JP2641826B2 - Combustion method of liquid fuel in circulating fluidized bed - Google Patents
Combustion method of liquid fuel in circulating fluidized bedInfo
- Publication number
- JP2641826B2 JP2641826B2 JP4181371A JP18137192A JP2641826B2 JP 2641826 B2 JP2641826 B2 JP 2641826B2 JP 4181371 A JP4181371 A JP 4181371A JP 18137192 A JP18137192 A JP 18137192A JP 2641826 B2 JP2641826 B2 JP 2641826B2
- Authority
- JP
- Japan
- Prior art keywords
- fluidized bed
- liquid fuel
- combustion chamber
- fuel
- 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.)
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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、循環流動床で石炭、燃
料油等の炭材を燃焼させ、それら燃料の燃焼熱を効率良
く回収する方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for combusting coal and fuel oil in a circulating fluidized bed and efficiently recovering the heat of combustion of the fuel.
【０００２】[0002]
【従来の技術】流動層を利用した燃焼装置は、多様な固
体燃料を安定した条件下で効率良く燃焼することができ
る特徴を活かし、種々の分野で利用されている。また、
この燃焼装置によるとき、燃焼時に発生するＳＯ2 ，Ｎ
Ｏx 等の有害成分も少なくなる。2. Description of the Related Art Combustion apparatuses utilizing a fluidized bed are utilized in various fields, taking advantage of the feature that various solid fuels can be efficiently burned under stable conditions. Also,
With this combustion device, SO 2 , N generated during combustion
Harmful components such as Ox are also reduced.
【０００３】この燃焼装置は、一つの層内で炭材を流動
化させるバブリング流動層式と、層外に飛散した炭材を
層内に循環させる循環流動層式とに大別される。[0003] This combustion device is roughly classified into a bubbling fluidized bed type in which the carbon material is fluidized in one bed and a circulating fluidized bed type in which the carbon material scattered outside the bed is circulated in the bed.
【０００４】この循環流動層式の燃焼装置は、空塔速度
を大きくし炭材、熱媒体等を積極的に循環させているの
で、良好な混合特性および高い伝熱特性が得られる。ま
た、均一な温度場の中で燃料と空気との接触が充分に行
なわれることから、低温燃焼が可能となり、流動層を構
成する部材の耐久性が向上することは勿論、サーマルＮ
Ｏx の発生も抑制される。[0004] In this circulating fluidized bed combustion apparatus, good mixing characteristics and high heat transfer characteristics can be obtained because the superficial velocity is increased and the carbonaceous material, the heat medium and the like are actively circulated. Further, since the fuel and the air are sufficiently contacted in a uniform temperature field, low-temperature combustion becomes possible, so that the durability of the members constituting the fluidized bed is improved, and the thermal N
Ox generation is also suppressed.
【０００５】図４は、すでに知られている循環流動層式
の燃焼装置の一つを示す（特公昭５７−２８０４６号公
報、特公昭５９−１３６４４号公報等参照）。FIG. 4 shows one of the known circulating fluidized bed combustion apparatuses (see Japanese Patent Publication No. 57-28046, Japanese Patent Publication No. 59-13644, etc.).
【０００６】この燃焼装置においては、流動層反応炉４
１にランス４２から石炭、燃料油等の炭材が吹き込まれ
る。炭材は、流動層反応炉４１の底部から導管４３を介
して吹き込まれた流動化ガスによって流動状態に維持さ
れる。そして、流動化ガスに含まれている酸素および二
次ガス導入管４４から吹き込まれる空気によって炭材が
燃焼し、燃焼ガスは流動層反応炉４１内を上昇する。流
動層反応炉４１の内部には、水等の冷媒を循環させる管
を多数備えた冷却面４５が設けられている。また、流動
層反応炉４１の炉壁部分にも、同様な構造をもつ冷却面
４６が設けられている。In this combustion apparatus, the fluidized bed reactor 4
Coal material such as coal and fuel oil is blown into lance 1 from lance 42. The carbonaceous material is maintained in a fluidized state by the fluidizing gas blown from the bottom of the fluidized bed reactor 41 through the conduit 43. Then, the carbon material is combusted by oxygen contained in the fluidizing gas and air blown from the secondary gas introduction pipe 44, and the combustion gas rises in the fluidized bed reactor 41. Inside the fluidized bed reactor 41, a cooling surface 45 provided with a number of pipes for circulating a coolant such as water is provided. Further, a cooling surface 46 having a similar structure is provided also on the furnace wall portion of the fluidized bed reaction furnace 41.
【０００７】燃焼ガスが炉内を上昇する過程で冷却面４
５および冷却面４６を流れる冷媒と熱交換され、燃焼ガ
スの保有熱は高温の冷媒として外部に取り出される。他
方、熱交換後の燃焼ガスは、分離器４７に送られる。こ
の分離器４７にも、同様な構造をもつ冷却面４８が設け
られている。流動層反応炉４１から送り出された燃焼ガ
スは、この分離器４７を下降流として流れる。As the combustion gas rises in the furnace, the cooling surface 4
Heat exchange is performed with the refrigerant flowing through the cooling gas 5 and the cooling surface 46, and the retained heat of the combustion gas is taken out as a high-temperature refrigerant. On the other hand, the combustion gas after the heat exchange is sent to the separator 47. This separator 47 is also provided with a cooling surface 48 having a similar structure. The combustion gas sent from the fluidized bed reactor 41 flows down the separator 47 as a downward flow.
【０００８】この過程で、燃焼ガスの保有熱は、更に冷
却面４８によって系外に取り出される。また、燃焼ガス
に浮遊している未燃焼炭材、灰分等の粒子は、燃焼ガス
から分離され、返送管４９を経由して流動層反応炉４１
に戻される。他方、冷却された燃焼ガスは、排気管５０
を経て排熱ボイラー５１に送られ、更に抜熱された後、
集塵機５２に送られる。In this process, the retained heat of the combustion gas is further taken out of the system by the cooling surface 48. Further, particles such as unburned carbon material and ash floating in the combustion gas are separated from the combustion gas, and the fluidized bed reactor 41 is returned via the return pipe 49.
Is returned to. On the other hand, the cooled combustion gas is supplied to the exhaust pipe 50.
After being sent to the waste heat boiler 51 and further heat removal,
It is sent to the dust collector 52.
【０００９】集塵機５２で除塵された燃焼ガスは、排ガ
スとして系外に放出される。他方、燃焼ガスから分離し
た固形物質は、導管５３を介して流動層冷却器５４に送
り込まれる。流動層冷却器５４には、返送管４９の途中
に接続された導管５５を介して、分離器４７で分離され
た固形物質の一部も送り込まれる。[0009] The combustion gas removed by the dust collector 52 is discharged out of the system as exhaust gas. On the other hand, the solid matter separated from the combustion gas is sent to a fluidized bed cooler 54 via a conduit 53. A part of the solid matter separated by the separator 47 is also fed into the fluidized bed cooler 54 via a conduit 55 connected in the middle of the return pipe 49.
【００１０】これらの固形物質は、導管５６から吹き込
まれる酸素含有ガスによって流動化される。このガス
は、フードで集められ、二次ガスとして二次ガス導入管
４４から流動層反応炉４１に吹き込まれる。[0010] These solids are fluidized by an oxygen-containing gas blown from conduit 56. This gas is collected in a hood and blown into the fluidized bed reactor 41 from the secondary gas introduction pipe 44 as a secondary gas.
【００１１】また、流動層冷却器５４内の固形物質は、
導管５７から吹き込まれる酸素含有ガスと熱交換され
る。このようにして予熱された酸素含有ガスは、流動化
ガスとして導管４３から、およびキャリアガスとしてラ
ンス４２から流動層反応炉４１の内部に吹き込まれる。The solid matter in the fluidized bed cooler 54 is:
The heat is exchanged with the oxygen-containing gas blown from the conduit 57. The oxygen-containing gas thus preheated is blown into the fluidized bed reactor 41 from a conduit 43 as a fluidizing gas and from a lance 42 as a carrier gas.
