JP2001221405A - Circulating type fluidized bed combustion furnace - Google Patents
Circulating type fluidized bed combustion furnaceInfo
- Publication number
- JP2001221405A JP2001221405A JP2000030853A JP2000030853A JP2001221405A JP 2001221405 A JP2001221405 A JP 2001221405A JP 2000030853 A JP2000030853 A JP 2000030853A JP 2000030853 A JP2000030853 A JP 2000030853A JP 2001221405 A JP2001221405 A JP 2001221405A
- Authority
- JP
- Japan
- Prior art keywords
- space
- fluidized bed
- furnace
- partition wall
- circulating
- 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.)
- Withdrawn
Links
Landscapes
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、下水汚泥、都市ゴ
ミ、産業廃棄物、石炭等の固形炭素質系を焼却する流動
層焼却装置に係り、特に循環型流動層炉を具えた焼却装
置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a fluidized bed incinerator for incinerating solid carbonaceous materials such as sewage sludge, municipal waste, industrial waste and coal, and more particularly to an incinerator equipped with a circulating fluidized bed furnace. .
【０００２】[0002]
【従来の技術】従来より、産業廃棄物や都市ゴミ、下水
汚泥等の焼却処理には、流動床焼却炉が広く用いられて
おり、該流動層焼却炉は汚泥供給の瞬時の変動に安定
で、流動層中に直接補助燃料を供給することができ、ま
た流動層の熱吸収力が強いため一般燃焼装置のように火
炎による局部高温を発生しない等の利点により、特に、
含水率の高い汚泥の焼却に多用される傾向にある。2. Description of the Related Art Conventionally, fluidized bed incinerators have been widely used for incineration of industrial waste, municipal waste, sewage sludge, and the like. Fluidized bed incinerators are stable to instantaneous fluctuations in sludge supply. In particular, the auxiliary fuel can be supplied directly into the fluidized bed, and the fluidized bed has a strong heat absorbing power, so that it does not generate a local high temperature due to a flame unlike a general combustion device.
It tends to be frequently used for incinerating sludge with a high moisture content.
【０００３】前記流動層焼却炉には気泡流動層炉と循環
流動層炉とに分類され、前記気泡流動層炉は、炉床に砂
等の流動砂を敷き、１次空気の吹き込みにより砂を流動
化して層内を沸騰状態にさせ、該流動層中に汚泥等の廃
棄物を投入し燃焼させる装置である。[0003] The fluidized bed incinerators are classified into a bubble fluidized bed furnace and a circulating fluidized bed furnace. In the bubble bed fluidized bed furnace, fluidized sand such as sand is spread on a hearth and the sand is blown by primary air. This is a device that fluidizes and makes the inside of the bed a boiling state, and throws waste such as sludge into the fluidized bed and burns it.
【０００４】該気泡流動層炉による汚泥の燃焼過程を説
明するに、ある一定以上の速度の１次空気を吹き込み、
気泡の発生を伴いながら流動する気泡流動層内に投入さ
れた汚泥は、該気泡流動層内で高温の流動砂と激しく混
合流動化されて短時間で乾留ガス化するとともに、不揮
発性の固定炭素分は該流動層内で緩慢燃焼する。[0004] To explain the process of burning sludge by the bubble fluidized bed furnace, primary air is blown at a certain speed or higher.
The sludge introduced into the bubble fluidized bed which flows with the generation of bubbles is mixed and fluidized vigorously with the high-temperature fluidized sand in the bubble fluidized bed and gasified in a short period of time. The components burn slowly in the fluidized bed.
【０００５】前記汚泥中の揮発分や未燃ガス、軽い汚泥
粒子は気泡流動層上方のフリーボード部に導かれ、該フ
リーボードで燃焼する。[0005] Volatile components, unburned gas, and light sludge particles in the sludge are guided to a freeboard section above the bubble fluidized bed and burned by the freeboard.
【０００６】しかし、前記気泡流動層炉では、汚泥の燃
焼をフリーボードに頼っている部分が多く、フリーボー
ドの過熱を招く問題点がある。また、下水汚泥等のよう
に高含水廃棄物を焼却する場合には炉床面積を増大する
か、若しくは供給空気量を増やす等の対策をとる必要が
生じ、排ガス量が増大する問題がある。[0006] However, in the bubble fluidized bed furnace, there are many parts that rely on the freeboard for burning sludge, and there is a problem that the freeboard is overheated. Further, when incinerating high-water content waste such as sewage sludge, it is necessary to take measures such as increasing the hearth area or increasing the amount of supplied air, and there is a problem that the amount of exhaust gas increases.
【０００７】そこで、炉内温度差が小さく、かつ流動砂
を循環させることによる排ガス量の低減や設備のコンパ
クト化が可能である循環流動層炉が普及しつつある。Therefore, a circulating fluidized bed furnace, which has a small temperature difference in the furnace and is capable of reducing the amount of exhaust gas and making the equipment compact by circulating fluidized sand, is becoming widespread.
【０００８】前記循環流動層炉の構成は図３に示すよう
に、フリーボード５１と流動層５３とからなる流動層炉
本体５０と、該フリーボード５１に吹き上げられた流動
砂を出口通路５２を介して捕集するサイクロン５４と、
流動砂を返送するダウンカマー５６と、炉内未燃ガスの
サイクロン５４への吹き抜けを防止するシールポット５
５と戻し通路５７とから構成される。尚、（Ａ）は正面
断面図、（Ｂ）は平面図である。As shown in FIG. 3, the circulating fluidized bed furnace has a fluidized bed furnace main body 50 comprising a free board 51 and a fluidized bed 53, and a fluidized sand blown up by the free board 51 through an outlet passage 52. A cyclone 54 to collect through
Downcomer 56 for returning the fluidized sand, and seal pot 5 for preventing unburned gas in the furnace from flowing into cyclone 54
5 and a return passage 57. (A) is a front sectional view, and (B) is a plan view.
【０００９】かかる流動層において、１次空気投入口５
９から導入される１次空気により約７００〜８００℃に
加熱されて流動層５３を形成する流動砂中に汚泥投入口
６１から汚泥を供給すると、該汚泥は流動層５３内を混
合攪拌され、流動砂との接触により微細化されるととも
に、該流動砂と混合状態で流動しつつ乾燥、熱分解しな
がら燃焼する。In such a fluidized bed, the primary air inlet 5
When the sludge is supplied from the sludge inlet 61 into the fluidized sand which is heated to about 700 to 800 ° C. by the primary air introduced from 9 to form the fluidized bed 53, the sludge is mixed and stirred in the fluidized bed 53, It is made finer by contact with the liquid sand, and is dried and thermally decomposed and burned while flowing in a mixed state with the liquid sand.
【００１０】このとき、分散板６０から吹き込む１次空
気は、流動砂が前記流動砂濃厚層からガスとともに上方
に伴送される速度以上、すなわち終端速度以上に制御さ
れる必要がある。これは、１次空気を流動開始化速度程
度に維持する気泡流動層炉と異なり、流動砂を外部循環
させるために必須の条件となる。At this time, the primary air blown from the dispersion plate 60 needs to be controlled at a speed equal to or higher than the speed at which the fluidized sand is sent upward together with the gas from the fluidized sand thick layer, that is, at a speed equal to or higher than the terminal speed. This is an essential condition for externally circulating the fluidized sand, unlike a bubble fluidized bed furnace in which primary air is maintained at a flow initiation speed or so.
