WO2015014233A1 - 一种带二次再热的循环流化床锅炉 - Google Patents

一种带二次再热的循环流化床锅炉 Download PDF

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Publication number
WO2015014233A1
WO2015014233A1 PCT/CN2014/082913 CN2014082913W WO2015014233A1 WO 2015014233 A1 WO2015014233 A1 WO 2015014233A1 CN 2014082913 W CN2014082913 W CN 2014082913W WO 2015014233 A1 WO2015014233 A1 WO 2015014233A1
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WO
WIPO (PCT)
Prior art keywords
furnace
flue
reheater
fluidized bed
circulating fluidized
Prior art date
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PCT/CN2014/082913
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English (en)
French (fr)
Inventor
聂立
苏虎
周棋
巩李明
黄敏
杨雪芬
尹莉
梁红伟
鲁佳易
Original Assignee
东方电气集团东方锅炉股份有限公司
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Publication of WO2015014233A1 publication Critical patent/WO2015014233A1/zh

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K7/00—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating
    • F01K7/16—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating the engines being only of turbine type
    • F01K7/22—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating the engines being only of turbine type the turbines having inter-stage steam heating
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B31/00—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus
    • F22B31/0007—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus with combustion in a fluidized bed
    • F22B31/0015—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus with combustion in a fluidized bed for boilers of the water tube type
    • F22B31/003—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus with combustion in a fluidized bed for boilers of the water tube type with tubes surrounding the bed or with water tube wall partitions
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B31/00—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus
    • F22B31/0007—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus with combustion in a fluidized bed
    • F22B31/0084—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus with combustion in a fluidized bed with recirculation of separated solids or with cooling of the bed particles outside the combustion 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
    • 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

