JP3095499B2 - Fluidized bed combustion boiler - Google Patents
Fluidized bed combustion boilerInfo
- Publication number
- JP3095499B2 JP3095499B2 JP03345821A JP34582191A JP3095499B2 JP 3095499 B2 JP3095499 B2 JP 3095499B2 JP 03345821 A JP03345821 A JP 03345821A JP 34582191 A JP34582191 A JP 34582191A JP 3095499 B2 JP3095499 B2 JP 3095499B2
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- JP
- Japan
- Prior art keywords
- combustion
- fluidized bed
- zone
- furnace
- heat transfer
- 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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- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Description
【０００１】[0001]
【産業上の利用分野】本発明は原動機製品の流動層方式
の流動層燃焼ボイラに関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a fluidized bed combustion boiler for a motor product in a fluidized bed system.
【０００２】[0002]
【従来の技術】気泡型流動層燃焼では、従来、空気の多
段投入によりＮＯｘ発生の抑制は可能であったが、脱硫
は層内で行なわれるため、ＮＯｘ，ＳＯｘ両者を抑制す
る事が困難であった。また、流動層温度の制御機構もな
く、燃料、ボイラ負荷等の変化に対応する事も困難であ
った。2. Description of the Related Art In bubble-type fluidized bed combustion, it has been conventionally possible to suppress the generation of NOx by multi-stage injection of air. However, since desulfurization is performed in the bed, it is difficult to suppress both NOx and SOx. there were. Also, there is no control mechanism for the fluidized bed temperature, and it is difficult to cope with changes in fuel, boiler load, and the like.
【０００３】図２に従来の流動層ボイラの一実施例を示
す。同図に示すように、火炉１１下部には１次空気１２
が投入され、流動層１３が形成される。燃料としての石
炭１４は流動層１３内に投入され、脱硫剤（石灰石等）
１５とともに層内で燃焼、脱硫反応が進行する。FIG. 2 shows an embodiment of a conventional fluidized bed boiler. As shown in FIG.
And the fluidized bed 13 is formed. Coal 14 as fuel is injected into the fluidized bed 13 and a desulfurizing agent (limestone, etc.)
Combustion and desulfurization reactions proceed in the bed together with 15.
【０００４】火炉１１の中間点より２次空気１６を投入
するが、ＮＯｘ抑制のためこの量を増加させると流動層
内の空気比が低下し脱硫反応が起きにくくなるという欠
点がある。火炉１１を出た燃焼ガスは、火炉上部伝熱面
１７、対流伝熱面１８で冷却され、集塵装置を経て大気
へ放出される。一方、ガス中から分離された未燃分は、
未燃灰リサイクル１９を経て流動層内へ投入される。
尚、流動層１３の内部には、層温度を制御するために層
内管２０が設置されている。[0004] The secondary air 16 is supplied from the intermediate point of the furnace 11, but if this amount is increased to suppress NOx, there is a disadvantage that the air ratio in the fluidized bed is reduced and desulfurization reaction is less likely to occur. The combustion gas that has exited the furnace 11 is cooled by the furnace upper heat transfer surface 17 and the convection heat transfer surface 18 and is discharged to the atmosphere via a dust collector. On the other hand, the unburned matter separated from the gas is
The unburned ash is fed into the fluidized bed through the recycle 19.
In addition, inside the fluidized bed 13, an inner tube 20 is installed to control the bed temperature.
【０００５】[0005]
【発明が解決しようとする課題】ところで、気泡型流動
層燃焼方式においては、二段燃焼はＮＯｘ低減手段とし
て従来から採用されているが、二段燃焼を行なうと、流
動層内の空気比が低下し、酸化雰囲気下での反応である
石灰石による脱硫反応が防げられるという問題がある。
また、流動層燃焼は、一般に８００〜９００℃の低温燃
焼であるため、Ｎ2Ｏの発生量が多く、ダイオキシンの
分解にも充分な温度となっていないという不具合があ
る。By the way, in the bubble type fluidized bed combustion system, the two-stage combustion has been conventionally employed as the NOx reduction means. However, when the two-stage combustion is performed, the air ratio in the fluidized bed is reduced. Therefore, there is a problem that the desulfurization reaction by limestone, which is a reaction under an oxidizing atmosphere, can be prevented.