【００１１】前記流動層５３から吹き上げる流動砂は汚
泥中の未燃ガスや揮発分、軽いゴミは２次空気６ａとと
もにフリーボード５１へ導かれ、該フリーボード５１で
未燃分が燃焼した後、出口通路５２を介してサイクロン
５４で捕集され、ダウンカマー５６、シールポット５５
及び戻し通路５７を経て流動層炉本体５０に還流され
る。The fluidized sand blown up from the fluidized bed 53 is led to the freeboard 51 together with the unburned gas and volatiles in the sludge, and the light garbage together with the secondary air 6a. Collected by the cyclone 54 through the outlet passage 52, the downcomer 56, the seal pot 55
The fluid is returned to the fluidized bed furnace main body 50 through the return passage 57.
【００１２】前記循環流動層炉は、上述のように流動砂
を循環して用いるので、気泡流動層炉に比較して炉内温
度が安定であり、混合攪拌効果が大きいため完全燃焼を
促すことができる。Since the circulating fluidized bed furnace circulates and uses the fluidized sand as described above, the temperature inside the furnace is more stable than the bubble fluidized bed furnace, and the mixing and stirring effect is large. Can be.
【００１３】しかしながら、汚泥のように水分の多い比
燃焼物では、前記循環構造をとっても流動層５３内に助
燃用の燃焼ガスを必要とするのみならず、流動砂を外部
循環させるために、サイクロン５４及びシールポット５
５を流動層炉本体５０と別置して並設しなければなら
ず、装置大型化につながる。然もサイクロン５４及びシ
ールポット５５と、流動層炉本体５０との間には、両者
間を連絡する出口通路５２と戻し通路５７を設けなけれ
ばならず、結果として前記通路長だけ更に装置幅が大き
くなり、大型化が避けられないとともに、炉の表面積の
増大による温度低下が避けられない。However, in the case of a specific combustion product having a high moisture content such as sludge, even if the above-mentioned circulation structure is employed, not only the combustion gas for auxiliary combustion is required in the fluidized bed 53, but also the cyclone for external circulation of the fluidized sand is required. 54 and seal pot 5
5 must be provided separately and in parallel with the fluidized bed furnace main body 50, which leads to an increase in the size of the apparatus. Of course, between the cyclone 54 and the seal pot 55 and the fluidized-bed furnace main body 50, an outlet passage 52 and a return passage 57 communicating between them must be provided. As a result, the apparatus width is further increased by the passage length. It is inevitable that the temperature increases due to an increase in the surface area of the furnace.
【００１４】又図４に示すように、前記シールポット５
５内の高温の流動砂を熱回収装置６１側に取り出し、該
装置内の熱回収管６２で熱回収を行った後、第２戻し通
路６３を経て流動層炉本体５０に還流される構造のもの
も存在するが、かかる装置によれば熱回収装置６１内へ
の流動砂の抜き出し量を調整することにより、流動層
(濃厚層)５３の温度調節も出来好ましいが、一方ではシ
ールポット５５の更に下方に熱回収装置６１を設けなけ
ればならず、結果として流動層炉全体の層高が高くな
る。Further, as shown in FIG.
5 is taken out to the heat recovery device 61 side, heat is recovered by the heat recovery pipe 62 in the device, and then returned to the fluidized bed furnace main body 50 through the second return passage 63. However, according to such a device, the amount of fluidized sand withdrawn into the heat recovery device 61 is adjusted so that the fluidized bed is removed.
The temperature of the (dense layer) 53 can be adjusted, which is preferable. On the other hand, a heat recovery device 61 must be provided further below the seal pot 55, and as a result, the bed height of the entire fluidized bed furnace increases.
【００１５】一方前記角形の流動層炉本体５０と丸形の
サイクロン５４の組み合わせではなく、角形と角形の組
み合わせになるように構成した技術が特開平１０-８９
６４９に開示されている。On the other hand, Japanese Patent Application Laid-Open No. 10-89 discloses a technique in which the rectangular fluidized-bed furnace body 50 and the circular cyclone 54 are not combined with each other, but are combined with each other.
649.
【００１６】かかる技術は図５に示すように、シールポ
ット５５上方の流動層炉本体５０出口通路５２と接続さ
れる空間６５を方形状に形成するとともに、該空間６５
を垂直仕切壁６６を介して入口側流域６８ａ(下降流)と
ボイラー６７に連通する出口側流域６８ｂ(上昇流)に分
割し、その仕切壁６６底部の分割境界域６８をシールポ
ット５５の入口側に導かれるように斜めに形成し、該分
割境界域６８に粒子捕集スクリーンを配した技術が存在
する。According to this technique, as shown in FIG. 5, a space 65 connected to the outlet passage 52 of the fluidized bed furnace main body 50 above the seal pot 55 is formed in a rectangular shape.
Is divided into an inlet-side flow area 68a (downflow) and an outlet-side flow area 68b (upflow) communicating with the boiler 67 through a vertical partition wall 66, and the divided boundary area 68 at the bottom of the partition wall 66 is used as an inlet for the seal pot 55. There is a technique in which a particle collecting screen is formed obliquely so as to be guided to the side, and a particle collecting screen is arranged in the divided boundary area 68.
【００１７】そしてかかる技術はフリーボード５１を狭
幅化し、その分上方空間６５の拡幅化を可能にしている
が、両者間に出口通路５２と戻し通路５７を設けなけれ
ばならない点は前記従来技術と同様であり、且つ上方空
間６５の出口側に出口通路５２を介してボイラー６７を
連接せねばならず、結果として流動層炉本体５０、上方
空間、ボイラー６７の三連装構造となり、装置の大型化
とともに、炉の表面積の増大による温度低下が避けられ
ない。Although such a technique makes the free board 51 narrower and allows the upper space 65 to be widened by that amount, the point that an outlet passage 52 and a return passage 57 must be provided between the two is that the prior art. And the boiler 67 must be connected to the outlet side of the upper space 65 via the outlet passage 52. As a result, the fluidized bed furnace main body 50, the upper space, and the boiler 67 have a triple structure, and the size of the apparatus is large. With the increase in temperature, a decrease in temperature due to an increase in the surface area of the furnace is inevitable.
【００１８】本発明はかかる従来技術の欠点に鑑み、装
置全体の省スペース化と、流動砂の循環効率と温度効率
の向上、流動層炉の運転状態の安定化を図ることを目的
とする。The present invention has been made in view of the above-mentioned drawbacks of the prior art, and has as its object to save the space of the entire apparatus, improve the efficiency of circulating sand and temperature, and stabilize the operating state of a fluidized bed furnace.
