸発する上昇力により効率よく熱交換される。ま
た、１０〜３０ｍの充分な高さが取れるため、充分な熱
交換時間を取ることができ、設置面積はかなり節減する
ことが出来る。受熱した缶水は前記ボイラに戻され、温
水として利用されるか、過熱器により過熱蒸気にされ、
発電に利用される。また、前記缶水により冷やされた流
動媒体は熱交換器底部より排出され、前記不燃物排出装
置より排出された５５０〜６５０℃の流動媒体と合流し
混合される。混合された流動媒体は４５０℃程度にな
り、前記流動媒体エレベータに投入される。流動媒体エ
レベータは１０〜３０ｍとかなり高さを有するため、流
動媒体が６００℃を越す高温になると熱膨張が大きくな
り、構造が複雑となるが４５０℃程度に抑えられるた
め、簡易な構造となり機器コストも節減できる。Therefore, heat is efficiently exchanged by the downward movement of the fluidized medium and the rising force of the evaporation of the can water. Also, since a sufficient height of 10 to 30 m can be obtained, a sufficient heat exchange time can be taken, and the installation area can be considerably reduced. The can water that has received heat is returned to the boiler and is used as hot water or is turned into superheated steam by a superheater,
Used for power generation. Further, the fluid medium cooled by the can water is discharged from the bottom of the heat exchanger, and is joined and mixed with the fluid medium at 550 to 650 ° C. discharged from the incombustible substance discharging device. The mixed fluid medium reaches about 450 ° C. and is put into the fluid medium elevator. Since the fluidized medium elevator has a considerably high height of 10 to 30 m, the thermal expansion of the fluidized medium becomes large when the fluidized medium reaches a high temperature of over 600 ° C, and the structure becomes complicated, but it can be suppressed to about 450 ° C, so that the structure becomes simple. Costs can also be saved.
【００１１】さらに、流動床焼却炉においては、炉床中
の不燃物含有量をコントロールするため、前記不燃物排
出装置により不燃物とともに流動媒体を抜き出すが、大
量に流動媒体を抜き出した場合においても、熱交換器に
流動媒体を分配する比率を増やすことより、熱回収量を
増やすことができ、流動媒体循環における熱損失を防ぐ
ことができると共に、流動媒体循環エレベータ投入口前
で、機器許容温度４５０℃程度に抑えることができる。
また、熱回収分だけ炉床温度を低下させることができる
ため、炉床の温度を制御することができる。また、熱交
換器は充分な高さを有するため、大量に流動媒体を抜き
出した場合でも設置面積を少なく抑えることが出来る。Further, in the fluidized bed incinerator, in order to control the content of incombustibles in the hearth, the incombustibles discharging device extracts the fluidized medium together with the incombustibles, but even when a large amount of the fluidized medium is extracted. By increasing the distribution ratio of the fluidized medium to the heat exchanger, the heat recovery amount can be increased, heat loss in the fluidized medium circulation can be prevented, and the allowable device temperature before the fluidized medium circulation elevator inlet It can be suppressed to about 450 ° C.
Further, since the hearth temperature can be lowered by the amount of heat recovered, the hearth temperature can be controlled. Further, since the heat exchanger has a sufficient height, the installation area can be reduced even when a large amount of fluid medium is extracted.
【００１２】このように、本発明では、熱交換器が流動
媒体循環ラインに直列ではなく、並列に設置されている
ため、熱交換器のメンテナンス時、故障時においても炉
床注水等を使用することにより熱効率は下がるものの、
プラント運転全体を停止する必要がなくなる。よって、
本発明は流動媒体循環量と熱交換器への流動媒体量を各
々操作することにより、任意に、熱損失なく、炉床中の
不燃物含有量及び、炉床温度の制御ができる。また、設
置面積が少なく運転に支障の無い効率の良い熱回収が出
来る。また、ごみ中の不燃物量や発熱量は常に変動する
が、充分に変動に対応できる流動床焼却炉となる。As described above, in the present invention, since the heat exchangers are installed in parallel in the fluid medium circulation line, not in series, hearth water injection or the like is used even during maintenance or failure of the heat exchangers. Although this reduces the thermal efficiency,
There is no need to stop the entire plant operation. Therefore,
In the present invention, by controlling the fluidized medium circulation amount and the fluidized medium amount to the heat exchanger, it is possible to arbitrarily control the incombustible content in the hearth and the hearth temperature without heat loss. In addition, the installation area is small and efficient heat recovery that does not hinder operation can be performed. In addition, although the amount of incombustibles and the amount of heat generated in the waste constantly fluctuate, the fluidized bed incinerator can sufficiently cope with such fluctuations.