Further, since fluidized bed combustion is generally low-temperature combustion at 800 to 900 ° C., there is a problem that a large amount of N 2 O is generated and the temperature is not sufficient for decomposition of dioxin.
【０００６】本発明は上記問題に鑑み、ＮＯｘ，ＳＯｘ
の発生を抑制しつつ流動層温度の制御を可能とした流動
層燃焼ボイラを提供することを目的とする。The present invention has been made in view of the above problems, and has been developed for NOx, SOx
It is an object of the present invention to provide a fluidized-bed combustion boiler capable of controlling the temperature of a fluidized bed while suppressing generation of the fluidized bed.
【０００７】[0007]
【課題を解決するための手段】前記目的を達成する本発
明に係る流動層燃焼ボイラの構成は、石油，油，ガス，
各種廃棄物等を燃料とし、石灰石等を脱硫剤として使用
する流動層燃焼方式のボイラであって、火炉下部に気泡
型流動層となる濃厚層を有し、該濃厚層の空気比を理論
燃焼空気量の０．５〜０．８の還元雰囲気を形成したガ
ス化１次燃焼域と、上記層上に２次空気投入口を設け、
２次空気投入後の空気比を理論燃焼空気量の０．８〜
１．０としてＮＯｘ分解領域を形成した２次脱硝燃焼域
と、該２次脱硝燃焼域の上部に３次空気投入口を設け、
未燃ガス燃焼による雰囲気温度の上昇によるＮ2Ｏ，ダ
イオキシン分解領域を形成した３次高温完全燃焼域と、
火炉出口部に伝熱管のガス流速が下部燃焼炉の空塔速度
よりも早くなる伝熱管群を設置し、伝熱管群出口の空塔
速度を下部燃焼炉の空塔速度よりも遅くして伝熱管群上
部に粒子の滞留する領域を形成すると共に、伝熱面積を
適宜選定して雰囲気ガス温度８００℃〜９００℃の脱硫
反応域を形成した脱硫域とを具備してなることを特徴と
する。A fluidized bed combustion boiler according to the present invention, which achieves the above object, comprises oil, oil, gas,
A fluidized bed combustion type boiler that uses various wastes as fuel and limestone etc. as a desulfurizing agent. A gasification primary combustion zone in which a reducing atmosphere having an air amount of 0.5 to 0.8 is formed, and a secondary air inlet provided on the layer,
The air ratio after secondary air injection is 0.8 to the theoretical combustion air amount.
A secondary denitration combustion zone in which a NOx decomposition zone is formed as 1.0, and a tertiary air inlet above the secondary denitration combustion zone;
A tertiary high-temperature complete combustion region in which an N 2 O and dioxin decomposition region is formed due to an increase in ambient temperature due to unburned gas combustion;
Install a heat transfer tube group at the furnace exit where the gas flow velocity of the heat transfer tubes is faster than the superficial velocity of the lower combustion furnace. A desulfurization zone is provided, in which a region where particles stay is formed at the top of the heat tube group, and a desulfurization zone in which a heat transfer area is appropriately selected to form a desulfurization reaction zone at an ambient gas temperature of 800 ° C to 900 ° C. .