【００１９】[0019]
【課題を解決するための手段】本発明はかかる課題を解
決するために、請求項１記載の発明は、流動砂と被燃焼
物を混合しながら燃焼する流動層炉本体と該本体より飛
び出した流動砂を流動層炉本体内に戻す粒子循環部とを
具えた循環型流動層燃焼炉において、底部に散気部を有
する炉内空間を、仕切壁を介して、散気部上及び炉頂部
とが連絡するように左右に分割し、一側を流動層炉本
体、他側を粒子循環部とする一体構造に構成したことを
特徴とする。SUMMARY OF THE INVENTION In order to solve the above-mentioned problems, the present invention is directed to a fluidized bed furnace body which burns while mixing fluidized sand and an object to be burned, and protrudes from the body. In a circulating fluidized bed combustion furnace having a particle circulating section for returning fluidized sand to the inside of a fluidized bed furnace main body, a furnace space having an air diffusing section on the bottom is separated from the air diffusing section on the air diffusing section and the furnace top via a partition wall. Are divided into right and left so as to communicate with each other, and are configured as an integrated structure having a fluidized bed furnace main body on one side and a particle circulation section on the other side.
【００２０】従って本発明によれば、流動流動層炉本体
と粒子循環部とが仕切壁を介して分割した一体構造とし
たために、言い換えれば、共通する仕切壁により、流動
層炉本体と粒子循環部とが隣接配置され、その間には分
離空間が存在しないために、炉の表面積の減少と装置の
小型化が達成出来、特に下水汚泥のように助燃を必要と
していた多含水廃棄物では助燃の量を減らすことが出来
る。Therefore, according to the present invention, since the fluidized bed furnace main body and the particle circulating section have an integrated structure divided through the partition wall, in other words, the fluidized bed furnace main body and the particle circulating section are formed by the common partition wall. Because there is no separation space between them, a reduction in the surface area of the furnace and a reduction in the size of the equipment can be achieved, especially in the case of multi-water-containing waste that required combustion, such as sewage sludge. The amount can be reduced.
【００２１】請求項２記載の発明は、前記仕切壁下部の
散気部上を、粒子循環部と流動層炉本体を連絡する開設
空間となすとともに、該開設空間を反重力方向に設定
し、該開設空間内の流動媒体を散気部より吹き上げる制
御空気により搬送させることを特徴とする。The invention according to claim 2 is to provide an opening space for connecting the particle circulating section and the fluidized bed furnace body on the air diffusion section below the partition wall, and to set the opening space in a direction opposite to gravity. It is characterized in that the fluid medium in the opening space is transported by control air blown up from the air diffuser.
【００２２】かかる発明によれば独立したシールポット
部を設けなくてもガスシールと流動媒体の搬送が可能と
なり、請求項３に記載のように、前記粒子循環部に位置
する散気部上方空間をシールポット入口側通路とし、前
記開設空間をシールポット出口側空間とし、夫々の空間
に供給する空気流の制御により流動媒体の搬送量を制御
することにより好ましいガスシールと流動媒体の搬送が
容易である。According to this invention, the gas seal and the transport of the fluid medium can be carried out without providing an independent seal pot, and the space above the air diffuser located in the particle circulation section as described in claim 3. Is used as a seal-pot inlet-side passage, and the opening space is used as a seal-pot outlet-side space. By controlling the flow rate of the flowing medium by controlling the air flow supplied to each space, it is easy to transfer the preferable gas seal and the flowing medium. It is.
【００２３】請求項４記載の発明は、前記仕切壁上に位
置する連絡通路と開口する粒子循環部上方空間を拡幅化
し、該拡幅化した空間上部に重力沈降式固気分離器を設
けた事を特徴とし、より具体的には請求項５に記載のよ
うに、前記粒子循環部上方空間を拡幅化し、該拡幅化し
た空間上部に外部に延設するほぼ水平な出口通路を設け
た事を特徴とする。According to a fourth aspect of the present invention, the space above the particle circulation portion, which opens to the communication passage located on the partition wall, is widened, and a gravity sedimentation type solid-gas separator is provided above the widened space. More specifically, as described in claim 5, the space above the particle circulation portion is widened, and a substantially horizontal outlet passage extending to the outside is provided above the widened space. Features.
【００２４】かかる発明によれば、排ガス分離を重力沈
降式とすることで、従来サイクロンを用いた場合に出来
る上部空間を省略できるために、炉高を低くできるとと
もに、連絡通路出口側の下向きの慣性流が生じた部分を
拡幅化した空間を有する重力沈降式固気分離器としたた
めに、一層効率の良い固気分離が可能である。According to this invention, since the exhaust gas separation is of the gravity sedimentation type, the upper space created by using the conventional cyclone can be omitted, so that the furnace height can be lowered and the exhaust gas is separated downward. Since the portion where the inertial flow has occurred is a gravity sedimentation type solid-gas separator having a widened space, more efficient solid-gas separation is possible.
【００２５】請求項６記載の発明は、仕切壁を介して隣
接する流動層炉本体と粒子循環部とが共通する散気部上
に位置させた事を特徴とする。The invention according to claim 6 is characterized in that the fluidized bed furnace main body and the particle circulation section which are adjacent to each other via the partition wall are located on a common air diffusion section.
【００２６】かかる発明によれば、シールポットと流動
濃厚層とが共通する散気部（散気板）上に位置し、言い
換えれば同一平面に配置する事が出来るので、粒子循環
部高さを十分に高くしても炉高を抑えることが出来る。According to this invention, the seal pot and the fluidized thick layer are located on the common air diffuser (diffuse plate), in other words, they can be arranged on the same plane. Even if it is sufficiently high, the furnace height can be suppressed.
【００２７】請求項７記載の発明は、散気部上に位置す
る前記粒子循環部下部空間に底部が開口する隔壁を設
け、該隔壁の仕切壁側空間をシールポット入口側空間、
炉壁側空間を熱回収管を有する熱回収空間とした事を特
徴とする。According to a seventh aspect of the present invention, a partition having an opening at the bottom is provided in the space below the particle circulating portion located above the air diffuser, and the partition side space of the partition is defined as a seal pot inlet side space,
The furnace wall side space is a heat recovery space having a heat recovery pipe.
【００２８】かかる発明においても粒子循環部のシール
ポット側面に熱回収部を設けることで、シールポットと
流動濃厚層とともに熱回収空間もほぼ同一平面に配置す
る事が出来るので、粒子循環部高さを十分に高くしても
炉高を抑えることが出来るとともに、炉の表面積の減少
と装置の小型化が達成出来、特に石炭のように熱回収を
行う燃焼では熱回収量を増やすことが出来る。In this invention as well, by providing the heat recovery section on the side of the seal pot of the particle circulation section, the heat recovery space can be arranged on substantially the same plane as the seal pot and the fluidized thick layer. Even if the temperature of the furnace is sufficiently increased, the furnace height can be reduced, the surface area of the furnace can be reduced, and the size of the apparatus can be reduced. In particular, the amount of heat recovery can be increased in combustion that recovers heat like coal.
