CN1011335B - 用流化床燃烧固体燃料的方法 - Google Patents

用流化床燃烧固体燃料的方法

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CN1011335B
CN1011335B CN89100176A CN89100176A CN1011335B CN 1011335 B CN1011335 B CN 1011335B CN 89100176 A CN89100176 A CN 89100176A CN 89100176 A CN89100176 A CN 89100176A CN 1011335 B CN1011335 B CN 1011335B
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fluid bed
ratio
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CN1035173A (zh
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山内康弘
荒川善久
藤间幸久
竹永清昌
日野裕一
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Mitsubishi Heavy Industries Ltd
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K3/00—Feeding or distributing of lump or pulverulent fuel to combustion apparatus
    • F23K3/02—Pneumatic feeding arrangements, i.e. by air blast
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/38—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
    • B01J8/384—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
    • B01J8/388—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
    • F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
    • F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
    • F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2206/00—Fluidised bed combustion
    • F23C2206/10—Circulating fluidised bed
    • F23C2206/101—Entrained or fast fluidised bed

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)

Abstract

改进的用流化床燃烧固体燃料的方法，减少NOx生成量，提高燃烧效率。把主回路空气、第二及第三回路空气分别从主回路空气入口、流化床上方空间的第二回路空气入口以及第二回路空气入口上方的第三回路空气入口送入。分别控制主回路、第二回路及第三回路的空气流量，使送入主回路空气、第二回路空气、第三回路空气以后，空气量与理论空气量的比分别为0.6-0.8，0.8-1.0及1.0以上。并且把喷出的煤灰重新送回流化床。