【０００８】[0008]
【作用】前記構成において、気泡流動層域では、理論燃
焼用空気の0.５〜0.８倍の１次空気を投入し、還元雰囲
気でガス化燃焼を行なう。流動層上方に導かれた未燃ガ
スは、層上に投入された２次空気で一部燃焼し、空気比
０．８〜１．０の高温還元雰囲気を形成し、ＮＯｘの還
元分解反応が進行する。２次空気投入後の残留未燃ガス
は、３次空気投入により燃焼し、高温酸化雰囲気を形成
し、Ｎ2Ｏ、ダイオキシンの分解を促進する。炉出口の
燃焼ガスは酸素を含んではいるが高温状態であり、脱硫
反応に適した温度まで冷却する必要が有る。炉出口に設
置した冷却面は、このガスを冷却する目的と、燃焼炉と
脱硫部とを分割する役割を持っている。炉下部より上昇
してきた石灰石を含む微粒子は、炉出口冷却面を通過し
て炉上部の脱硫域に達する。冷却面内のガス速度は、炉
下部より早くなる様寸法が決められており、冷却面出口
のガス速度は炉下部より遅くなる様寸法が決められてい
るため、炉を上昇してきた粒子の一部は冷却面上部で落
下、上昇をくり返す。そして、炉上部に石灰石を含む濃
厚な微粒子の群が形成され、この部分の温度雰囲気を８
００〜８５０℃に維持する事により、脱硫反応を促進す
る事が出来る。In the above structure, in the bubble fluidized bed region, primary air 0.5 to 0.8 times the theoretical combustion air is supplied, and gasification combustion is performed in a reducing atmosphere. The unburned gas introduced above the fluidized bed is partially burned by the secondary air charged on the bed to form a high-temperature reducing atmosphere having an air ratio of 0.8 to 1.0, and the NOx reduction decomposition reaction is performed. proceed. The residual unburned gas after charging the secondary air is burned by the charging of the tertiary air to form a high-temperature oxidizing atmosphere, thereby promoting the decomposition of N 2 O and dioxin. The combustion gas at the furnace outlet contains oxygen but is in a high temperature state, and needs to be cooled to a temperature suitable for the desulfurization reaction. The cooling surface installed at the furnace outlet has the purpose of cooling this gas and the role of dividing the combustion furnace from the desulfurization section. The fine particles containing limestone that have risen from the lower part of the furnace pass through the furnace outlet cooling surface and reach the desulfurization zone at the upper part of the furnace. The gas velocity in the cooling surface is dimensioned to be faster than the lower part of the furnace, and the gas velocity at the cooling surface outlet is dimensioned to be lower than that in the lower part of the furnace. The part falls and rises repeatedly at the upper part of the cooling surface. Then, a group of dense particles including limestone is formed in the upper part of the furnace, and the temperature atmosphere in this part is reduced to 8%.
By maintaining the temperature at 00 to 850 ° C., the desulfurization reaction can be promoted.
【０００９】[0009]
【実施例】以下、本発明に係る流動層ボイラの好適な一
実施例を図面を参照して説明する。図１は本実施例に係
る流動層ボイラの概念図を示す。同図に示すように、気
泡型流動層となる濃厚層を有する火炉２１内には、火炉
下部から火炉上部へ向ってガス化１次燃焼域２２、２次
脱硝燃焼域２３、３次高温完全燃焼域２４及び火炉上部
出口に脱硫域２５を各々機能別に形成してなり、例えば
石炭，油，ガス，各種廃棄物等を燃料２６とし石灰石等
を脱硫剤２７として使用することで気泡型流動層燃焼を
行っている。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS A preferred embodiment of a fluidized bed boiler according to the present invention will be described below with reference to the drawings. FIG. 1 is a conceptual diagram of a fluidized-bed boiler according to the present embodiment. As shown in the figure, in a furnace 21 having a dense layer that becomes a bubble-type fluidized bed, a gasification primary combustion zone 22, a secondary denitration combustion zone 23, and a tertiary high-temperature complete zone are provided from the furnace lower part toward the furnace upper part. A desulfurization zone 25 is formed for each function at the combustion zone 24 and the furnace upper exit. For example, coal, oil, gas, various wastes, etc. are used as a fuel 26 and limestone is used as a desulfurization agent 27. Burning.