【００２９】請求項８記載の発明は、前記隔壁が、該隔
壁底部と散気部間の開口空間を可変する隔壁である事を
特徴とする。The invention according to claim 8 is characterized in that the partition wall is a partition wall which changes an opening space between the bottom of the partition wall and the air diffuser.
【００３０】かかる発明によれば、前記開口空間を調節
するだけで、シールポットや流動層炉内の熱制御が容易
である。According to this invention, heat control in the seal pot or the fluidized-bed furnace is easy only by adjusting the opening space.
【００３１】請求項９記載の発明は、前記隔壁の上端を
粒子抜出量調節機構に取り付け、該調節機構を介して前
記隔壁上部より熱回収空間へ進入する流動媒体量を調節
可能に構成した事を特徴とする。かかる発明によれば、
前記熱回収空間へ進入する流動媒体量を任意に調節でき
で、熱回収量の制御とともに、シールポットや流動層炉
内へ供給する流動媒体の制御も容易である。According to the ninth aspect of the present invention, the upper end of the partition is attached to a particle extraction amount adjusting mechanism, and the amount of the fluid medium entering the heat recovery space from the upper portion of the partition via the adjusting mechanism can be adjusted. It is characterized by things. According to such invention,
The amount of the fluid medium entering the heat recovery space can be arbitrarily adjusted, and the control of the heat medium and the fluid medium supplied to the seal pot or the fluidized bed furnace can be easily performed.
【００３２】請求項１０記載の発明は、前記回収空間の
底部に位置する散気部が、前記シールポット入口空間へ
向けて下向きに傾斜させた散気部である事を特徴とす
る。[0032] The invention according to claim 10 is characterized in that the diffuser located at the bottom of the recovery space is a diffuser inclined downward toward the seal pot inlet space.
【００３３】かかる発明によれば、独立した戻し路を設
けずに傾斜させた散気部でこれを共通化でき、一層の小
型化と省設置化が達成できる。According to this invention, this can be shared by the inclined diffuser without providing an independent return path, and further downsizing and installation reduction can be achieved.
【００３４】請求項１１記載の発明は、前記仕切壁内に
熱回収管を埋設した事を特徴とする。An eleventh aspect of the present invention is characterized in that a heat recovery pipe is buried in the partition wall.
【００３５】かかる発明によれば仕切壁自体も熱回収機
能を持たせることが出来る。According to this invention, the partition wall itself can have a heat recovery function.
【００３６】請求項１２記載の発明は、前記仕切壁下部
を開設空間とした請求項２記載の循環型流動層燃焼炉に
おいて、シールポット入口空間と対面する仕切壁内に熱
回収管を埋設した事を特徴とする。According to a twelfth aspect of the present invention, in the circulating fluidized bed combustion furnace of the second aspect, a heat recovery pipe is buried in the partition wall facing the seal pot inlet space. It is characterized by things.
【００３７】[0037]
【発明の実施の形態】以下、本発明を図に示した実施形
態を用いて詳細に説明する。但し、この実施形態に記載
される構成部品の寸法、形状、その相対配置などは特に
特定的な記載がない限り、この発明の範囲をそれのみに
限定する趣旨ではなく単なる説明例に過ぎない。図１は
本発明の実施形態に係り、（Ａ）は正面断面図、（Ｂ）
はＢ−Ｂ線断面図、（Ｃ）は側面図であり、炉一体型で
仕切壁にて炉内を分割した内部循環構造の循環型流動層
燃焼装置を示し、図において、１は底部に散気部１１を
有する断面略横凸型の角形炉、より具体的には広幅方形
炉側面に厚幅の垂直仕切壁１２を散気部１１付近まで垂
設するとともに、前記厚幅の仕切壁１２上端と炉壁頂部
間は、開口されて固気分離器１４側への連絡通路１３と
なす。そして前記仕切壁１２右側は上方側より連絡通路
１３と対面する方形通路下側は、一側に拡幅化された偏
平角錐台状の重力沈降式固気分離器１４を取り付ける。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, the present invention will be described in detail with reference to an embodiment shown in the drawings. However, the dimensions, shapes, relative arrangements, and the like of the components described in this embodiment are not intended to limit the scope of the present invention but to merely illustrative examples unless otherwise specified. 1A and 1B relate to an embodiment of the present invention, in which FIG.
Is a cross-sectional view taken along the line BB, and (C) is a side view showing a circulating fluidized bed combustion apparatus having an internal circulation structure in which the furnace is integrated and the inside of the furnace is divided by a partition wall. A rectangular furnace having a substantially horizontal cross-sectional shape having an air diffuser 11, more specifically, a thick vertical partition 12 is vertically provided on the side of a wide rectangular furnace near the air diffuser 11. An opening is formed between the upper end of the furnace 12 and the top of the furnace wall to form a communication passage 13 to the solid-gas separator 14 side. On the right side of the partition wall 12, the lower side of the rectangular passage facing the communication passage 13 from the upper side is attached with a flattened truncated pyramidal gravity sedimentation type solid-gas separator 14 widened on one side.
【００３８】該固気分離器１４は拡幅側の上側開口より
円筒筒を水平方向に延設し、排ガス(飛灰を含む)排出通
路１５として構成するとともに、前記固気分離器１４の
下側を徐々に挟小化させて、ダウンカマー状の通路１６
となす。そして前記通路１６は垂直仕切壁１２に沿って
そのまま垂直下方に延設し、底部に散気板１１ｂと制御
空気８の導入部１７を設け、シールポット５の入口空間
５ａを形成する。又該散気部１１付近の下部仕切壁１２
は鍵型(Ｌ字型)状に開設され、前記シールポット５の出
口側空間５ｂとなすとともに、該空間５ｂの出口開口５
ｃは、汚泥投入口９より下方の濃厚層位置に開口させ
る。The solid-gas separator 14 has a cylindrical cylinder extending horizontally from the upper opening on the widening side to constitute an exhaust gas (including fly ash) discharge passage 15. Is gradually narrowed, and the downcomer-like passage 16 is formed.
And The passage 16 extends vertically downward along the vertical partition wall 12 as it is, and a diffusion plate 11b and an inlet 17 for the control air 8 are provided at the bottom to form an inlet space 5a for the seal pot 5. The lower partition wall 12 near the air diffuser 11
Is formed in the shape of a key (L-shape) and forms an outlet side space 5b of the seal pot 5, and an outlet opening 5 of the space 5b.
“c” is opened at a dense layer position below the sludge inlet 9.