【００１３】[0013]
【実施例】以下、本発明を図面を用いて具体的に説明す
るが、本発明はこれに限定されるものではない。
実施例１
図１に本発明の流動媒体循環経路を有する流動床焼却装
置の概略構成図を示す。図１において、１は流動層７を
有する流動床焼却炉であり、流動媒体エレベータ４と並
列に熱交換器５が置かれる。流動床焼却炉１の下部には
不燃物排出装置２が設けられ、該排出装置２から排出さ
れる流動媒体と不燃物は不燃物分級装置３で分級され、
不燃物は系外に除去される。分級された流動媒体は５５
０〜６５０℃の高温であるが、通路１３内で、熱交換器
５で冷やされた流動媒体と合流し、流動媒体エレベータ
４に許容温度内で投入される。DESCRIPTION OF THE PREFERRED EMBODIMENTS The present invention will be specifically described below with reference to the drawings, but the present invention is not limited thereto. Example 1 FIG. 1 shows a schematic configuration diagram of a fluidized bed incinerator having a fluidized medium circulation path of the present invention. In FIG. 1, 1 is a fluidized bed incinerator having a fluidized bed 7, in which a heat exchanger 5 is placed in parallel with a fluidized medium elevator 4. An incombustible material discharge device 2 is provided below the fluidized bed incinerator 1, and the fluid medium and incombustible material discharged from the discharge device 2 are classified by an incombustible material classifying device 3.
Incombustibles are removed outside the system. 55 fluid media classified
Although it is a high temperature of 0 to 650 ° C., it merges with the fluidized medium cooled in the heat exchanger 5 in the passage 13 and is fed into the fluidized medium elevator 4 within an allowable temperature.
【００１４】流動媒体エレベータ４は流動媒体を流動床
焼却炉１に循環するための高さまで持ち上げ、頂部９よ
り排出する。排出された流動媒体は分配器１０により一
部は流動床焼却炉１に戻され、残りは通路１１を通り、
熱交換器５の上部に投入される。投入された流動媒体は
熱交換器５内を落下する。一方、排熱ボイラ６の缶水の
一部は経路１４から熱交換器５内の熱交換チューブ１６
の底部に導入される。導入された缶水は熱交換器５内を
沈降する流動媒体より受熱し、缶水は熱水から蒸気に変
わり、熱交換チューブ内１６を上昇し、頂部より排熱ボ
イラ６の上部ヘッダに戻される。この流動床焼却炉流動
媒体循環経路では焼却物発熱量が高く、流動床焼却炉１
の炉床の温度が高すぎた場合は、分配器１０により、熱
交換器５内に投入する流動媒体量を増やすことにより、
熱交換量分炉床温度を下げることができる。The fluidized medium elevator 4 raises the fluidized medium to a height for circulating it in the fluidized bed incinerator 1 and discharges it from the top 9. A part of the discharged fluid medium is returned to the fluidized bed incinerator 1 by the distributor 10, and the rest passes through the passage 11,
It is put in the upper part of the heat exchanger 5. The introduced fluid medium falls in the heat exchanger 5. On the other hand, a part of the canned water of the exhaust heat boiler 6 flows from the path 14 to the heat exchange tube 16 in the heat exchanger 5.
Introduced at the bottom of the. The introduced can water receives heat from the fluidized medium that settles in the heat exchanger 5, the can water changes from hot water to steam, rises in the heat exchange tube 16, and returns from the top to the upper header of the waste heat boiler 6. Be done. The fluidized bed incinerator has a high calorific value of the incinerator in the fluidized medium circulation path, and thus the fluidized bed incinerator 1
When the temperature of the hearth is too high, the distributor 10 increases the amount of the fluidized medium charged into the heat exchanger 5,
The hearth temperature can be lowered by the amount of heat exchange.