Description

本发明涉及对用流化床燃烧如煤、焦油、油页岩等固体燃料的方法的改进。
特开昭58-208509公开了一种用流化床燃烧固体燃料的方法。下面参照图6说明用流化床燃烧固体燃料的现有方法。在该图中，通过装有流动物质如砂子、生石灰等的流化床1底部的主回路空气进口，送入主回路空气，使流动物质流化，同时通过燃料进口3装入固体燃料如煤等，使它燃烧。使水或蒸汽流过流化床1里的热交换器管4来控制流化床1的温度。此外在上方空间5里安装了一个对流式热交换器6，让水或蒸汽流过该热交换器来吸收废气具有的热量。此外为了抑制NOx气体的生成量和CO气体的排放，让第二回路空气由第二回路空气入口7送入。通常为了减少CO气体的产生，流化床1是在主回路空气形成的空气量与理论空气量的比大约为1.0的条件下工作的。其理由是流化床燃烧是在800-900℃的较低温度下进行的，上方空间5的温度要低到500-700℃，因此，如果固体燃料在流化床上以1.0的低空气比值或更低的比值燃烧，那末甚至用了第二回路空气也会出现使生成的CO气体不能完全燃烧而排放到外边去的不利现象。因此，在实际工作条件下，限度是把主回路空气在流化床1里形成的空气量与理论空气量的比减小到1.0左右，从而流化床不是还原气氛，结果NOx气体的生成量增多（150-200ppm，相当于6%O2）。
要指出的是，用除尘器8或其他类似装置把从流化床飞散出来的未燃尽煤灰收集並储存在储存室9。为了提高燃烧效率，把一部分收集到的未燃烧尽煤灰通过未燃烧尽煤灰进料器10和循环管道11，以每公斤煤0.1-0.5公斤煤灰的循环比例重新送回流化床1，但是其余的未烧尽煤灰通过煤灰排放口12排出。
未烧尽煤灰在除尘器8里被分离。燃烧产生的废气经除尘器的出口13排放。
根据用现有技术的流化床燃烧固体燃烧的上述方法，一般获得下述性能：
①NOX气体的生成量为150-250ppm（相当于6%O2），
②燃烧效率为90-95%。
由现有技术的燃烧方法所能达到的上述性能水平使人不满意。
因此本发明的目的是提供一种用流化床燃烧固体燃料的改进方法，其中NOX气体的生成量少而燃烧效率高。
根据本发明的一个特征，提供了一种用流化床燃烧固体燃料的方法，该方法包括以下各个步骤：通过流化床上的主回路空气入口送入主回路空气，使流化床里的空气量与理论空气量的比大约为0.6-0.8;通过流化床上方空间的第二回路空气入口送入第二回路空气，使送入第二回路空气后空气量与理论空气量的比可到0.8-1.0左右;通过上方空间里的第二回路空气入口以上的第三回路空气入口送入第三回路的空气，使送入该空气后的空气量与理论空气量的比可达1.0或更高;以及使从流化床飞出的未燃尽煤灰重新循环回流化床。
根据本发明，由于除了以前用的第二回路空气进口外，在流化床燃烧炉的上方空间里还有第三回路空气进口，並且使由主回路空气在流化床里形成的空气量与理论空气量的比为0.6-0.8，流化床里因缺少空气而呈现出还原性燃烧，因此抑制了NOX气体的产生。通过经流化床上方空间的第二回路空气入口送入第二回路的空气，使在流化床里生成的未燃烧气体部分地燃烧，且其温度达到900-1000℃。即使在送入第二回路空气以后，该空气量与理论空气量的比才为0.8-1.0左右，这表示它是一种还原气氛。而且由于该部分的温度是900℃或900℃以上的高温，这将发生NOX气体的还原和NH3、HCN气体分解。此后，通过经过空间里第二回路空气入口上方的第三回路空气入口送入第三回路的空气，使未燃烧的CO气体燃烧，这样燃烧过程就完成了。
从流化床喷飞出的未燃尽煤灰的循环不仅提高了燃烧效率，而且由于往流化床里添进了未燃烧的碳而进一步加强了流化床里的还原气氛，因而有效地使NOX气体还原。
关于流化床里的温度，其温度越低，就越能抑制流化床里NOX气体的生成量，因此，从抑制NOX气体的产生量来看，较低温度是较好的。
结合附图通过下面对本发明一个最佳实施例的说明，可使本发明的上述和其他目的、特征和优点更显而易见。
在附图中，
图1是本发明一个最佳实施例的用流化床燃烧固体燃料的方法的示意图，
图2表示出由主回路空气形成的空气量的比值与NOX气体生成 量之间的关系曲线，
图3表示送入第二回路空气后的空气量的比与NOX生成量及与上方空间温度的关系曲线，其中主回路空气形成的空气量的比为0.7。
图4表示循环比与NOX气体生成量及与燃烧效率之间的关系曲线，其中由主回路空气形成的空气量的比为0.7，送入第二回路空气后的空气量的比为0.85。
图5表示流化床内的温度与NOX气体生成量之间的关系曲线，其中主回路空气形成的空气量的比为0.7，送入第二回路空气后的空气量的比为0.85，循环比值为1。
图6是现有技术用流化床燃烧固体燃料的方法简图。
现在参照图1按照本发明的一个最佳实施例说明用流化床燃烧固体燃料的方法。
在图1中，和图6相同的数字表示相同的作用和名称。现在参看图1。把主回路空气经过在装了流动物质（如砂子、灰石等）的流化床1的底部主回路空气进口送入，使流动物质流化，然后把如煤或其他类似固体燃料经送料口3送入。由控制装置（图中未画出）调节主回路空气的流量使流化床里的空气量与理论空气量的比大约等于0.6-0.8。
调节流过流化床1里的热交换器管道4的流体流量使流化床1里的温度保持在800-1000℃。
在流化床1里，由于空气量与理论空气量的比为0.6-0.8而呈现出还原气氛，所以生成未燃烧气体，但是经流化床1的上方空间靠下部分5a附近的第二回路空气入口7送入的第二回路空气使一 部分末燃烧气体燃烧。因此，上方空间靠下部分5a的温度大约在900-1100℃。要指出的是通过调节从第二回路空气的入口7送入的空气量使该区域的空气量与理论空气量的比达到大约0.8-1.0。
再有，为了使其余未燃烧气体（主要是CO）燃烧，把第三回路的空气经流化床1上方空间的靠上部分5b附近的第三回路空气入口送入，並且使燃烧过程在该部分完成。
要指出的是通过调节第三回路的空气流量使送入第三回路后的空气量与理论空气量的比达到1.0左右或更高。
用对流式热交换器6冷却並且从除尘器8里未燃烧尽煤灰中分离出的燃烧产生的废气从除尘器的排放口13排入大气。在除尘器8里分离出来的未燃烧尽煤灰被储存在储存室9，然后把它们以等于或大于1的循环比例经未燃烧尽煤灰加料器10和循环管道11送回流化床1，此外把与装到燃烧系统里的煤所含煤灰含量相应的煤灰经储存室9的煤灰排放口12排放到外边。
为了参照起见，将主回路空气形成的空气量与理论空气量的比和NOX生成量之间的关系曲线示于图2。正如从图2所示曲线所见，当由主回路的空气形成的空气量与理论空气量的比减小时，NOX的生成量也减少，並且当该空气量的比在0.6-0.8时，NOX的生成量最少。如果由主回路的空气形成的空气量的比进一步减小，未燃烧气体将增加，同时由于上方空间里未燃烧气体的增加，使NOX的生成量也增加。因为这个理由主回路的空气在流化床1里形成的空气量与理论空气量的比被调整在0.6-0.8左右。
图3表示出送入第二回路空气后的空气量与理论空气量的比同NOX生成量之间的关系曲线以及主回路空气量的比为0.7时送入第二回路空气后的空气量与理论空气量的比向上方空间的温度之间的关系曲线。
如由图3所示曲线所见，当送入第二回路空气后的空气量的比调 到0.8-1.0时，呈现还原性气氛的上方空间的温度要升高，并且NOX的生成会减少。
此外，图4表示未燃烧煤灰的循环比例与NOX生成量之间的关系曲线以及前者和燃烧效率之间的关系曲线。如图4所示曲线所见，增加循环比例，NOX的生成量将减少，燃烧效率增加。要指出的是循环比例等于或大于1时，各种效果几乎都达到饱和，所以循环比例要等于或大于1。
再有，图5表示流化床里的温度与NOX生成量之间的关系曲线，正如由图5所示曲线所见，由于降低了流化床的温度，所以，NOX的生成量减少了。但是如果流化床的温度降得过低，燃烧效率将变低，因此流化床的温度最好选在800-1000℃之间。
如上详细所述，按照本发明，NOX的生成量与当前燃烧方法的相比大大减少了，而且大大提高了燃烧效率。这些改进可用数字更具体地说明如下：
（1）NOX的生成量降低了而且在烧普通煤时，NOX的生成量为100ppm（6%O2）或更少些。
（2）燃烧效率提高到95-99%左右。
尽管上面用本发明的一个最佳实施例说明了本发明的原理，当然在不违背本发明实质前提下可以举出本发明的无数个不同实施例。