【００３９】又垂直仕切壁１２右側の散気板１１ｂ上に
位置する一次空気導入空間(シールポット入口空間５ａ)
と下部仕切壁１２の鍵型開設空間(シールポット出口空
間５ｂ)に対応する散気板下方空間は隔壁１８で夫々分
割し、前記入口側空間５ａと出口側空間５ｂに夫々制御
空気８を導入可能に構成することによりシールポット５
が形成されることとなる。又、垂直仕切壁１２左側に位
置する炉内空間は、散気板１１ａが底部に有し、その上
方に流動濃厚層７、該流動濃厚層７上部位置の炉壁に汚
泥投入口９、その上方に二次空気導入口５を夫々設ける
とともに、その上方空間をフリーボード４となす循環型
流動層炉本体１０を形成する。The primary air introduction space (seal pot entrance space 5a) located on the air diffusion plate 11b on the right side of the vertical partition 12
And the lower space of the diffusing plate corresponding to the key-shaped opening space (seal pot outlet space 5b) of the lower partition wall 12 is divided by a partition wall 18, and control air 8 is introduced into the inlet space 5a and the outlet space 5b, respectively. By making it possible, the seal pot 5
Is formed. In the furnace space located on the left side of the vertical partition wall 12, a diffuser plate 11a is provided at a bottom portion, and a fluid thick layer 7 is provided above the diffuser plate 11a. A circulating fluidized bed furnace main body 10 is provided above each of which the secondary air inlets 5 are provided, and the upper space of which is the free board 4.
【００４０】かかる構成による焼却炉においては、次の
ような作用をなす。垂直仕切壁１２左側に位置する循環
型流動層炉本体１０をなす炉内空間では、１次空気投入
口３を介して散気板１１ａから導入される１次空気６に
より約７００〜８００℃に加熱されて流動濃厚層７を形
成する。そして該流動濃厚層７中に汚泥投入口９から汚
泥を供給すると、該汚泥は流動濃厚層７内を混合攪拌さ
れ、流動砂との接触により微細化されるとともに、該流
動砂と混合状態で流動しつつ乾燥、熱分解しながら燃焼
する。In the incinerator having such a configuration, the following operation is performed. In the furnace space that forms the circulating fluidized bed furnace main body 10 located on the left side of the vertical partition wall 12, the primary air 6 introduced from the diffuser plate 11 a through the primary air inlet 3 reaches about 700 to 800 ° C. It is heated to form a fluidized thick layer 7. When sludge is supplied from the sludge inlet 9 into the fluidized thick layer 7, the sludge is mixed and stirred in the fluidized thickened layer 7, and is made finer by contact with the fluidized sand. Dry while flowing, burn while pyrolyzing.
【００４１】前記流動濃厚層７から吹き上げる流動砂と
汚泥中の未燃ガスや揮発分、軽いゴミは２次空気ととも
にフリーボード４へ導かれ、該フリーボード４で未燃分
が燃焼した後、逆Ｕ字状の連絡通路１３を介し重力沈降
式固気分離器１４に導かれる。The unburned gas, volatile matter and light dust in the sludge and the sludge blown up from the thick layer 7 are guided to the free board 4 together with the secondary air. It is guided to a gravity sedimentation type solid-gas separator 14 through an inverted U-shaped communication passage 13.
【００４２】重力沈降式固気分離器１４内では、前記逆
Ｕ字状の連絡通路１３で下向きな慣性流１３ａが生じて
いるために、空気に比較して比重の大きい流動砂はダウ
ンカマー状の通路１６を介して、シールポット入口空間
５ａに送られる。シールポット入口空間５ａでは、散気
板１１ｂ下方より供給される制御空気８により必要な量
の流動砂が出口空間５ａを介して流動濃厚層７に戻され
る。一方流動砂より比重の軽い空気や飛灰は、下向きな
慣性流が反転して水平方向の出口空間５２により後工程
の熱交換器を介してバグフィルタ等(いずれも不図示)に
導かれる。In the gravity sedimentation type solid-gas separator 14, since the downward inertial flow 13a is generated in the inverted U-shaped communication passage 13, the flowing sand having a higher specific gravity than air is downcomer-shaped. Is sent to the seal pot entrance space 5a through the passage 16 of the above. In the seal pot inlet space 5a, a necessary amount of fluidized sand is returned to the flowing thick layer 7 through the outlet space 5a by the control air 8 supplied from below the diffuser plate 11b. On the other hand, air and fly ash having a specific gravity lower than that of the fluidized sand reverses the downward inertial flow and is guided to a bag filter or the like (both not shown) via a heat exchanger in a later process by a horizontal outlet space 52.
【００４３】従って本実施形態においては、流動砂と被
燃焼物を混合しながら燃焼する流動層炉本体１０と該本
体１０より飛び出した流動砂を流動層炉本体１０内に戻
す粒子循環部２０とが仕切壁１２を介して分割した一体
構造としたために、言い換えれば、共通する仕切壁１２
により、流動層炉本体１０と粒子循環部２０とが隣接配
置され、その間には分離空間が存在しないために、炉の
表面積の減少と装置の小型化が達成出来、特に下水汚泥
のように助燃を必要としていた多含水廃棄物では助燃の
量を減らすことが出来る。又排ガス分離を重力沈降式と
することで、従来サイクロン５４を用いた場合に出来る
上部空間を省略できるために、炉高を低くできる。Therefore, in the present embodiment, the fluidized bed furnace main body 10 that burns while mixing the fluidized sand and the material to be burned, and the particle circulating section 20 that returns the fluidized sand ejected from the body 10 to the fluidized bed furnace main body 10 Has an integral structure divided through the partition wall 12, in other words, the common partition wall 12
As a result, the fluidized bed furnace main body 10 and the particle circulating section 20 are arranged adjacent to each other, and there is no separation space between them, so that the furnace surface area can be reduced and the apparatus can be downsized. The amount of auxiliary combustion can be reduced in the case of multi-water waste, which required water. Further, by using the gravity sedimentation method for the exhaust gas separation, the upper space which can be formed when the conventional cyclone 54 is used can be omitted, so that the furnace height can be reduced.
【００４４】更に、シールポット５と濃厚層７とが共通
する散気部１１（散気板１１ａ、１１ｂ）上に位置し、
言い換えれば同一平面に配置する事が出来るので、粒子
循環部２０高さを十分に高くしても炉高を抑えることが
出来る。Further, the seal pot 5 and the thick layer 7 are located on the common air diffuser 11 (air diffusers 11a and 11b).
In other words, since they can be arranged on the same plane, the furnace height can be suppressed even if the height of the particle circulation section 20 is sufficiently increased.
【００４５】図２は熱回収機構を付設した本発明の他の
実施形態で、（Ａ）は正面断面図、（Ｂ）はＢ−Ｂ線
図、（Ｃ）は側面図であり、被燃焼物に石炭を用い熱回
収を行うようにした概略図である。図１との違いを説明
するに、前記厚肉の仕切壁１２及びその下側のシールポ
ット５５側の薄肉の仕切壁１２内にはボイラ水若しくは
水蒸気が循環して熱回収を図るボイラ管若しくはスーパ
ヒート管等の熱回収管２１が埋設されている。FIG. 2 shows another embodiment of the present invention provided with a heat recovery mechanism. FIG. 2 (A) is a front sectional view, FIG. 2 (B) is a BB diagram, and FIG. FIG. 4 is a schematic diagram in which coal is used for heat recovery. The difference from FIG. 1 will be described. A boiler tube or a boiler tube in which boiler water or steam circulates and heat is recovered in the thick partition wall 12 and the thin partition wall 12 on the seal pot 55 side below the thick partition wall 12 or A heat recovery pipe 21 such as a superheat pipe is embedded.