【００１２】[0012]
【発明が解決しようとする課題】従来、循環流動床燃焼
装置が対象としてきた主要炭材は、固体燃料の石炭であ
り、今日、その安定燃焼方法は既に確立し、随所で実施
されている。また他の対象燃料として、気体燃料と液体
燃料があるが、なかでも工業的には液体燃料の重油が重
要である。Conventionally, the main carbon material to which the circulating fluidized bed combustion apparatus has been applied is solid fuel coal, and its stable combustion method has been already established and implemented everywhere. Other target fuels include gaseous fuel and liquid fuel. Among them, heavy oil of liquid fuel is important industrially.
【００１３】しかし、現在までのところ液体燃料を循環
流動床において石炭と同様に環境上の問題を発生させる
ことなく、安全に効率良く燃焼させる方法が確立されて
いるとは云い難い。However, to date, it has been difficult to say that a method for safely and efficiently burning liquid fuel in a circulating fluidized bed in a circulating fluidized bed without causing the same environmental problems as coal has been established.
【００１４】一つの燃焼装置において固体から液体燃料
まで使用燃料の種類が拡大できればユーザーにとって、
燃料の購入政策上有利であり、より低価格の燃料が使用
できるためエネルギーコストが削減でき、また、一燃料
系にトラブルが発生した場合でも、他燃料系への切替に
より設備停止が回避でき、長期間高稼動率を維持するこ
とが可能となる等のメリットを享受できる。If the type of fuel used in a single combustion device can be expanded from solid to liquid fuel,
It is advantageous in terms of fuel purchase policy, and lower cost fuel can be used, so energy costs can be reduced, and even if a problem occurs in one fuel system, equipment stoppage can be avoided by switching to another fuel system, Advantages such as being able to maintain a high operation rate for a long time can be enjoyed.
【００１５】液体燃料は固体燃料に比べてかなり燃焼速
度が速いため、循環流動床での重油燃焼において、石炭
燃焼時と同レベルの温度分布およびＳＯ2 ，ＮＯx 等の
環境値を達成し、安全に効率良く燃焼させるためには、
重油の燃焼室内での集中を如何に回避するかがポイント
で、循環粒子の平均懸濁濃度の高い部位において重油と
循環粒子との充分な混合状態を確保し、流動層燃焼室の
水平断面内に一様に重油を行きわたらせることが必要で
ある。Since the combustion speed of liquid fuel is considerably higher than that of solid fuel, in fuel oil combustion in a circulating fluidized bed, the same level of temperature distribution and environmental values such as SO 2 and NOx as in coal combustion are achieved, and In order to burn efficiently
The point is how to avoid the concentration of heavy oil in the combustion chamber, ensuring a sufficient mixing state of heavy oil and circulating particles in the area where the average suspended concentration of circulating particles is high, and in the horizontal section of the fluidized bed combustion chamber. It is necessary to distribute the heavy oil uniformly.
【００１６】つまり、循環粒子が多数存在し、かつ粒子
群が活発に運動している領域に重油を供給し、供給重油
を粒子と充分に混合させることが第一であり、燃焼室内
においては、底部からの１次空気による粒子群の強力な
撹拌機能を利用して重油との混合粒子を燃焼室水平断面
内に広く拡散させることが安定な燃焼状態を維持する上
の課題である。That is, the first is to supply heavy oil to a region where a large number of circulating particles are present and the particle group is actively moving, and to sufficiently mix the supplied heavy oil with the particles. It is a problem in maintaining a stable combustion state that a mixed particle with heavy oil is widely diffused in a horizontal section of the combustion chamber by utilizing a strong stirring function of the particle group by the primary air from the bottom.
【００１７】すなわち、重油の供給位置や供給方法がそ
の混合・拡散状態、ひいては燃焼性を左右し、重油の循
環粒子との混合・拡散状態が不充分な場合には、重油供
給部近傍に局部的な高温域が形成され、設備構造上の支
障を招くと共に高濃度のＳＯ2 ，ＮＯx 等が発生し環境
上の問題を生じる。That is, the supply position and supply method of the heavy oil affect its mixing / diffusion state, and furthermore, the combustibility. If the mixing / diffusion state of the heavy oil with the circulating particles is insufficient, a local part is provided near the heavy oil supply section. A high temperature region is formed, which causes troubles in the structure of the equipment, and generates high concentrations of SO 2 , NOx, etc., thereby causing environmental problems.
【００１８】一方、重油が循環粒子の平均懸濁濃度が低
い空間内に供給された場合には、重油の循環粒子および
燃焼用空気との混合・拡散が不良となり、局部燃焼や燃
焼不良を起こして未燃分排出によるエネルギー的な損失
の他、安全上、環境上の問題を生じる。On the other hand, if the heavy oil is supplied into a space having a low average suspended concentration of the circulating particles, the mixing and diffusion of the heavy oil with the circulating particles and the combustion air become poor, causing local combustion and poor combustion. In addition to energy loss due to unburned emission, it causes safety and environmental problems.
【００１９】そこで本発明は、上記問題を解決して液体
燃料も石炭等と同様に安定した条件下で燃焼を行ない、
効率良く燃焼ガスから燃焼熱を回収する燃焼方法を提供
するものである。Accordingly, the present invention solves the above-mentioned problems, and the liquid fuel burns under stable conditions like coal, etc.
An object of the present invention is to provide a combustion method for efficiently recovering combustion heat from combustion gas.
【００２０】[0020]
【課題を解決するための手段】本発明は流動層燃焼室内
で１次と２次の上下２段に分けて供給された空気により
流動状態にされた燃料を燃焼させ、未燃成分および灰分
と共に燃焼ガスを分離器に送り、該分離器で前記未燃成
分および灰分を分離して前記流動層燃焼室に返送しなが
ら燃料を燃焼する際、前記２次下段空気の前記流動層燃
焼室内への導入口より下方のレベルにて、液体燃料の供
給のレベル比を０．３〜０．８とすると共に、液体燃料
を液体燃料噴射ガンの軸線と該軸線を含む鉛直面内の水
平線のなす角度が、前記水平線より下向きの５度〜２０
度の液体燃料噴射ガンより供給して燃焼させることを特
徴とする循環流動床における液体燃料の燃焼方法であ
る。SUMMARY OF THE INVENTION According to the present invention, a fuel in a fluidized state is burned by air supplied in a primary and secondary upper and lower stages in a fluidized bed combustion chamber, and together with unburned components and ash. When the combustion gas is sent to a separator, and the unburned components and ash are separated by the separator and returned to the fluidized bed combustion chamber to burn the fuel, the secondary lower air enters the fluidized bed combustion chamber. Supply liquid fuel at a level below the inlet.
The angle between the axis of the liquid fuel injection gun and a horizontal line in a vertical plane including the axis is 5 degrees to 20 degrees below the horizontal line.
A liquid fuel combustion method in a circulating fluidized bed, wherein the liquid fuel is supplied from a liquid fuel injection gun and burned.
【００２１】更に本発明は流動層燃焼室内で１次と２次
の上下２段に分けて供給された空気により流動状態にさ
れた燃料を燃焼させ、未焼成分および灰分等の循環粒子
と共に燃焼ガスを分離器に送り、該分離器で前記循環粒
子を分離し、ニューマチックバルブを経由して前記流動
層燃焼室に返送しながら燃料を燃焼する際、液体燃料を
前記ニューマチックバルブの循環粒子排出側空間内に供
給して燃焼させることを特徴とする循環流動床における
液体燃料の燃焼方法である。Further, the present invention burns a fuel in a fluidized state by air supplied in two stages of primary and secondary in a fluidized bed combustion chamber, and burns it together with circulating particles such as unburned components and ash. When the gas is sent to a separator, the circulating particles are separated by the separator, and the fuel is burned while returning to the fluidized bed combustion chamber via a pneumatic valve, the liquid fuel circulates through the pneumatic valve. A method for burning liquid fuel in a circulating fluidized bed, characterized in that the fuel is supplied into a discharge side space and burned.