Claims (2)

1、一种用流化床燃烧如煤、焦油及油页岩等固体燃料的方法，包括：
把主回路空气经流化床下部的主回路空气入口送入，
把第二回路空气经流化床的上方空间里的第二回路空气入口送入，
其特征在于：
(1)使送入主回路空气后的空气量与理论空气量的比为0.6-0.8左右，
(2)使送入第二回路空气后的空气量与理论空气量的比达到0.8-1.0左右，
(3)把第三回路的空气经该上方空间里的第二回路入口以上的第三回路空气入口送入，使送入第三回路空气后的空气量与理论空气量的比等于或大于1.0。
2、一种如权利要求1的燃烧固体燃料的方法，其特征是把从流化床飞散出的未燃烧尽煤灰重新送回流化床。
CN89100176A 1988-01-12 1989-01-12 用流化床燃烧固体燃料的方法 Expired CN1011335B (zh)

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JP63003085A JP2637449B2 (ja) 1988-01-12 1988-01-12 流動床燃焼方法
JP3085/88 1988-01-12

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CN1011335B true CN1011335B (zh) 1991-01-23

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JP2637449B2 (ja) 1997-08-06
KR920001094B1 (ko) 1992-02-01
CN1035173A (zh) 1989-08-30
AU591621B2 (en) 1989-12-07
JPH01181005A (ja) 1989-07-19
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