【００１０】ガス化１次燃焼域２２は、濃厚層としての
気泡型の流動層２８が形成され、投入された燃料例えば
石炭２６はここで導入される１次空気２９によって燃焼
される。ここで、導入する１次空気２９の量は濃厚層の
空気比を理論燃焼空気量の０．５〜０．８としており、
還元雰囲気を形成し、上記石炭２６は還元燃焼となる。
低ＮＯｘ燃焼を行なうには、この空気比の範囲が望まし
い。In the gasification primary combustion zone 22, a bubble type fluidized bed 28 is formed as a dense layer, and the injected fuel, for example, coal 26 is burned by the primary air 29 introduced here. Here, the amount of the primary air 29 to be introduced is such that the air ratio of the rich layer is 0.5 to 0.8 of the theoretical combustion air amount,
A reducing atmosphere is formed, and the coal 26 undergoes reduction combustion.
This range of air ratio is desirable for performing low NOx combustion.
【００１１】２次脱硝燃焼域２３は、上記流動層２８の
上方から導入する２次空気投入口を設け、投入後の空気
比が理論燃焼空気量の０．８〜１．０となる２次空気３
０を投入し、流動層２８から上昇する未燃ガスの一部を
燃焼し、３次空気投入までの間に脱硝反応に最適な雰囲
気を形成している。The secondary denitrification combustion zone 23 is provided with a secondary air inlet for introducing the fluid from above the fluidized bed 28, and the secondary air ratio after the injection becomes 0.8 to 1.0 of the theoretical combustion air amount. Air 3
0 is injected, a part of the unburned gas rising from the fluidized bed 28 is burned, and an optimum atmosphere for the denitration reaction is formed before the tertiary air is injected.
【００１２】３次高温完全燃焼域２４は３次空気投入口
を設け、未燃ガス燃焼による雰囲気温度の上昇によるＮ
2Ｏ、ダイオキシンを、３次空気３１の導入により火炉
上部伝熱面３２までの間で高温の酸化雰囲気を形成し、
完全燃焼させている。The tertiary high-temperature complete combustion zone 24 is provided with a tertiary air inlet, and N 3 is generated by an increase in ambient temperature due to unburned gas combustion.
2 O and dioxin form a high-temperature oxidizing atmosphere up to the furnace upper heat transfer surface 32 by introducing tertiary air 31;
Completely burned.
【００１３】脱硫域２５は火炉出口部近傍に設けられた
伝熱管群よりなる火炉上部伝熱面３２を有し、伝熱管の
ガス流速が下部燃焼炉の空塔速度よりも早くすると共
に、伝熱管出口の空塔速度を下部燃焼炉の空塔速度より
も遅くすることで伝熱管群上部に粒子の滞留する領域を
形成している。すなわち、炉を上昇してきた粒子の一部
は冷却面上部で落下，上昇をくり返すこととなる。そし
て、伝熱面積を適宜選定することで脱硫反応に最適な雰
囲気ガス温度８００〜９００℃の脱硫反応域をサイクロ
ン３３までの間に形成することとなる。The desulfurization zone 25 has a furnace upper heat transfer surface 32 composed of a group of heat transfer tubes provided in the vicinity of the furnace outlet. The gas flow rate of the heat transfer tubes is higher than the superficial velocity of the lower combustion furnace, and the heat transfer is performed. By making the superficial velocity at the heat tube outlet lower than the superficial superficial velocity of the lower combustion furnace, an area where particles stay in the upper part of the heat transfer tube group is formed. In other words, some of the particles that have risen in the furnace repeatedly fall and rise above the cooling surface. By appropriately selecting the heat transfer area, a desulfurization reaction zone having an atmosphere gas temperature of 800 to 900 ° C. optimal for the desulfurization reaction is formed up to the cyclone 33.