【００２２】[0022]
【作用】本発明者等は、液体燃料の供給方法および供給
位置が燃焼性を支配することを見い出し、液体燃料の供
給レベルや供給角度等を適切に設定することにより、液
体燃料を低公害で効率良く燃焼できることを解明した。The present inventors have found that the supply method and supply position of the liquid fuel dominates the combustibility, and by appropriately setting the supply level and supply angle of the liquid fuel, the liquid fuel can be reduced in pollution. Clarified that it can be burned efficiently.
【００２３】[0023]
【実施例】そこで、実施例により本発明を具体的に説明
する。図１は、本実施例において使用した燃焼装置の概
略を示す。また、図２に流動層燃焼室の詳細を示す。The present invention will now be described specifically with reference to examples. FIG. 1 shows an outline of the combustion apparatus used in the present embodiment. FIG. 2 shows details of the fluidized bed combustion chamber.
【００２４】炭材としては、２０mm以下の粒状石炭１を
石炭供給ホッパー２に蓄えておく。また、脱硫材として
１mm以下の粒状石灰石３を石灰石供給ホッパー４に、更
に補助循環粒子として１mm以下の粒状珪砂３３を補助循
環粒子供給ホッパー３４に貯留している。これら石炭
１、石灰石３および珪砂３３はそれぞれのホッパー２，
４，３４から切り出されて、原料供給管５に送り出さ
れ、この原料供給管５を介して流動層燃焼室６の下部に
送り込まれる。この流動層燃焼室６の底部には空気供給
源７に接続されている１次空気導入管８が開孔してい
る。As a carbon material, granular coal 1 having a size of 20 mm or less is stored in a coal supply hopper 2. Further, granular limestone 3 of 1 mm or less as a desulfurizing material is stored in a limestone supply hopper 4, and granular silica sand 33 of 1 mm or less as auxiliary circulation particles is stored in an auxiliary circulation particle supply hopper 34. These coal 1, limestone 3 and quartz sand 33 are placed in respective hoppers 2, 2.
It is cut out from the feed pipes 4 and 34, sent out to the raw material supply pipe 5, and sent into the lower part of the fluidized bed combustion chamber 6 via the raw material supply pipe 5. A primary air introduction pipe 8 connected to an air supply source 7 is opened at the bottom of the fluidized bed combustion chamber 6.
【００２５】この１次空気導入管８から吹き込まれた１
次空気によって、原料供給管５から送り込まれた石炭
１、石灰石３等が流動層燃焼室６で流動状態に維持され
る。また、１次空気導入管８から分岐して設けられた２
次上段空気導入管９と２次下段空気導入管２４は、流動
層燃焼室６内に開孔している。The primary air blown from the primary air introduction pipe 8
By the secondary air, the coal 1, the limestone 3, etc. sent from the raw material supply pipe 5 are maintained in a fluidized state in the fluidized bed combustion chamber 6. In addition, the secondary air branching from the primary air introduction pipe 8 is provided.
The next upper air introduction pipe 9 and the second lower air introduction pipe 24 are opened in the fluidized bed combustion chamber 6.
【００２６】２次上段空気導入管９および２次下段空気
導入管２４から吹き込まれた空気は、１次空気導入管８
からの空気と相まって、石炭１の燃焼を促進させる。こ
の時に発生した燃焼熱は、主として粒状石炭、石灰石、
灰分、珪砂等の固形物質に担持され、この固形物質から
周囲に輻射熱として放散される。The air blown from the secondary upper air introducing pipe 9 and the secondary lower air introducing pipe 24 is supplied to the primary air introducing pipe 8.
In combination with the air from, the combustion of coal 1 is promoted. The heat of combustion generated at this time is mainly granular coal, limestone,
It is carried on a solid substance such as ash and silica sand, and is radiated from the solid substance to the surroundings as radiant heat.
【００２７】そこで、流動層燃焼室６の内部に、図３の
冷却面４５，４６と同様に内部に水等の流体を循環させ
る配管系を備えた抜熱機構３２を設け、燃焼熱を高温流
体として系外に取り出す。Therefore, inside the fluidized-bed combustion chamber 6, there is provided a heat removal mechanism 32 provided with a piping system for circulating a fluid such as water inside similarly to the cooling surfaces 45 and 46 in FIG. Take it out of the system as a fluid.
【００２８】この燃焼によって生成した燃焼ガスは微細
な未燃炭材、石灰石、灰分、珪砂等の循環粒子と共に流
動層燃焼室６内を上昇し、その上部に取り付けられた連
絡管１０を介してサイクロン１１に送られる。The combustion gas generated by this combustion rises in the fluidized-bed combustion chamber 6 together with circulating particles of fine unburned carbonaceous material, limestone, ash, silica sand, etc., and passes through a connecting pipe 10 mounted on the upper part thereof to form a cyclone. 11 is sent.
【００２９】サイクロン１１で循環粒子と分離された燃
焼ガスは、排気管１２を経由して対流ボイラ１３に送ら
れ、熱回収される。そしてこの燃焼ガスは、集塵器１４
で除塵された後、系外に放出される。他方、サイクロン
１１で燃焼ガスから分離された循環粒子は、返送管１５
を下降する。返送管１５の下部は、図示のように一部が
上方に指向した屈曲部とされている。The combustion gas separated from the circulating particles by the cyclone 11 is sent to a convection boiler 13 via an exhaust pipe 12 and heat is recovered. The combustion gas is supplied to the dust collector 14.
After the dust is removed, it is released outside the system. On the other hand, the circulating particles separated from the combustion gas in the cyclone 11 are returned to the return pipe 15.
Descend. The lower part of the return pipe 15 is formed as a bent part partially upward as shown in the figure.
【００３０】この屈曲部にサイクロン１１からの循環粒
子が溜り、返送管１５の下部と流動層燃焼室６の下部と
の間の粉体シールを行なうニューマチックバルブ１６が
構成される。このニューマチックバルブ１６に溜ってい
る循環粒子は、１次空気導入管８から分岐した気送管１
７から吹き込まれる空気圧力によって、流動層燃焼室６
内に適宜返送される。The circulating particles from the cyclone 11 accumulate in the bent portion, and a pneumatic valve 16 for sealing the powder between the lower part of the return pipe 15 and the lower part of the fluidized-bed combustion chamber 6 is formed. The circulating particles accumulated in the pneumatic valve 16 are supplied to the pneumatic pipe 1 branched from the primary air introduction pipe 8.
7, the fluidized bed combustion chamber 6
Will be returned as appropriate.
【００３１】このように、石炭１は、流動層燃焼室６→
サイクロン１１→ニューマチックバルブ１６→流動層燃
焼室６を繰返し循環しながら、完全燃焼する。また、供
給する石炭１中に混入する脈石や流動層燃焼室６内の燃
焼によって生じた比較的粒度の大きな灰分等は、流動層
燃焼室６の底部に接続された排出管１８を経由して、灰
分級器１９に送られる。As described above, the coal 1 is supplied to the fluidized bed combustion chamber 6 →
Complete combustion is performed while repeatedly circulating through the cyclone 11 → pneumatic valve 16 → fluidized bed combustion chamber 6. Further, gangue mixed into the supplied coal 1 and ash having a relatively large particle size generated by combustion in the fluidized bed combustion chamber 6 pass through a discharge pipe 18 connected to the bottom of the fluidized bed combustion chamber 6. Then, it is sent to the ash classifier 19.