【００４６】又重力沈降式固気分離器１４下方に垂設さ
れるダウンカマー状の通路１６に仕切壁１２と平行に隔
壁２２を垂設し、該隔壁２２の下端をシールポット５の
入口空間５ａ内に埋没させる為、又該埋没深さが可変に
なるように、隔壁２２を上下に昇降自在に構成してもよ
いが、本実施形態では固定する。そして前記隔壁２２の
上端に粒子抜出量調節機構２３を取り付け、該調節機構
２３を介して前記隔壁２２の熱回収空間２４側の上部空
間の開放量を調節し、熱回収空間２４側への流動媒体の
進入量の調整を図る。Further, a partition wall 22 is provided in parallel with the partition wall 12 in a downcomer-like passage 16 which is provided below the gravity sedimentation type solid-gas separator 14, and the lower end of the partition wall 22 is formed in the entrance space of the seal pot 5. The partition 22 may be configured to be vertically movable so as to be buried in the inside 5a and to have a variable buried depth, but is fixed in this embodiment. A particle extraction amount adjusting mechanism 23 is attached to the upper end of the partition wall 22, and the opening amount of the upper space of the partition wall 22 on the side of the heat recovery space 24 is adjusted via the adjusting mechanism 23, so that the amount of the particle to the heat recovery space 24 is adjusted. Adjust the amount of fluid medium entering.
【００４７】さらに、隔壁２２を挟んでシールポット入
口側空間５ａのと反対側に位置する空間は熱回収空間２
４となし、該回収空間２４内に熱回収管２５を収納させ
る。又前記熱回収空間２４の底部に位置する散気板１１
ｃは斜め上方に立ち上げ、隔壁２２の反対側のシールポ
ット５の入口空間５ａへ向け、流動砂が流下するように
構成する。Further, the space located on the opposite side of the seal pot entrance side space 5a across the partition wall 22 is the heat recovery space 2
The heat recovery pipe 25 is housed in the recovery space 24. The diffuser plate 11 located at the bottom of the heat recovery space 24
c rises obliquely upward, and the flowing sand flows down toward the entrance space 5a of the seal pot 5 on the opposite side of the partition wall 22.
【００４８】かかる装置によれば、斜め散気板１１ｃよ
り空気を導入することで、前記シールポット５の入口空
間５ａ内の高温の流動砂を熱回収空間２４側に移送させ
ることが出来、該空間２４内の熱回収管２５で熱回収を
行った後、空気の循環に伴流されて熱回収後の流動砂が
シールポット入口空間５ａ側に還流する。そして前記斜
め散気板１１ｃよりの導入空気により流動砂がシールポ
ット入口空間５ａ側への還流に作用させるとともに、粒
子抜出量調節機構２３の開度を調整することで、熱回収
空間２４側に移送(下降進入)させる流動砂量を調節出来
る。即ち前記粒子抜出量調節機構２３の開度を上げるこ
とにすれば、熱回収空間２４内への流動砂の移送量を多
くすることが出来る。According to such an apparatus, by introducing air from the oblique diffuser plate 11c, high-temperature fluidized sand in the inlet space 5a of the seal pot 5 can be transferred to the heat recovery space 24 side. After the heat recovery is performed by the heat recovery pipe 25 in the space 24, the flowing sand after the heat recovery is returned to the seal pot inlet space 5a side with the circulation of the air. The flowing air from the oblique diffuser plate 11c causes the fluidized sand to return to the seal pot inlet space 5a side, and the opening degree of the particle extraction amount adjusting mechanism 23 is adjusted, so that the heat recovery space 24 side The amount of fluidized sand to be transported (downwardly entering) can be adjusted. That is, if the degree of opening of the particle extraction amount adjusting mechanism 23 is increased, the transfer amount of the fluidized sand into the heat recovery space 24 can be increased.
【００４９】従って本実施形態においても炉の表面積の
減少と装置の小型化が達成出来、特に炭のように熱回収
を行う燃焼では熱回収量を増やすことが出来るととも
に、熱制御を隔壁２２により仕切られた熱回収空間２４
で実施するために、シールポット５と流動濃厚層７とと
もに熱回収空間２４もほぼ同一平面に配置する事が出来
るので、粒子循環部２０高さを十分に高くしても炉高を
抑えることが出来る。Therefore, also in this embodiment, a reduction in the surface area of the furnace and a reduction in the size of the apparatus can be achieved. In particular, in the combustion in which heat recovery is performed like charcoal, the amount of heat recovery can be increased. Separated heat recovery space 24
Since the heat recovery space 24 can be arranged substantially on the same plane as the seal pot 5 and the fluidized thick layer 7, the furnace height can be suppressed even if the height of the particle circulation section 20 is sufficiently increased. I can do it.
【００５０】[0050]
【発明の効果】以上記載のごとく請求項１記載の発明に
よれば、流動層炉本体と粒子循環部との間には分離空間
が存在しないために、炉の表面積の減少と装置の小型化
が達成出来、特に下水汚泥のように助燃を必要としてい
た多含水廃棄物では助燃の量を減らすことが出来る。As described above, according to the first aspect of the present invention, since there is no separation space between the fluidized bed furnace main body and the particle circulation section, the surface area of the furnace is reduced and the size of the apparatus is reduced. The amount of auxiliary combustion can be reduced especially in a multi-water waste which requires auxiliary combustion such as sewage sludge.
【００５１】請求項２及び３記載の発明によれば、独立
したシールポット部を設けなくてもガスシールと流動媒
体の搬送が可能となる。According to the second and third aspects of the present invention, the gas seal and the fluid medium can be transported without providing an independent seal pot.
【００５２】請求項４及び５記載の発明によれば、排ガ
ス分離を重力沈降式とすることで、炉高を低くできる。According to the fourth and fifth aspects of the present invention, the furnace height can be reduced by using a gravity sedimentation method for separating the exhaust gas.
【００５３】請求項６記載の発明によれば、シールポッ
トと流動濃厚層とが同一平面に配置する事が出来るの
で、粒子循環部高さを十分に高くしても炉高を抑えるこ
とが出来る。According to the sixth aspect of the present invention, since the seal pot and the fluid thick layer can be arranged on the same plane, the furnace height can be suppressed even if the height of the particle circulation portion is sufficiently increased. .
【００５４】請求項７記載の発明においても粒子循環部
のシールポット側面に熱回収部を設けることで、粒子循
環部高さを十分に高くしても炉高を抑えることが出来る
とともに、炉の表面積の減少と装置の小型化が達成出来
る。Also in the invention according to claim 7, by providing a heat recovery section on the side of the seal pot of the particle circulating section, the furnace height can be suppressed even if the height of the particle circulating section is sufficiently increased, and the furnace can be cooled. A reduction in surface area and miniaturization of the device can be achieved.
【００５５】請求項８及び９記載の発明によれば、前記
開口空間を調節するだけで、熱回収空間とともに、シー
ルポットや流動層炉内の熱制御が容易である。According to the eighth and ninth aspects of the present invention, heat control in the seal pot and the fluidized bed furnace together with the heat recovery space can be easily performed only by adjusting the opening space.