【００１４】よって流動層２８から飛散した脱硫剤２７
は火炉２１、火炉上部伝熱面３２を通過し火炉出口の脱
硫域２５で減速され、濃度の高い脱硫雰囲気が形成さ
れ、ＳＯｘが脱硫剤に吸着される。The desulfurizing agent 27 scattered from the fluidized bed 28
Passes through the furnace 21 and the furnace upper heat transfer surface 32 and is decelerated in the desulfurization zone 25 at the furnace outlet to form a highly-desulfurized atmosphere, and SOx is adsorbed by the desulfurizing agent.
【００１５】火炉出口の脱硫域２５から飛散した粒子は
下端に循環粒子ホッパ３４を備えたサイクロン３３で捕
集され、当該循環粒子ホッパ３４で貯えられ、次いで当
該循環粒子ホッパ３４出口に設けられた循環粒子調整バ
ルブ３５により循環流動層を制御し、流動層式熱交換器
流動用ガス３６を導入する流動層式熱交換器３７に導か
れる。The particles scattered from the desulfurization zone 25 at the furnace outlet are collected by a cyclone 33 having a circulating particle hopper 34 at the lower end, stored in the circulating particle hopper 34, and then provided at the circulating particle hopper 34 outlet. The circulating fluidized bed is controlled by a circulating particle regulating valve 35 and guided to a fluidized bed heat exchanger 37 for introducing a fluidized bed heat exchanger flowing gas 36.
【００１６】流動層式熱交換器３７の中には、層内管３
８が設置されており、循環灰を冷却後前記流動層２８に
戻すことにより、燃焼温度の制御が可能となる。The fluidized bed heat exchanger 37 contains an inner tube 3
8 is installed, and after the circulating ash is cooled and returned to the fluidized bed 28, the combustion temperature can be controlled.
【００１７】また、粒子が分離されたガスは、その後サ
イクロン３３の出口から対流伝熱面３９を経て冷却後、
集塵器、煙突へと導かれている。The gas from which the particles have been separated is cooled after passing through the convection heat transfer surface 39 from the outlet of the cyclone 33.
It is led to a dust collector and a chimney.
【００１８】[0018]
【発明の効果】以上、実施例と共に説明したように、本
発明に係る流動層燃焼ボイラは、燃料の燃焼過程をガス
化１次燃焼域、２次脱硝燃焼域、３次高温完全燃焼域及
び脱硫域というプロセスに分け、それぞれ最適な条件を
実現し、ＮＯｘ，ＳＯｘの発生を抑制しつつ流動層温度
の制御を可能とするという効果を奏する。As described above, in the fluidized bed combustion boiler according to the present invention, the combustion process of the fuel is performed in a gasification primary combustion zone, a secondary denitrification combustion zone, a tertiary high temperature complete combustion zone, The process is divided into desulfurization zones, and the optimum conditions are realized, and the effect of controlling the temperature of the fluidized bed while suppressing the generation of NOx and SOx is achieved.
【図１】本実施例に係る流動層燃焼ボイラの概念図であ
る。FIG. 1 is a conceptual diagram of a fluidized bed combustion boiler according to the present embodiment.
【図２】従来技術に係る流動層燃焼ボイラの概念図であ
る。FIG. 2 is a conceptual diagram of a fluidized bed combustion boiler according to the related art.