【００３２】この灰分級器１９で、空気２０の吹き込み
により、排出管１８から送り込まれた灰分等が粒度分級
される。そして、比較的粒度の大きなものは、粗粒灰分
２１として系外へ排出される。他方、粒度の小さなもの
は、微細灰分２２として返送管２３を介して流動層燃焼
室６に返送される。In the ash classifier 19, the ash and the like sent from the discharge pipe 18 are subjected to particle size classification by blowing air 20. Those having a relatively large particle size are discharged as coarse ash 21 out of the system. On the other hand, those having a small particle size are returned to the fluidized bed combustion chamber 6 through the return pipe 23 as fine ash 22.
【００３３】図２（ａ）に図示した液体燃料供給管３５
は２次下段空気導入管２４より下方の循環粒子の平均懸
濁濃度の高いレベルに設置され、流動層燃焼室６内に開
孔している。また、液体燃料供給管３５の内部で同一中
心軸上には重油およびそれを噴霧して噴射するための蒸
気を流す液体燃料噴射ガン３６があり、該噴射ガン３６
と供給管３５の環状部には流動層燃焼室６内下部の濃厚
粒子群による供給管３５の閉塞防止のためパージ空気３
７を送気している。The liquid fuel supply pipe 35 shown in FIG.
Is installed at a level below the secondary lower air introduction pipe 24 where the average suspended concentration of circulating particles is high, and is opened in the fluidized bed combustion chamber 6. Inside the liquid fuel supply pipe 35, on the same central axis, there is a liquid fuel injection gun 36 for flowing heavy oil and steam for spraying and injecting the heavy oil.
In the annular portion of the supply pipe 35, purge air 3 is provided in order to prevent the supply pipe 35 from being blocked by a dense particle group in the lower part of the fluidized bed combustion chamber 6.
7 is being sent.
【００３４】また、図２（ｂ）に図示した液体燃料供給
管２６は供給管３５と同一構造で、２次下段空気導入管
２４より上方のレベルに設置したもので、この場合、液
体燃料は循環粒子の平均懸濁濃度の低い流動層燃焼室６
内に供給される。なお２次下段空気導入管２４の開孔部
レベルは流動層燃焼室６の底部から１ｍ上方である。第１参考例 この燃焼装置において、抜熱機構３２として長さ１０
ｍ、内径６５．９mm、外径７６．３mmの耐熱鋼製伝熱管
を５本配置したものを流動層燃焼室６の壁面に配置し
た。そしてポンプ３０で各パイプ当たり１２０kg／ｈの
流量で温度２０℃、圧力１０kg／cm2 の水３１を流し
た。また、原料供給管５から送り込まれる石炭１の供給
量を１５０kg／ｈ、石灰石３の供給量をＣａ／Ｓのモル
比で２．５相当として流動層燃焼室６に送り込み、流動
層燃焼室６内の温度を８５０℃に維持して石炭１を燃焼
させた。The liquid fuel supply pipe 26 shown in FIG. 2B has the same structure as the supply pipe 35 and is installed at a level above the secondary lower air introduction pipe 24. In this case, the liquid fuel is Fluidized bed combustion chamber 6 with low average suspended concentration of circulating particles
Supplied within. The level of the opening of the secondary lower air introduction pipe 24 is 1 m above the bottom of the fluidized bed combustion chamber 6. First Reference Example In this combustion apparatus, the heat removal mechanism 32 has a length of 10 mm.
A heat transfer pipe made of five heat-resistant steel tubes having a diameter of 65.9 mm, an inner diameter of 65.9 mm and an outer diameter of 76.3 mm was arranged on the wall of the fluidized-bed combustion chamber 6. Then, water 31 having a temperature of 20 ° C. and a pressure of 10 kg / cm 2 was flowed by the pump 30 at a flow rate of 120 kg / h for each pipe. The feed rate of the coal 1 fed from the raw material feed pipe 5 is set to 150 kg / h, and the feed rate of the limestone 3 is set to a molar ratio of Ca / S of 2.5, and is fed to the fluidized bed combustion chamber 6. The temperature of the inside was maintained at 850 ° C. to burn coal 1.
【００３５】また、１次空気、２次空気の合計供給量は
供給石炭の理論燃焼空気量の１．２倍とした。１次空気
の供給量は全供給量の５０％とし、残りを２次上段およ
び下段空気として供給した。この時、燃焼室内最高温度
は８５０℃であり、サイクロン１１出口における排ガス
中の一酸化炭素濃度は１７０ppm 、ＳＯ2 濃度は８０pp
m であった。The total supply amount of the primary air and the secondary air was set to 1.2 times the theoretical combustion air amount of the supplied coal. The supply amount of the primary air was 50% of the total supply amount, and the remainder was supplied as secondary upper and lower air. At this time, the maximum temperature in the combustion chamber was 850 ° C., the concentration of carbon monoxide in the exhaust gas at the outlet of the cyclone 11 was 170 ppm, and the concentration of SO 2 was 80 pp.
m.
【００３６】第２参考例 液体燃料として表１に性状を示す高硫黄Ｃ重油を、図２
（ｂ）に図示した２次下段空気導入管２４の上方に設置
した液体燃料供給管２６の内部で、かつ同一中心軸上の
燃料噴射ガン２７より供給量３９kg／ｈ（全入熱の４０
％相当）で流動層燃焼室６内へ供給し、全入熱を一定と
するため石炭１の供給量を９０kg／ｈに減らした。 Second Reference Example As a liquid fuel, high sulfur C heavy oil whose properties are shown in Table 1 was used.
The supply amount of 39 kg / h from the fuel injection gun 27 on the same central axis inside the liquid fuel supply pipe 26 installed above the secondary lower air introduction pipe 24 shown in FIG.
%), And the supply amount of coal 1 was reduced to 90 kg / h in order to keep the total heat input constant.
【００３７】[0037]
【表１】 [Table 1]
【００３８】また、石灰石３の供給量はＣａ／Ｓのモル
比で３．０とし、同時に珪砂３３を２．４kg／ｈ供給し
た。そして、１次空気・２次空気の合計供給量は全供給
燃料の理論燃焼空気量の１．２倍とし、１次空気の供給
量は全供給量の５０％、残りを２次上段および下段空気
として供給した。The supply amount of the limestone 3 was adjusted to 3.0 by a molar ratio of Ca / S, and 2.4 kg / h of silica sand 33 was supplied at the same time. The total supply amount of the primary air and the secondary air is 1.2 times the theoretical combustion air amount of all the supplied fuels, the supply amount of the primary air is 50% of the total supply amount, and the rest is the secondary upper and lower stages. Supplied as air.
【００３９】なお、流動層燃焼室６の底部から液体燃料
供給管２６の開孔部のレベルと２次下段空気導入管のそ
れとのレベル比は３．０であり、供給管２６の軸線と該
軸線を含む鉛直面内の水平線のなす角度（以下、重油供
給角度と記す）を５度とした。The level ratio between the level of the opening of the liquid fuel supply pipe 26 from the bottom of the fluidized bed combustion chamber 6 and that of the secondary lower air introduction pipe is 3.0, and the axis of the supply pipe 26 is The angle between the horizontal lines in the vertical plane including the axis (hereinafter referred to as heavy oil supply angle) was set to 5 degrees.
【００４０】この時、燃焼室内温度は重油の供給近傍域
が高温化して大きな温度偏差が生じ、最高温度は９７０
℃に上昇した。また、サイクロン１１出口における排ガ
ス中の一酸化炭素濃度は８００ppm に、ＳＯ2 濃度は４
００ppm となった。At this time, the temperature in the combustion chamber becomes high in the vicinity of the supply of heavy oil, causing a large temperature deviation.
° C. The carbon monoxide concentration in the exhaust gas at the outlet of the cyclone 11 was 800 ppm, and the SO 2 concentration was 4 ppm.
It became 00 ppm.