【００１５】一方、焼却物不燃物量が多い場合、不燃物
排出装置２の排出量を増加させ、不燃物分級装置３で不
燃物の系外への排出を多くする。残りの流動媒体は流動
媒体循環エレベータ４により、分配器１０、焼却炉投入
口１９を通り、焼却炉に戻される。この際、大量の流動
媒体抜き出しにより、炉床温度が下がりすぎる場合、分
配器１０による熱交換器５への流動媒体投入量を減らす
ことで、炉床温度を制御することができる。熱交換器５
は流動床焼却炉１の外部でかつ、流動媒体エレベータと
並列に置かれているため、炉床内の腐食ガスや不燃物に
よるダメージがなくメンテナンスが容易であると共に該
メンテナンス時、及び故障時においてもプラント運転を
停止させる必要がない。また、熱交換器５は受熱体の流
動媒体の落下運転、受熱体のボイラ缶水の蒸発上昇力を
利用できるため伝熱効率が良く、かつ充分な高さを取れ
るため設置面積はかなり節減できる。On the other hand, when the amount of incombustibles incombustibles is large, the amount of incombustibles discharging device 2 is increased, and the incombustibles classifying device 3 increases the amount of incombustibles discharged to the outside of the system. The remaining fluidized medium is returned to the incinerator by the fluidized medium circulation elevator 4 through the distributor 10 and the incinerator inlet 19. At this time, if the hearth temperature falls too much due to extraction of a large amount of the fluid medium, the hearth temperature can be controlled by reducing the amount of the fluid medium charged into the heat exchanger 5 by the distributor 10. Heat exchanger 5
Is placed outside the fluidized bed incinerator 1 and in parallel with the fluidized medium elevator, so there is no damage due to corrosive gas or incombustibles in the hearth, and maintenance is easy, and at the time of maintenance and when there is a failure. Also, it is not necessary to stop the plant operation. In addition, the heat exchanger 5 has good heat transfer efficiency because it can use the drop operation of the fluidized medium of the heat receiver and the evaporation rising force of the boiler can water of the heat receiver, and can take a sufficient height to save the installation area considerably.
【００１６】[0016]
【発明の効果】本発明は流動媒体循環量と熱交換器への
流動媒体量を各々操作することにより、任意に、熱損失
無く、流動焼却炉の炉床中の不燃物含有量及び、炉床温
度の制御ができ、また設置面積が少なく運転に支障の無
い、効率の良い熱回収ができる。よって、ごみ中の不燃
物量や発熱量は常に変動するが、充分に変動に対応でき
る流動床焼却炉となる。INDUSTRIAL APPLICABILITY The present invention controls the circulating amount of the flowing medium and the amount of the flowing medium to the heat exchanger so that the content of the incombustibles in the hearth of the fluidized incinerator and the furnace can be arbitrarily adjusted without heat loss. The floor temperature can be controlled, and the installation area is small, which does not hinder the operation and enables efficient heat recovery. Therefore, the fluidized bed incinerator can sufficiently cope with fluctuations in the amount of incombustibles in the waste and the amount of heat generation, although the fluctuations are always changing.
【図１】本発明の流動媒体循環経路を有する流動床焼却
装置を示す概略構成図。FIG. 1 is a schematic configuration diagram showing a fluidized bed incinerator having a fluidized medium circulation path of the present invention.
【図２】公知の流動床焼却炉の概略図。FIG. 2 is a schematic diagram of a known fluidized bed incinerator.
１：流動床焼却炉、２：不燃物排出装置、３：不燃物分
級装置、４：流動媒体エレベータ、５：熱交換器、６：
排熱ボイラ、７：流動層、１０：分配器、１１〜１３、
１９：流動媒体通路1: Fluidized bed incinerator, 2: Incombustible substance discharging device, 3: Incombustible substance classifying device, 4: Fluidized medium elevator, 5: Heat exchanger, 6:
Exhaust heat boiler, 7: fluidized bed, 10: distributor, 11-13,
19: Fluid medium passage
───────────────────────────────────────────────────── フロントページの続き (56)参考文献 特開 昭60−101414（ＪＰ，Ａ) 特開 平３−279701（ＪＰ，Ａ) 特開 平５−141637（ＪＰ，Ａ) 特開 昭62−182513（ＪＰ，Ａ) 特開 平５−223232（ＪＰ，Ａ) 特開 昭59−197724（ＪＰ，Ａ) (58)調査した分野(Int.Cl.7，ＤＢ名) F23G 5/30 ZAB F23C 10/24 F23G 5/46 ZAB F23G 5/50 ZAB ─────────────────────────────────────────────────── --- Continuation of the front page (56) References JP-A-60-101414 (JP, A) JP-A-3-279701 (JP, A) JP-A-5-141637 (JP, A) JP-A-62-1 182513 (JP, A) JP 5-223232 (JP, A) JP 59-197724 (JP, A) (58) Fields investigated (Int.Cl. 7 , DB name) F23G 5/30 ZAB F23C 10/24 F23G 5/46 ZAB F23G 5/50 ZAB
Claims (5)
動媒体投入口を有する流動床焼却炉と、前記不燃物排出
装置より排出される流動媒体と不燃物とを分ける分級装
置と、分けられた流動媒体を前記流動媒体投入口に持ち
上げる流動媒体循環エレベータとを有し、それらを流動
媒体循環経路で接続した流動床焼却装置において、前記
流動媒体循環経路に流動媒体エレベータと並列に流動媒
体を熱源とする熱交換器を設けたことを特徴とする流動
床焼却装置。1. A fluidized bed incinerator having a non-combustible substance discharging device at a lower portion and a fluid medium charging port at an upper portion, and a classifying device for separating the fluid medium discharged from the non-combustible substance discharging device and the non-combustible substance, In a fluidized bed incinerator having a fluidized medium circulation elevator that lifts the divided fluidized medium to the fluidized medium input port, and in a fluidized bed incinerator in which they are connected by a fluidized medium circulation path, the fluidized medium circulation path flows in parallel with the fluidized medium elevator. A fluidized bed incinerator comprising a heat exchanger having a medium as a heat source.