２１ 火炉 ２２ ガス化１次燃焼域 ２３ ２次脱硝燃焼域 ２４ ３次高温完全燃焼域 ２５ 脱硫域 ２６ 燃料 ２７ 脱硫剤 ２８ 流動層 ２９ １次空気 ３０ ２次空気 ３１ ３次空気 ３２ 火炉上部伝熱面 ３３ サイクロン ３４ 循環粒子ホッパ ３５ 循環粒子調整バルブ ３６ 流動層式熱交換器流動層用ガス ３７ 流動層式熱交換器 ３８ 層内管 ３９ 対流伝熱面 DESCRIPTION OF SYMBOLS 21 Furnace 22 Gasification primary combustion zone 23 Secondary denitrification combustion zone 24 Tertiary high-temperature complete combustion zone 25 Desulfurization zone 26 Fuel 27 Desulfurizer 28 Fluidized bed 29 Primary air 30 Secondary air 31 Tertiary air 32 Heat transfer at upper part of furnace Surface 33 Cyclone 34 Circulating particle hopper 35 Circulating particle regulating valve 36 Fluidized bed heat exchanger Gas for fluidized bed 37 Fluidized bed heat exchanger 38 Inner tube 39 Convection heat transfer surface
───────────────────────────────────────────────────── フロントページの続き (72)発明者 藤間 幸久 長崎県長崎市深堀町五丁目717番１号 三菱重工業株式会社 長崎研究所内 (72)発明者 田頭 健二 長崎県長崎市深堀町五丁目717番１号 三菱重工業株式会社 長崎研究所内 (56)参考文献 特開 昭64−79503（ＪＰ，Ａ) 特開 平２−247407（ＪＰ，Ａ) 実開 昭58−66210（ＪＰ，Ｕ) (58)調査した分野(Int.Cl.7，ＤＢ名) F23C 10/00 - 10/32 F22B 1/02 F23G 5/30 ──────────────────────────────────────────────────の Continuing on the front page (72) Inventor Yukihisa Fujima 5-717-1, Fukahori-cho, Nagasaki-city, Nagasaki Prefecture Mitsubishi Heavy Industries, Ltd. Nagasaki Research Laboratory (72) Inventor Kenji Tagami 5-717, Fukahori-cho, Nagasaki-city, Nagasaki Prefecture 1 Nagasaki Research Laboratory, Mitsubishi Heavy Industries, Ltd. (56) References JP-A-64-79503 (JP, A) JP-A-2-247407 (JP, A) JP-A-58-66210 (JP, U) (58) Field surveyed (Int.Cl. 7 , DB name) F23C 10/00-10/32 F22B 1/02 F23G 5/30
Claims (3)
し、石灰石等を脱硫剤として使用する流動層燃焼方式の
ボイラであって、 火炉下部に気泡型流動層となる濃厚層を有し、該濃厚層
の空気比を理論燃焼空気量の０. ５〜０. ８の還元雰囲
気を形成したガス化１次燃焼域と、 上記層上に２次空気投入口を設け、２次空気投入後の空
気比を理論燃焼空気量の０. ８〜１. ０としてＮＯｘ分
解領域を形成した２次脱硝燃焼域と、 該２次脱硝燃焼域の上部に３次空気投入口を設け、未燃
ガス燃焼による雰囲気温度の上昇によるＮ2Ｏ，ダイオ
キシン分解領域を形成した３次高温完全燃焼域と、 火炉出口部に伝熱管のガス流速が下部燃焼炉の空塔速度
よりも早くなる伝熱管群を設置し、伝熱管群出口の空塔
速度を下部燃焼炉の空塔速度よりも遅くして伝熱管群上
部に粒子の滞留する領域を形成すると共に、伝熱面積を
適宜選定して雰囲気ガス温度８００℃〜９００℃の脱硫
反応域を形成した脱硫域とを具備してなることを特徴と
する流動層燃焼ボイラ。1. A fluidized bed combustion type boiler using petroleum, oil, gas, various wastes, etc. as fuel and limestone etc. as a desulfurizing agent. And a gasification primary combustion zone in which a reducing atmosphere having a theoretical combustion air volume of 0.5 to 0.8 is formed, and a secondary air inlet is provided on the layer, and the secondary air A secondary denitrification combustion zone in which the NOx decomposition zone is formed by setting the air ratio after the injection to 0.8 to 1.0 of the theoretical combustion air amount, and a tertiary air inlet is provided above the secondary denitration combustion zone. A tertiary high-temperature complete combustion zone in which an N 2 O and dioxin decomposition zone is formed due to an increase in ambient temperature due to combustion of gas, and a heat transfer tube in which the gas flow velocity of the heat transfer tube at the furnace outlet is higher than the superficial velocity of the lower combustion furnace Install a group and set the superficial velocity at the outlet of the heat transfer tube group lower than the superficial velocity of the lower combustion furnace. Forming a region where particles stay in the upper part of the heat transfer tube group, and a desulfurization region in which a heat transfer area is appropriately selected to form a desulfurization reaction region at an ambient gas temperature of 800 ° C to 900 ° C. Fluidized bed combustion boiler.