【００４１】流動層燃焼装置６は燃焼温度８５０℃を前
提として各部の耐熱設計をしており、本参考例の状態は
設備保護上危険な状態であり、またエネルギーの有効利
用上・環境上の問題も発生した。The fluidized bed combustion apparatus 6 is designed to be heat-resistant for each part on the premise of a combustion temperature of 850 ° C. The state of this reference example is a dangerous state for equipment protection, and is also effective for effective use of energy and environmental protection. Problems also occurred.
【００４２】第１実施例 第１実施例では、他の条件は第２参考例と同一として、
重油を図２（ａ）に図示したように２次下段空気導入管
２４の下方のレベルに設置した液体燃料供給管３５の内
部でかつ同一中心軸上の燃料噴射ガン３６より供給し
た。この時、供給管３５と２次下段空気導入管２４との
レベル比は０．４７、重油供給角度は５度とした。 First Embodiment In the first embodiment, other conditions are the same as in the second reference example.
As shown in FIG. 2A, heavy oil was supplied from a fuel injection gun 36 inside a liquid fuel supply pipe 35 installed at a level below the secondary lower air introduction pipe 24 and on the same central axis. At this time, the level ratio between the supply pipe 35 and the secondary lower air introduction pipe 24 was 0.47, and the heavy oil supply angle was 5 degrees.
【００４３】この結果、燃焼室内の最高温度は８５０
℃、一酸化炭素濃度は１８０ppm 、ＳＯ2 濃度は９０pp
m となり、第１参考例と同等の良好な燃焼状態が得られ
た。As a result, the maximum temperature in the combustion chamber is 850
° C, carbon monoxide concentration is 180 ppm, SO 2 concentration is 90 pp
m, and a good combustion state equivalent to that of the first reference example was obtained.
【００４４】第３参考例 第３参考例は、第１実施例において液体燃料供給管３５
の重油供給角度を０度に設定し、他の条件は同一とし
た。この結果、第１実施例より燃焼室内の温度偏差が増
加し、最高温度は９２０℃、一酸化炭素濃度は２３０pp
m 、ＳＯ2 濃度は１５０ppm となり、不安定な燃焼状態
となった。The third reference example 3 Reference example liquid fuel supply pipe 35 in the first embodiment
Was set to 0 degree, and other conditions were the same. As a result, the temperature deviation in the combustion chamber increased from the first embodiment, the maximum temperature was 920 ° C., and the carbon monoxide concentration was 230 pp.
The m 2 and SO 2 concentrations became 150 ppm, resulting in an unstable combustion state.
【００４５】第２実施例 次に、第１実施例において液体燃料供給管３５の重油供
給角度を２０度に設定し、他の条件は同一とした。その
結果、燃焼室内温度偏差は解消し最高温度は８５０℃、
一酸化炭素濃度は１７０ppm 、ＳＯ2 濃度は７０ppm と
なり第１実施例と同様に安定な燃焼状態が得られた。 Second Embodiment Next, in the first embodiment, the heavy oil supply angle of the liquid fuel supply pipe 35 was set to 20 degrees, and other conditions were the same. As a result, the temperature deviation in the combustion chamber was eliminated and the maximum temperature was 850 ° C.
The carbon monoxide concentration was 170 ppm and the SO 2 concentration was 70 ppm, and a stable combustion state was obtained as in the first embodiment.
【００４６】第４参考例 更に、第１実施例において液体燃料供給管３５の重油供
給角度を２５度に設定し、他の条件は同一とした。この
時、第２実施例より燃焼室内の温度偏差が増加し、最高
温度は９１０℃、一酸化炭素濃度は２２０ppm 、ＳＯ2
濃度は１２０ppm となり、不安定な燃焼状態となった。 Fourth Reference Example Further, in the first embodiment, the fuel oil supply angle of the liquid fuel supply pipe 35 was set to 25 degrees, and other conditions were the same. At this time, the temperature deviation in the combustion chamber increased from the second embodiment, the maximum temperature was 910 ° C., the carbon monoxide concentration was 220 ppm, and the SO 2
The concentration became 120 ppm, resulting in an unstable combustion state.
【００４７】第５参考例 第５参考例では、液体燃料供給管３５と２次下段空気導
入管２４とのレベル比を０．８５、すなわち循環粒子の
平均懸濁濃度変化が比較的大きな境界部付近とし、重油
供給角度を５度に設定し、他の条件を第１実施例と同一
とした。この結果、第２実施例より温度偏差が上昇し、
一酸化炭素濃度、ＳＯ2 濃度等が増加した。 Fifth Reference Example In the fifth reference example, the level ratio between the liquid fuel supply pipe 35 and the secondary lower air introduction pipe 24 is 0.85, that is, the boundary portion where the change in the average suspended concentration of the circulating particles is relatively large. In the vicinity, the fuel oil supply angle was set to 5 degrees, and the other conditions were the same as in the first embodiment. As a result, the temperature deviation increases as compared with the second embodiment,
Carbon monoxide concentration, SO 2 concentration, etc. increased.
【００４８】第６参考例 次に、他の条件は同一として第５参考例の液体燃料供給
管３５のレベル比を０．２５、すなわち流動層燃焼室６
の底部近傍とし、重油供給角度を２０度に設定した。こ
の結果、流動層燃焼室６底部の１次空気導入管８の重油
による汚染・閉塞の他、第５参考例と同様に燃焼室内の
温度偏差の上昇、一酸化炭素濃度、ＳＯ2 濃度の増加等
の問題が発生した。 Sixth Embodiment Next, the other conditions are the same, and the level ratio of the liquid fuel supply pipe 35 of the fifth embodiment is 0.25, that is, the fluidized bed combustion chamber 6
And the fuel oil supply angle was set to 20 degrees. As a result, the primary air introduction pipe 8 at the bottom of the fluidized-bed combustion chamber 6 is contaminated and blocked by heavy oil, as in the fifth embodiment, the temperature deviation in the combustion chamber increases, the carbon monoxide concentration, and the SO 2 concentration increase. And other problems.
【００４９】表２に、石炭との混焼結果を含め、コーク
ス炉ガスとの混焼および重油専焼の結果を要約して示
す。Table 2 summarizes the results of co-firing with coke oven gas and heavy oil firing, including the results of co-firing with coal.
【００５０】[0050]
【表２】 [Table 2]
【００５１】図３は別の実施例を示す。図３（ａ）およ
び（ｂ）に図示した液体燃料供給管３５は濃厚な粒子群
が存在しているニューマチックバルブ１６の循環粒子３
９の排出側に設置され、ニューマチックバルブ１６内に
開孔している。FIG. 3 shows another embodiment. The liquid fuel supply pipe 35 shown in FIGS. 3A and 3B is provided with the circulating particles 3 of the pneumatic valve 16 in which a dense particle group exists.
9 and is opened in the pneumatic valve 16.
【００５２】また、液体燃料供給管３５の内部で同一中
心軸上には重油およびそれを噴霧して噴射するための蒸
気を流す液体燃料噴射ガン３６があり、該噴射ガン３６
と供給管３５の環状部にはニューマチックバルブ１６内
の濃厚粒子群による供給管３５の閉塞防止、燃焼補助用
として空気３７を送気している。また、図３（ｃ）は下
記、第２参考例として実施したケースを図示したもの
で、液体燃料供給管２６は供給管３５と同一構造で、流
動層燃焼室６本体の２次下段空気導入管２４より２ｍ上
方のレベルに設置した。Further, on the same central axis inside the liquid fuel supply pipe 35, there is a liquid fuel injection gun 36 for flowing heavy oil and steam for spraying and injecting it.
Air 37 is supplied to the annular portion of the supply pipe 35 to prevent blockage of the supply pipe 35 by the dense particles in the pneumatic valve 16 and to assist combustion. FIG. 3C shows a case implemented as a second reference example, in which the liquid fuel supply pipe 26 has the same structure as the supply pipe 35, and the secondary lower air introduction of the fluidized bed combustion chamber 6 main body is performed. It was installed at a level 2 m above the tube 24.