【００５６】請求項１０記載の発明によれば、独立した
戻し路を設けずに傾斜させた散気部でこれを共通化で
き、一層の小型化と省設置化が達成できる。According to the tenth aspect of the present invention, this can be shared by the inclined diffuser without providing an independent return path, and further downsizing and installation reduction can be achieved.
【００５７】請求項１１記載の発明によれば仕切壁自体
も熱回収機能を持たせることが出来る。According to the eleventh aspect, the partition wall itself can also have a heat recovery function.
【００５８】請求項１２記載の発明によれば、濃厚層側
の薄肉の仕切壁に熱回収管が埋設されていないために、
濃厚層の温度低下を招かない。According to the twelfth aspect of the present invention, since the heat recovery pipe is not embedded in the thin partition wall on the dense layer side,
Does not cause the temperature drop of the dense layer.
【図１】 炉一体型で仕切壁にて炉内を分割した内部循
環構造の循環型流動層燃焼装置を示す本発明の基本構成
図である。FIG. 1 is a basic configuration diagram of the present invention showing a circulating fluidized bed combustion apparatus having an internal circulation structure in which a furnace is integrated and the inside of a furnace is divided by a partition wall.
【図２】 図１の基本構成図に熱回収機構を付設した本
発明の他の実施形態を示す概略図である。FIG. 2 is a schematic diagram showing another embodiment of the present invention in which a heat recovery mechanism is added to the basic configuration diagram of FIG.
【図３】 従来の循環型流動層燃焼装置を示す基本構成
図である。FIG. 3 is a basic configuration diagram showing a conventional circulating fluidized bed combustion apparatus.
【図４】 図３の基本構成図に熱回収機構を付設した従
来概略図である。FIG. 4 is a conventional schematic diagram in which a heat recovery mechanism is added to the basic configuration diagram of FIG.
【図５】 従来の内部循環型流動層燃焼装置を示す構成
図である。FIG. 5 is a configuration diagram showing a conventional internal circulation type fluidized bed combustion device.
４ フリーボード ５ シールポット ５ａ シールポット入口空間 ５ｂ シールポット出口側空間 ７ 流動濃厚層 ８ 制御空気 ９ 汚泥投入口 １０ 循環型流動層炉本体 １１ 散気部 １１ａ 散気板 １１ｂ 散気板 １１ｃ 散気板 １２ 仕切壁 １３ 連絡通路 １４ 重力沈降式固気分離器 １５ 排出通路 １７ 制御空気の導入部 ２０ 粒子循環部 ２１ 熱回収管 ２２ 隔壁 ２３ 粒子抜出量調節機構 ２４ 熱回収空間 Reference Signs List 4 Free board 5 Seal pot 5a Seal pot inlet space 5b Seal pot outlet side space 7 Fluid thick layer 8 Control air 9 Sludge inlet 10 Circulating fluidized bed furnace main body 11 Air diffuser 11a Air diffuser plate 11b Air diffuser plate 11c Air diffuser Plate 12 Partition wall 13 Communication passage 14 Gravity sedimentation type solid-gas separator 15 Discharge passage 17 Control air introduction part 20 Particle circulation part 21 Heat recovery pipe 22 Partition wall 23 Particle extraction amount adjustment mechanism 24 Heat recovery space
フロントページの続き (72)発明者 伊部 治重 横浜市中区錦町12番地 三菱重工業株式会 社横浜製作所内 (72)発明者 逸見 眞知 横浜市中区錦町12番地 三菱重工業株式会 社横浜製作所内 Ｆターム(参考） 3K064 AA10 AA20 AB01 AB03 AD05 AD08 AE16 BA03 BA05 BA13 BA14 BA18 Continued on the front page. (72) Inventor Harigeshi Ibe 12 Nishikicho, Naka-ku, Yokohama-shi Inside Mitsubishi Heavy Industries, Ltd.Yokohama Mfg. Co., Ltd. Terms (reference) 3K064 AA10 AA20 AB01 AB03 AD05 AD08 AE16 BA03 BA05 BA13 BA14 BA18
Claims (12)
る流動層炉本体と該本体より飛び出した流動砂を流動層
炉本体内に戻す粒子循環部とを具えた循環型流動層燃焼
炉において、 底部に散気部を有する炉内空間を、仕切壁を介して、散
気部上及び炉頂部とが連絡するように左右に分割し、一
側を流動層炉本体、他側を粒子循環部とする一体構造に
構成したことを特徴とする循環型流動層燃焼炉。A circulating fluidized bed combustion furnace comprising: a fluidized bed furnace main body for burning while mixing fluidized sand and an object to be burned; and a particle circulating section for returning fluidized sand ejected from the main body into the fluidized bed furnace main body. In the furnace space having a diffuser section at the bottom is divided into left and right through a partition wall so that the diffuser section and the furnace top communicate with each other, one side is a fluidized bed furnace body, and the other side is particles. A circulating fluidized-bed combustion furnace, wherein the circulating section has an integral structure.
部と流動層炉本体を連絡する開設空間となすとともに、
該開設空間を反重力方向に設定し、該開設空間内の流動
媒体を散気部より吹き上げる制御空気により搬送させる
ことを特徴とする請求項１記載の循環型流動層燃焼炉。2. An opening space that connects the particle circulation unit and the fluidized bed furnace body on the air diffusion unit below the partition wall,
2. The circulating fluidized bed combustion furnace according to claim 1, wherein the opening space is set in a direction opposite to gravity, and the fluid medium in the opening space is conveyed by control air blown up from a diffuser.
間をシールポット入口側通路とし、前記開設空間をシー
ルポット出口側空間とし、夫々の空間に供給する空気流
の制御により流動媒体の搬送量を制御することを特徴と
する請求項２記載の循環型流動層燃焼炉。3. A space above the air diffuser located in the particle circulation section is defined as a seal-pot inlet-side passage, and the opening space is defined as a seal-pot outlet-side space. The flow of the fluid medium is controlled by controlling the air flow supplied to each space. 3. The circulating fluidized bed combustion furnace according to claim 2, wherein the transport amount is controlled.
する粒子循環部上方空間を拡幅化し、該拡幅化した空間
上部に重力沈降式固気分離器を設けた事を特徴とする請
求項１記載の循環型流動層燃焼炉。4. The apparatus according to claim 1, wherein a space above the particle circulation portion, which is open to the communication passage located on the partition wall, and the particle circulation section are widened, and a gravity sedimentation type solid-gas separator is provided above the widened space. 2. The circulating fluidized bed combustion furnace according to 1.
拡幅化した空間上部に外部に延設するほぼ水平な出口通
路を設けた事を特徴とする請求項１記載の循環型流動層
燃焼炉。5. The circulating fluidized-bed combustion according to claim 1, wherein the space above the particle circulation portion is widened, and a substantially horizontal outlet passage extending outside is provided above the widened space. Furnace.
粒子循環部とが共通する散気部上に位置させた事を特徴
とする請求項１記載の循環型流動層燃焼炉。6. The circulating fluidized-bed combustion furnace according to claim 1, wherein the fluidized-bed furnace main body and the particle circulating portion adjacent to each other via a partition wall are located on a common diffuser portion.