て、 脱硫域出口部に脱硫反応域から飛散した脱硫剤及び未燃
分を捕集するサイクロンと、該サイクロン下部にこれら
の粒子を貯えるホッパと、該ホッパ出口に粒子の循環量
を制御する循環粒子調整バルブとを設けてなることを特
徴とする流動層燃焼ボイラ。2. A fluidized bed combustion boiler according to claim 1, wherein a cyclone for collecting desulfurizing agent and unburned matter scattered from a desulfurization reaction zone at a desulfurization zone outlet, and a hopper for storing these particles under the cyclone. And a circulating particle adjusting valve for controlling a circulating amount of particles at an outlet of the hopper.
において、 サイクロン捕集粒子を流動層式熱交換器に導き、冷却粒
子量を制御しながら火炉に再投入し燃焼温度を制御可能
することを特徴とする流動層燃焼ボイラ。3. The fluidized-bed combustion boiler according to claim 1, wherein the cyclone trapping particles are guided to a fluidized-bed heat exchanger, and the combustion temperature can be controlled by re-charging the particles into the furnace while controlling the amount of cooling particles. A fluidized bed combustion boiler, characterized in that:
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP03345821A JP3095499B2 (en) | 1991-12-27 | 1991-12-27 | Fluidized bed combustion boiler |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP03345821A JP3095499B2 (en) | 1991-12-27 | 1991-12-27 | Fluidized bed combustion boiler |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH05180413A JPH05180413A (en) | 1993-07-23 |
| JP3095499B2 true JP3095499B2 (en) | 2000-10-03 |
Family
ID=18379207
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP03345821A Expired - Fee Related JP3095499B2 (en) | 1991-12-27 | 1991-12-27 | Fluidized bed combustion boiler |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3095499B2 (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07198111A (en) * | 1993-12-29 | 1995-08-01 | Mitsui Eng & Shipbuild Co Ltd | Combustor inside temperature control method for circulating fluidized bed boiler |
| JPH1182968A (en) * | 1997-09-08 | 1999-03-26 | Ishikawajima Harima Heavy Ind Co Ltd | Rdf fired circulation fluidized bed furnace |
| JP4817459B2 (en) * | 2007-12-10 | 2011-11-16 | メタウォーター株式会社 | Sludge incineration apparatus and sludge incineration method using the same |
| JP5435973B2 (en) * | 2009-01-30 | 2014-03-05 | メタウォーター株式会社 | Fluidized incinerator |
| JP5336898B2 (en) * | 2009-03-27 | 2013-11-06 | 三菱重工業株式会社 | Bubble type fluidized bed boiler and operation method thereof |
| CN106989386A (en) * | 2017-05-08 | 2017-07-28 | 中国华能集团清洁能源技术研究院有限公司 | A kind of depth presses down the CFBB of nitrogen minimum discharge |
| JP7075574B2 (en) * | 2017-05-29 | 2022-05-26 | 国立研究開発法人産業技術総合研究所 | Combustion furnace of organic waste and treatment system of organic waste using the combustion furnace |
| CN114135897B (en) * | 2021-11-24 | 2023-12-19 | 吉林省电力科学研究院有限公司 | Online monitoring method for high-sulfur coal fired boiler |
-
1991
- 1991-12-27 JP JP03345821A patent/JP3095499B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH05180413A (en) | 1993-07-23 |
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