【００５３】この場合、液体燃料は循環粒子の平均懸濁
濃度の低い流動層燃焼室６内に供給される。なお２次下
段空気導入管２４の開孔部レベルは流動層燃焼室６の底
部から１ｍ上方である。In this case, the liquid fuel is supplied into the fluidized bed combustion chamber 6 having a low average suspended concentration of circulating particles. The level of the opening of the secondary lower air introduction pipe 24 is 1 m above the bottom of the fluidized bed combustion chamber 6.
【００５４】第７参考例 この燃焼装置において、抜熱機構３２として長さ１０
ｍ、内径６５．９mm、外径７６．３mmの耐熱鋼製伝熱管
を５本配置したものを流動層燃焼室６の壁面に配置し
た。そしてポンプ３０で各パイプ当たり１２０kg／ｈの
流量で温度２０℃、圧力１０kg／cm2 の水３１を流し
た。 Seventh Reference Example In this combustion apparatus, the heat removal mechanism 32 has a length of 10 mm.
A heat transfer pipe made of five heat-resistant steel tubes having a diameter of 65.9 mm, an inner diameter of 65.9 mm and an outer diameter of 76.3 mm was arranged on the wall of the fluidized-bed combustion chamber 6. Then, water 31 having a temperature of 20 ° C. and a pressure of 10 kg / cm 2 was flowed by the pump 30 at a flow rate of 120 kg / h for each pipe.
【００５５】また、原料供給管５から送り込まれる石炭
１の供給量を１５０kg／ｈ、石灰石３の供給量をＣａ／
Ｓのモル比で２．５相当として流動層燃焼室６に送り込
み、流動層燃焼室６内の温度を８５０℃に維持して石炭
１を燃焼させた。また、１次空気、２次空気の合計供給
量は供給石炭の理論燃焼空気量の１．２倍とした。The supply amount of coal 1 fed from the raw material supply pipe 5 is 150 kg / h, and the supply amount of limestone 3 is Ca /
S was supplied to the fluidized bed combustion chamber 6 at a molar ratio of 2.5, and the temperature of the fluidized bed combustion chamber 6 was maintained at 850 ° C. to burn the coal 1. The total supply amount of the primary air and the secondary air was 1.2 times the theoretical combustion air amount of the supplied coal.
【００５６】１次空気の供給量は全供給量の５０％と
し、残りを２次上段および下段空気として供給した。こ
の時、燃焼室内最高温度は８５０℃であり、サイクロン
１１出口における排ガス中の一酸化炭素濃度は１７０pp
m 、ＳＯ2 濃度は８０ppm であった。The supply amount of the primary air was 50% of the total supply amount, and the remainder was supplied as secondary upper and lower air. At this time, the maximum temperature in the combustion chamber was 850 ° C., and the concentration of carbon monoxide in the exhaust gas at the outlet of the cyclone 11 was 170 pp.
m and SO 2 concentration were 80 ppm.
【００５７】第８参考例 液体燃料として表１に示す性状の高硫黄Ｃ重油を図３
（ｃ）に図示した２次下段空気導入管２４の上方に設置
した液体燃料供給管２６の内部でかつ同一中心軸上の燃
料噴射ガン２７より供給量３９kg／ｈ（全入熱の４０％
相当）で流動層燃焼室６内へ供給し、全入熱を一定とす
るため石炭１の供給量を９０kg／ｈに減らした。 Eighth Reference Example A high-sulfur C heavy oil having the properties shown in Table 1 was used as a liquid fuel in FIG.
The supply amount is 39 kg / h (40% of the total heat input) from the fuel injection gun 27 on the same central axis inside the liquid fuel supply pipe 26 installed above the secondary lower air introduction pipe 24 shown in FIG.
(Equivalent), the coal 1 was supplied into the fluidized bed combustion chamber 6, and the supply amount of coal 1 was reduced to 90 kg / h in order to keep the total heat input constant.
【００５８】また、石灰石３の供給量はＣａ／Ｓのモル
比で３．０とし、同時に珪砂３３を２．４kg／ｈ供給し
た。そして、１次空気・２次空気の合計供給量は全供給
燃料の理論燃焼空気量の１．２倍とし、１次空気の供給
量は全供給量の５０％、残りを２次上段および下段空気
として供給した。The supply amount of the limestone 3 was set at 3.0 in a molar ratio of Ca / S, and 2.4 kg / h of silica sand 33 was supplied at the same time. The total supply amount of the primary air and the secondary air is 1.2 times the theoretical combustion air amount of all the supplied fuels, the supply amount of the primary air is 50% of the total supply amount, and the rest is the secondary upper and lower stages. Supplied as air.
【００５９】この時、燃焼室内温度は重油の供給点近傍
域が高温化して大きな温度偏差が生じ、最高温度は９７
０℃に上昇した。また、サイクロン１１出口における排
ガス中の一酸化炭素濃度は８００ppm に、ＳＯ2 濃度は
４００ppm となった。流動層燃焼室６は燃焼温度８５０
℃を前提として各部の耐熱設計をしており、本参考例の
状態は設備保護上危険な状態であり、またエネルギーの
有効利用上・環境上の問題も発生した。At this time, the temperature in the combustion chamber becomes large in the vicinity of the supply point of heavy oil, causing a large temperature deviation.
The temperature rose to 0 ° C. Further, the concentration of carbon monoxide in the exhaust gas at the outlet of the cyclone 11 was 800 ppm, and the concentration of SO 2 was 400 ppm. The fluidized bed combustion chamber 6 has a combustion temperature of 850.
Each part is designed to be heat-resistant on the assumption of ° C, and the state of this reference example is dangerous for equipment protection, and there are also problems in effective use of energy and environmental problems.
【００６０】第５実施例 次に、他の条件は第８参考例と同一として、重油を図３
（ａ）に図示したように濃厚な粒子群が存在しているニ
ューマチックバルブ１６の循環粒子３９の排出側上方に
設置した液体燃料供給管３５の内部でかつ同一中心軸上
の燃料噴射ガン３６より供給した。 Fifth Embodiment Next, the other conditions were the same as in the eighth embodiment, and heavy oil was used as shown in FIG.
As shown in (a), the fuel injection gun 36 is located inside the liquid fuel supply pipe 35 installed above the discharge side of the circulating particles 39 of the pneumatic valve 16 in which a dense particle group exists and on the same central axis. Supplied more.
【００６１】この結果、第８参考例のような燃焼室の局
部高温化、温度偏差は解消し燃焼室内の最高温度は８５
０℃、一酸化炭素濃度は１８０ppm 、ＳＯ2 濃度は９０
ppmとなり、第７参考例と同等の良好な燃焼状態が得ら
れた。また、重油供給点近傍のニューマチックバルブ１
６の空間内部の高温化、重油による汚染、塊状物の生成
および閉塞等の設備障害もみられなかった。As a result, the local high temperature of the combustion chamber and the temperature deviation as in the eighth embodiment are eliminated, and the maximum temperature in the combustion chamber becomes 85.
0 ° C., carbon monoxide concentration 180 ppm, SO 2 concentration 90
ppm, and a good combustion state equivalent to that of the seventh reference example was obtained. Also, a pneumatic valve 1 near the fuel oil supply point
No equipment troubles such as high temperature inside the space No. 6, contamination by heavy oil, formation of blockage and blockage were observed.
【００６２】第６実施例 第６実施例では、液体燃料供給管３５を図３（ｂ）に図
示したようにニューマチックバルブ１６の循環粒子３９
の排出側側方に設置し、他の条件は第１実施例と同一と
した。この結果、第５実施例と同等の安定な燃焼状態が
得られ、設備障害もなかった。 Sixth Embodiment In a sixth embodiment, the liquid fuel supply pipe 35 is connected to the circulating particles 39 of the pneumatic valve 16 as shown in FIG.