空間に底部が開口する隔壁を設け、該隔壁の仕切壁側空
間をシールポット入口側空間、炉壁側空間を熱回収管を
有する熱回収空間とした事を特徴とする請求項１記載の
循環型流動層燃焼炉。7. A partition having an opening at the bottom in the lower space of the particle circulation section located above the air diffuser, a partition wall side space of the partition wall being a seal pot inlet side space, and a furnace wall side space being a heat recovery pipe. The circulating fluidized-bed combustion furnace according to claim 1, wherein the heat recovery space has a heat recovery space.
口空間を可変可能に構成した事を特徴とする請求項７記
載の循環型流動層燃焼炉。8. The circulating fluidized bed combustion furnace according to claim 7, wherein said partition wall is configured to be able to change an opening space between a bottom portion of said partition wall and an air diffuser.
取り付け、該調節機構を介して前記隔壁上部より熱回収
空間へ進入する流動媒体量を調節可能に構成した事を特
徴とする請求項７記載の循環型流動層燃焼炉。9. The apparatus according to claim 1, wherein an upper end of the partition is attached to a particle extraction amount adjusting mechanism, and an amount of a fluid medium entering the heat recovery space from an upper portion of the partition through the adjusting mechanism is adjustable. Item 7. A circulating fluidized bed combustion furnace according to Item 7.
が、前記シールポット入口空間へ向けて下向きに傾斜さ
せた散気部である事を特徴とする請求項７記載の循環型
流動層燃焼炉。10. The circulating fluidized bed according to claim 7, wherein the diffuser located at the bottom of the recovery space is a diffuser inclined downward toward the seal pot inlet space. Combustion furnace.
を特徴とする請求項１記載の循環型流動層燃焼炉11. The circulating fluidized bed combustion furnace according to claim 1, wherein a heat recovery pipe is buried in the partition wall.
項２記載の循環型流動層燃焼炉において、シールポット
入口空間と対面する仕切壁内に熱回収管を埋設した事を
特徴とする請求項１１記載の循環型流動層燃焼炉12. The circulating fluidized bed combustion furnace according to claim 2, wherein a heat recovery pipe is buried in the partition wall facing the seal pot inlet space, wherein the lower part of the partition wall is an open space. Item 13. A circulating fluidized bed combustion furnace according to Item 11.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000030853A JP2001221405A (en) | 2000-02-08 | 2000-02-08 | Circulating type fluidized bed combustion furnace |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000030853A JP2001221405A (en) | 2000-02-08 | 2000-02-08 | Circulating type fluidized bed combustion furnace |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JP2001221405A true JP2001221405A (en) | 2001-08-17 |
Family
ID=18555811
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2000030853A Withdrawn JP2001221405A (en) | 2000-02-08 | 2000-02-08 | Circulating type fluidized bed combustion furnace |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2001221405A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102078782A (en) * | 2010-12-21 | 2011-06-01 | 哈尔滨工程大学 | Method and device for improving internal particle circulation in lift pipe through return air at tower top |
| JP2014510248A (en) * | 2011-01-24 | 2014-04-24 | エンデヴ オサケユキチュア | Method for improving the operation of a circulating mass reactor and a circulating mass reactor |
| CN105090941A (en) * | 2015-08-14 | 2015-11-25 | 广州迪森热能设备有限公司 | Low-nitrogen fluidized bed combustor for biomass |
| CN108640090A (en) * | 2018-08-03 | 2018-10-12 | 山东大学 | A kind of carbon thermal reduction SO2Prepare the device and method of sulphur |
-
2000
- 2000-02-08 JP JP2000030853A patent/JP2001221405A/en not_active Withdrawn
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102078782A (en) * | 2010-12-21 | 2011-06-01 | 哈尔滨工程大学 | Method and device for improving internal particle circulation in lift pipe through return air at tower top |
| CN102078782B (en) * | 2010-12-21 | 2013-02-06 | 哈尔滨工程大学 | Method and device for improving internal particle circulation in lift pipe through return air at tower top |
| JP2014510248A (en) * | 2011-01-24 | 2014-04-24 | エンデヴ オサケユキチュア | Method for improving the operation of a circulating mass reactor and a circulating mass reactor |
| US9470416B2 (en) | 2011-01-24 | 2016-10-18 | Endev Oy | Method to enhance operation of circulating mass reactor and method to carry out such reactor |
| CN105090941A (en) * | 2015-08-14 | 2015-11-25 | 广州迪森热能设备有限公司 | Low-nitrogen fluidized bed combustor for biomass |
| CN108640090A (en) * | 2018-08-03 | 2018-10-12 | 山东大学 | A kind of carbon thermal reduction SO2Prepare the device and method of sulphur |
| CN108640090B (en) * | 2018-08-03 | 2023-07-04 | 山东大学 | Carbothermic reduction of SO 2 Device and method for preparing sulfur |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| TW419574B (en) | Operating method of flow-level incinerator and the incinerator | |
| US6709636B1 (en) | Method and apparatus for gasifying fluidized bed | |
| KR950007013B1 (en) | Internal circulation type fluidized bed boiler & method of controlling same | |
| JP2001221405A (en) | Circulating type fluidized bed combustion furnace | |
| CN1206469C (en) | Fluidized bed boiler with multifunctional cyclone separator | |
| JP2005274015A (en) | Circulation fluidized bed boiler device and its operation control method | |
| CN103104912A (en) | Circulating fluidized bed boiler for coal water slurry combustion | |
| JP3770653B2 (en) | Gasification combustion method using fluidized bed furnace | |
| JP2002098308A (en) | Circulated fluidized bed combustion apparatus | |
| JP2007163132A (en) | Method and apparatus for gasifying fluidized bed | |
| CN202973068U (en) | Fired water-coal-slurry circulating fluidized bed boiler | |
| JP2005300077A (en) | Circulating fluidized bed furnace | |
| JPH0227290Y2 (en) | ||
| RU2162566C1 (en) | Solid fuel combustion plant | |
| JPH11325424A (en) | Waste-gasifying furnace and apparatus for gasifying, burning, and treating waste provided with the same | |
| JPS62196522A (en) | Heat recovery method from fluidized bed and its equipment | |
| JP2991638B2 (en) | Waste incineration equipment | |
| JP2009085572A (en) | Combustion boiler for combustible material containing powder and particulate | |
| JPS6141817A (en) | Fluidized bed incinerating device | |
| JP2005121342A (en) | Operation method of circulating fluidized bed furnace | |
| AU692286B2 (en) | Fluidized-bed combustor | |
| JP2002098313A (en) | Circulating fluidized bed combustion apparatus | |
| JPH07243632A (en) | Method and apparatus for burning for fluidized bed accompanied by partial combustion | |
| JP2775588B2 (en) | Fluidized bed combustion method and apparatus with partial combustion | |
| JPH0798101A (en) | Fluidized bed boiler |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A300 | Withdrawal of application because of no request for examination |
Free format text: JAPANESE INTERMEDIATE CODE: A300 Effective date: 20070501 |