高さを利用して流動媒体を落下させることによる受熱体
の運動を利用して構成された熱交換器であることを特徴
とする請求項１記載の流動床焼却装置。2. The heat exchanger is a heat exchanger configured by utilizing the motion of a heat receiving body caused by dropping the fluidized medium by utilizing the height of the fluidized medium elevator. Item 2. A fluidized bed incinerator according to item 1.
設け、該ボイラの缶水を前記熱交換器の受熱体として用
いて、該缶水を前記熱交換器下部より導入し受熱後、熱
交換器上部より抜き出して、ボイラ及びボイラ加熱器に
戻す構成としたことを特徴とする請求項１記載の流動床
焼却装置。3. The fluidized bed incinerator is provided with a boiler in a subsequent stage, and the boiler water of the boiler is used as a heat receiving body of the heat exchanger, and the boiler water is introduced from the lower portion of the heat exchanger to receive heat. The fluidized bed incinerator according to claim 1, wherein the fluidized bed incinerator is configured to be extracted from the upper portion of the heat exchanger and returned to the boiler and the boiler heater.
置から流動媒体エレベータに通じる流動媒体循環経路に
接続され、熱交換後の流動媒体と焼却炉より排出された
流動媒体とを混合することを特徴とする請求項１、２又
は３記載の流動床焼却装置。4. The fluidized medium outlet of the heat exchanger is connected to a fluidized medium circulation path leading from a classifier to a fluidized medium elevator to mix the fluidized medium after heat exchange with the fluidized medium discharged from the incinerator. The fluidized bed incinerator according to claim 1, 2 or 3, characterized in that.
炉への流動媒体循環量と熱交換器への流動媒体量とを調
節して、流動床焼却炉の炉床中の不燃物含有量及び、炉
床温度を制御する制御機構を有することを特徴とする請
求項１〜４のいずれか１項に記載の流動床焼却装置。5. The fluid medium circulation path is configured to control a fluid medium circulation amount to a fluidized bed incinerator and a fluid medium amount to a heat exchanger so as to contain an incombustible substance in a hearth of the fluidized bed incinerator. The fluidized bed incinerator according to any one of claims 1 to 4, further comprising a control mechanism for controlling the amount and the hearth temperature.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP16310795A JP3491783B2 (en) | 1995-06-07 | 1995-06-07 | Fluidized bed incinerator with fluidized media circulation path |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP16310795A JP3491783B2 (en) | 1995-06-07 | 1995-06-07 | Fluidized bed incinerator with fluidized media circulation path |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH08334219A JPH08334219A (en) | 1996-12-17 |
| JP3491783B2 true JP3491783B2 (en) | 2004-01-26 |
Family
ID=15767308
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP16310795A Expired - Fee Related JP3491783B2 (en) | 1995-06-07 | 1995-06-07 | Fluidized bed incinerator with fluidized media circulation path |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3491783B2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102901106B (en) * | 2012-09-29 | 2015-05-27 | 东南大学 | Flying ash processing device of fluidized bed incinerator |
| CN108800113A (en) * | 2017-05-03 | 2018-11-13 | 中国科学院过程工程研究所 | A method of for promoting biomass fuel to stablize burning in fluidized bed combustion |
-
1995
- 1995-06-07 JP JP16310795A patent/JP3491783B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH08334219A (en) | 1996-12-17 |
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