And the other conditions were the same as in the first embodiment. As a result, a stable combustion state equivalent to that of the fifth embodiment was obtained, and there was no equipment failure.
【００６３】表３に、上述の石炭との混焼結果を含め、
コークス炉ガスとの混焼および重油専焼の結果を要約し
て示す。Table 3 includes the results of co-firing with coal described above.
The results of co-firing with coke oven gas and heavy oil firing are summarized below.
【００６４】[0064]
【表３】 [Table 3]
【００６５】本発明者等は、以上述べてきた循環流動層
燃焼装置における液体燃料の燃焼方法について考察した
結果、燃焼状態と燃料供給方法および供給位置に関し、
次のような知見を得た。The present inventors have considered the method of burning liquid fuel in the circulating fluidized bed combustion apparatus described above, and have found that the combustion state, fuel supply method and supply position are as follows.
The following findings were obtained.
【００６６】すなわち、固体燃料より燃焼速度の速い液
体燃料を設備上安全に、エネルギー利用上有効に、かつ
環境上問題のない水準で安定して燃焼させるためには、
液体燃料を循環粒子が高密度で存在する燃焼室下部の粒
子濃厚層レベルから供給し、底部から吹き込まれている
１次空気による粒子群の活発な撹拌運動を利用して液体
燃料を循環粒子に坦持させるように混合すると共に、流
動層燃焼室水平断面内に拡散させ、循環粒子の上昇と共
に燃焼室の高さ方向で緩慢に燃焼させることである。In other words, in order to burn liquid fuel having a higher combustion rate than solid fuel safely on equipment, effectively on energy use, and stably at a level without environmental problems,
Liquid fuel is supplied from the dense particle level at the lower part of the combustion chamber where circulating particles exist at a high density, and the liquid fuel is circulated into the circulating particles by vigorous agitation of particles caused by primary air blown from the bottom. In addition to mixing so as to be supported, it is diffused in the horizontal section of the fluidized bed combustion chamber, and slowly burns in the height direction of the combustion chamber as the circulating particles rise.
【００６７】すなわち、液体燃料を直接燃焼室に供給し
て燃焼させる場合の液体燃料の供給方法として、燃料供
給レベルは２次下段空気導入管２４より下方であって、
それとのレベル比は０．３〜０．８が適当であり、そし
て、５〜２０度の供給角度を維持して噴射供給すること
が必要であることを実験的に見い出した。That is, as a method of supplying the liquid fuel when the liquid fuel is directly supplied to the combustion chamber for combustion, the fuel supply level is below the secondary lower air introduction pipe 24,
It has been experimentally found that a level ratio of 0.3 to 0.8 is appropriate, and that it is necessary to maintain the supply angle of 5 to 20 degrees for injection and supply.
【００６８】更に次の点も見い出した。循環粒子が高密
度で存在し、かつ活発に運動しながら流動層燃焼室下部
に流入しているニューマチックバルブの循環粒子排出側
の空間内に液体燃料を供給することにより循環粒子と確
実に混合して循環粒子に担持させ、そして流動層燃焼室
内に流入した液体燃料を底部からの１次空気による粒子
群の強力な撹拌運動を利用することにより、液体燃料と
粒子および燃焼用空気との混合を一層高め、かつ流動層
燃焼室水平断面内に広く拡散させて循環粒子の上昇と共
に燃焼室の高さ方向で緩慢に燃焼させることである。Further, the following points have also been found. Circulating particles are present at a high density, and while actively moving, liquid fuel is supplied into the space on the circulating particle discharge side of the pneumatic valve that flows into the lower part of the fluidized bed combustion chamber, thereby reliably mixing with the circulating particles. The liquid fuel flowing into the fluidized bed combustion chamber is mixed with the liquid fuel, and the liquid fuel is mixed with the particles and the combustion air by utilizing the strong stirring motion of the particles by the primary air from the bottom. And further diffuse widely in the horizontal cross section of the fluidized bed combustion chamber to slowly burn in the height direction of the combustion chamber with the rise of the circulating particles.
【００６９】すなわち、循環流動床での液体燃料の燃焼
において、石炭燃焼と同等の燃焼状態は、液体燃料の燃
焼室内での局部集中を回避し、液体燃料の循環粒子と空
気との良好な混合状態の確保および燃焼室内での一様な
分散がポイントであるが、本発明者等は、循環流動床の
各部位の中でそれが可能な液体燃料供給位置として、濃
厚粒子群が循環流動しているニューマチックバルブ部に
着目し、その粒子排出側空間内に噴射供給することで達
成した。That is, in the combustion of liquid fuel in the circulating fluidized bed, a combustion state equivalent to that of coal combustion avoids local concentration of liquid fuel in the combustion chamber, and provides good mixing of circulating particles of liquid fuel with air. The point is to secure the state and to uniformly distribute the particles in the combustion chamber. However, the present inventors have assumed that the dense particle group circulates and flows as a liquid fuel supply position where it is possible in each part of the circulating fluidized bed. This was achieved by focusing on the pneumatic valve part, and injecting and supplying it into the space on the particle discharge side.
【００７０】なお、本発明は、表２および表３に示した
ように固体燃料との混焼ばかりでなく、気体燃料との混
焼および液体燃料の専焼の場合でも有効な方法である。
また、以上の実施例では液体燃料として高硫黄Ｃ重油を
使用したが、本発明は、低硫黄Ａ重油等他の燃料油に対
しても適用可能である。The present invention is an effective method not only in the case of co-firing with a solid fuel, but also in the case of co-firing with a gaseous fuel and mono-firing of a liquid fuel, as shown in Tables 2 and 3.
Further, in the above embodiments, high-sulfur C heavy oil was used as the liquid fuel, but the present invention is also applicable to other fuel oils such as low-sulfur A heavy oil.
【００７１】[0071]
【発明の効果】本発明によれば、循環流動床において局
部高温域の発生による設備上の支障やＳＯ2 ，ＮＯx 等
の排出量の増加、および未燃分排出による省エネルギー
・環境上の問題を生じることなく、液体燃料の安定使用
が可能となる。According to the present invention, problems in facilities due to the occurrence of a local high-temperature region in the circulating fluidized bed, an increase in the emission of SO 2 , NOx, etc., and energy saving and environmental problems due to the emission of unburned components are solved. The liquid fuel can be used stably without causing any problem.
【図１】本発明の実施例で使用した装置の概略図であ
る。FIG. 1 is a schematic view of an apparatus used in an embodiment of the present invention.
【図２】（ａ）および（ｂ）は実施例の流動層燃焼室の
詳細図である。FIGS. 2 (a) and (b) are detailed views of a fluidized bed combustion chamber of an embodiment.
【図３】（ａ），（ｂ）および（ｃ）は他の実施例の流
動燃焼室の詳細図である。FIGS. 3 (a), (b) and (c) are detailed views of a fluidized combustion chamber of another embodiment.
【図４】従来の燃焼装置の説明図である。FIG. 4 is an explanatory diagram of a conventional combustion device.
１ 粒状石炭 ２ 石炭供給ホッパー ３ 粒状石灰石 ４ 石灰石供給ホッパー ５ 原料供給管 ６ 流動層燃焼室 ７ 欠番 ８ １次空気導入管 ９ ２次上段空気導入管 １０ 連絡管 １１ サイクロン １２ 排気管 １３ 対流ボイラ １４ 集塵器 １５ 返送管 １６ ニューマチックバルブ １７ 気送管 １８ 排出管 １９ 灰分級器 ２０ 空気 ２１ 粗粒灰分 ２２ 微細灰分 ２３ 返送管 ２４ ２次下段空気導入管 ２５ 気体燃料供給管 ２６ 液体燃料供給管 ２７ 液体燃料噴射ガン ２８ 欠番 ２９ 欠番 ３０ ポンプ ３１ 水 ３２ 抜熱機構 ３３ 粒状珪砂 ３４ 補助循環粒子供給ホッパー ３５ 液体燃料供給管 ３６ 液体燃料噴射ガン ３７ 空気 ３８ 重油供給角度 ３９ 循環粒子 ４０ 欠番 ４１ 流動層反応炉 ４２ ランス ４３ 導管 ４４ 二次ガス導入管 ４５ 冷却面 ４６ 冷却面 ４７ 分離器 ４８ 冷却面 ４９ 返送管 ５０ 排気管 ５１ 排熱ボイラー ５２ 集塵機 ５３ 導管 ５４ 流動層冷却器 ５５ 導管 ５６ 導管 ５７ 導管 REFERENCE SIGNS LIST 1 granular coal 2 coal supply hopper 3 granular limestone 4 limestone supply hopper 5 raw material supply pipe 6 fluidized bed combustion chamber 7 missing number 8 primary air introduction pipe 9 secondary upper stage air introduction pipe 10 communication pipe 11 cyclone 12 exhaust pipe 13 convection boiler 14 Dust collector 15 Return pipe 16 Pneumatic valve 17 Pneumatic pipe 18 Discharge pipe 19 Ash classifier 20 Air 21 Coarse ash 22 Fine ash 23 Return pipe 24 Secondary lower air introduction pipe 25 Gas fuel supply pipe 26 Liquid fuel supply pipe 27 Liquid Fuel Injection Gun 28 Missing Number 29 Missing Number 30 Pump 31 Water 32 Heat Removal Mechanism 33 Granular Silica 34 Auxiliary Circulating Particle Supply Hopper 35 Liquid Fuel Supply Pipe 36 Liquid Fuel Injection Gun 37 Air 38 Fuel Oil Supply Angle 39 Circulating Particle 40 Missing Number 41 Fluid Bed Reactor 42 Lance 43 Conduit 44 Secondary gas introduction pipe 45 Cooling surface 46 Cold Recirculation surface 47 separator 48 cooling surface 49 return pipe 50 exhaust pipe 51 exhaust heat boiler 52 dust collector 53 conduit 54 fluidized bed cooler 55 conduit 56 conduit 57 conduit
───────────────────────────────────────────────────── フロントページの続き (72)発明者 上谷 順一 北九州市戸畑区大字中原46−59 新日本 製鐵株式会社 機械・プラント事業部内 (72)発明者 古田 雅一 北九州市戸畑区大字中原46−59 新日本 製鐵株式会社 機械・プラント事業部内 (72)発明者 日浦 文明 北九州市戸畑区大字中原46−59 新日本 製鐵株式会社 機械・プラント事業部内 (72)発明者 藤田 源治 北九州市戸畑区大字中原46−59 日鐵プ ラント設計株式会社内 (56)参考文献 特開 昭63−29104（ＪＰ，Ａ) 実開 昭62−98916（ＪＰ，Ｕ) 特表 昭59−500681（ＪＰ，Ａ) ──────────────────────────────────────────────────続 き Continuing on the front page (72) Inventor Junichi Uetani 46-59 Ohara Nakahara, Tobata-ku, Kitakyushu Nippon Steel Corporation Machinery & Plant Division (72) Inventor Masakazu Furuta 46-46 Nakahara, Tobata-ku, Kitakyushu 59 Nippon Steel Corporation Machinery & Plant Division (72) Inventor Fumiaki Hiura 46-59 Ohara Nakahara, Tobata-ku, Kitakyushu City Nippon Steel Corporation Machinery & Plant Division (72) Inventor Genji Fujita Tobata, Kitakyushu City 46-59 Nakahara Ward, Nippon Steel Plant Design Co., Ltd. (56) References JP-A-63-29104 (JP, A) JP-A-62-98916 (JP, U) JP-A-59-500681 (JP, A) A)
Claims (2)
に分けて供給された空気により流動状態にされた燃料を
燃焼させ、未燃成分および灰分と共に燃焼ガスを分離器
に送り、該分離器で前記未燃成分および灰分を分離して
前記流動層燃焼室に返送しながら燃料を燃焼する際、前
記２次下段空気の前記流動層燃焼室内への導入口より下
方のレベルにて、液体燃料の供給のレベル比を０．３〜
０．８とすると共に、液体燃料を液体燃料噴射ガンの軸
線と該軸線を含む鉛直面内の水平線のなす角度が、前記
水平線より下向きの５度〜２０度の液体燃料噴射ガンよ
り供給して燃焼させることを特徴とする循環流動床にお
ける液体燃料の燃焼方法。1. A fuel in a fluidized state is burned by air supplied in two stages of primary and secondary in a fluidized bed combustion chamber, and a combustion gas is sent to a separator together with unburned components and ash. When the fuel is burned while separating the unburned components and ash in the separator and returning the unburned components and ash to the fluidized bed combustion chamber, the secondary lower stage air is brought to a level lower than an inlet into the fluidized bed combustion chamber. And the level ratio of the liquid fuel supply is 0.3 to
With the 0.8, the angle of the horizon vertical plane of the liquid fuel containing the axis and said axis of the liquid fuel injection guns, the
A method of burning liquid fuel in a circulating fluidized bed, wherein the liquid fuel is supplied from a 5 to 20 degree liquid fuel injection gun directed downward from a horizontal line and burned.
に分けて供給された空気により流動状態にされた燃料を
燃焼させ、未焼成分および灰分等の循環粒子と共に燃焼
ガスを分離器に送り、該分離器で前記循環粒子を分離
し、ニューマチックバルブを経由して前記流動層燃焼室
に返送しながら燃料を燃焼する際、液体燃料を前記ニュ
ーマチックバルブの循環粒子排出側空間内に供給して燃
焼させることを特徴とする循環流動床における液体燃料
の燃焼方法。2. A fuel in a fluidized state is burned by air supplied in two stages of primary and secondary in a fluidized bed combustion chamber, and a combustion gas is produced together with circulating particles such as unburned components and ash. When the fuel is burned while being sent to a separator and separated from the circulating particles by the separator and returned to the fluidized bed combustion chamber via a pneumatic valve, the liquid fuel is supplied to a circulating particle discharge side of the pneumatic valve. A method for burning liquid fuel in a circulating fluidized bed, wherein the fuel is supplied into a space and burned.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4181371A JP2641826B2 (en) | 1992-07-08 | 1992-07-08 | Combustion method of liquid fuel in circulating fluidized bed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4181371A JP2641826B2 (en) | 1992-07-08 | 1992-07-08 | Combustion method of liquid fuel in circulating fluidized bed |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0626612A JPH0626612A (en) | 1994-02-04 |
| JP2641826B2 true JP2641826B2 (en) | 1997-08-20 |
Family
ID=16099561
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP4181371A Expired - Fee Related JP2641826B2 (en) | 1992-07-08 | 1992-07-08 | Combustion method of liquid fuel in circulating fluidized bed |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2641826B2 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE69631494T2 (en) * | 1995-04-03 | 2004-12-02 | Sharp K.K. | Image forming apparatus |
| 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 |
| US9638418B2 (en) * | 2009-05-19 | 2017-05-02 | General Electric Technology Gmbh | Oxygen fired steam generator |
| JP6183066B2 (en) * | 2013-08-29 | 2017-08-23 | 株式会社Ihi | Fluidized bed boiler |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59500681A (en) * | 1982-04-29 | 1984-04-19 | リトル、ブル−ス・リクソン | Combustion entrained by particulate droplets |
| JPS6298916U (en) * | 1985-12-10 | 1987-06-24 | ||
| JPH076609B2 (en) * | 1986-07-21 | 1995-01-30 | 三菱重工業株式会社 | Circulating fluidized bed combustion method |
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1992
- 1992-07-08 JP JP4181371A patent/JP2641826B2/en not_active Expired - Fee Related
Also Published As
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| JPH0626612A (en) | 1994-02-04 |
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