Definitions

  • the invention relates to a circulating fluidized bed boiler, in particular to a circulating fluidized bed boiler with secondary reheating.
  • Circulating fluidized bed combustion technology is the only low-grade fuel efficient clean combustion utilization technology developed in the past 30 years, which is commercialized and large-scale at present. With its unparalleled low pollutant emission advantages, it effectively solves energy conservation and environmental protection. Two issues represent a major advancement in today's combustion technology.
  • the circulating fluidized bed boiler has encountered great difficulties in further improving the power generation efficiency of the unit. This is because, under the rated load of the circulating fluidized bed boiler, the normal combustion temperature in the furnace usually does not exceed 930 ° C. Compared with other combustion methods such as pulverized coal boilers or cyclone furnaces, the combustion temperature is low, and the combustion temperature is high.
  • the problem of the parameter heating surface metal material leads to a large bottleneck in further improving the steam parameters; if the number of reheating is increased, the arrangement position of the heating surface needs to be considered, and the pulverized coal boiler has a secondary reheating heating surface arranged at The precedent in the horizontal flue of the furnace exit with high smoke temperature, but due to the difference in gas-solid two-phase flow, the flue gas at the furnace exit of the circulating fluidized bed boiler carries a large amount of solid particles, and the flue gas velocity can be as high as about 30 m/ s, if the secondary reheating surface is arranged in this area, the wear is inevitably serious, making the boiler difficult to operate safely; if the secondary reheater is completely disposed in the tail flue, other heating surfaces are arranged in the tail flue, The heat absorption share of the heated surface is difficult to adjust synchronously, and it is difficult to arrange in temperature adjustment.
  • the secondary reheat steam pressure is lower than the primary reheat steam pressure, so that the secondary reheat steam pressure loss is not excessive, a lower steam flow rate is required, however, the low steam flow rate is also
  • the cooling capacity of the steam on the wall of the heating surface is very limited, that is, the wall temperature of the heating surface tube is closer to the temperature of the medium outside the tube. Therefore, in consideration of the heat carrying capacity of the tube on the heating surface, the steam flow rate cannot be taken too low. It is difficult to balance; at the same time, in the process of starting the boiler, in order to protect the reheater from overheating and dry burning, the reheater is often protected by means such as introduction of main steam cooling.
  • the introduction of the secondary reheater increases the area of the reheating heat receiving surface, so that the heat absorption share of the reheater exceeds the heat absorption share of the superheater.
  • the steam amount is difficult to meet and protects the primary reheater and the secondary reheater; the above limits the combination of secondary reheating and circulating fluidized bed combustion technology, making it more difficult to achieve further improvement in the efficiency of the circulating fluidized bed boiler unit.
  • the object of the present invention is to provide a circulating fluidized bed boiler with secondary reheating, which is not significant, in view of the above-mentioned deficiencies in the prior art and overcoming the difficulties of combining the above secondary reheating with a circulating fluidized bed boiler.
  • the heat transfer intensity and heat utilization rate in the furnace can be effectively improved, thereby achieving an effective combination of secondary reheating and circulating fluidized bed boilers, thereby achieving the purpose of further improving the cogeneration of power generation efficiency and low pollutant emissions of coal power units. And to ensure long-term efficient operation of the equipment.
  • a circulating fluidized bed boiler with secondary reheating of the present invention comprises a plenum, an air distribution device including a wind deflector and a hood, a furnace, a primary air system, a secondary air system, and a horizontal smoke. a channel, at least three cyclones, at least three external heat exchangers, a tail flue, and a water wall with upper and lower headers in the furnace, wherein a shrinkage ratio of the lower portion of the furnace in the depth direction is 0. 2-0.
  • the tail flue adopts a parallel multi-flue structure, comprising at least two parallel flue pipes, each flue is provided with a flue gas regulating baffle, and the flue gas in at least one parallel flue
  • the regulating baffle is provided with a low temperature superheater before the flow direction of the flue gas
  • the flue gas regulating baffle in at least the other parallel flue is provided with a low temperature reheater before the flow direction of the flue gas
  • all the flue gas baffles are along the smoke Economizer and air preheater are arranged in the tail flue after the gas flow direction
  • the furnace can be a single furnace, and a ventilation panel is arranged at the lower part thereof, and a plurality of hoods are arranged on the air distribution panel.
  • the above furnace can also adopt a single furnace double cloth wind plate structure, and the lower part is provided with two air distribution plates, and each air distribution plate is provided with several hoods.
  • the furnace can also be an annular furnace, and a lower portion of the furnace is provided with an annular air distribution plate, and the air distribution plate is provided with a plurality of hoods.
  • the boiler steam with a certain degree of superheat flows out of the water wall and then flows through the low temperature superheater, the intermediate temperature superheater and the high temperature superheater, and enters the steam turbine high pressure cylinder to work; the steam from the high pressure cylinder of the steam turbine flows through the low temperature one after another.
  • the steam After the heat exchanger and the high temperature reheater, the steam enters the first intermediate cylinder of the steam turbine to work; the steam from the first intermediate cylinder of the steam turbine flows through the secondary low temperature reheater and the secondary high temperature reheater, and then enters the steam turbine in turn.
  • the second intermediate pressure cylinder and the low pressure cylinder of the steam turbine work;
  • the singularity of the lower part of the furnace is controlled to 0. 2-0. 49, at one time, in the present invention, the shrinkage ratio of the lower part of the furnace is controlled to 0. 2-0.
  • the dragging and entraining ability of the particles in the furnace is stronger, the particle concentration in the upper part of the furnace can be increased, and the convective heat transfer intensity of the gas-solid two-phase flow in the upper part of the furnace is increased.
  • the heat absorption at the soda side is improved, and the need to introduce the secondary reheat heating surface into the circulating fluidized bed boiler is satisfied.
  • the large contraction ratio structure makes the primary air volume account for a smaller share of the total air volume, and the secondary air volume accounts for a larger share of the total air volume, providing a more favorable adjustment range for the secondary air volume adjustment.
  • the low temperature superheater and the primary low temperature reheater are disposed in the parallel flue before the flue gas baffle flows along the direction of the flue gas flow, and the particle concentration is low relative to the furnace, so the heat transfer intensity and the heating surface are The degree of wear is also lower than in the furnace, which reduces the grade of steel. In this way, not only the material cost is saved, but also the excessive heating surface is set in the furnace to greatly reduce the local flue gas temperature in the furnace, which can prevent the local smoke temperature from falling below the fuel ignition point and is not conducive to fuel burnout.
  • the medium temperature superheater, the primary high temperature reheater, the secondary low temperature reheater and the secondary high temperature reheater are all arranged in the external heat exchanger, and the external heat exchanger is highly propagated due to the internal bubbling fluidized bed.
  • the thermal strength characteristics make the temperature of the heated surface tube closer to the particle temperature.
  • the high heat transfer intensity in the integrated furnace and the high heat transfer strength characteristic of the bubbling fluidized bed in the external heat exchanger will satisfy the secondary reheating. Steam parameters are required.
  • the steam of the superheater, the primary reheater and the secondary reheater is adjusted by adjusting the opening degree of each group of flue gas regulating baffles and the ratio of different temperature ash flow rates of the external heat exchangers to and from the external heat exchanger.
  • the temperature is independently adjusted, and the steam parameters of the heating surfaces at all levels are guaranteed, while the efficiency of the unit is not reduced, and the economizer and the air preheater are normally operated; in addition, the secondary low temperature reheater and the secondary high temperature reheater are arranged.
  • the steam switching of the secondary reheater at each stage can be greatly facilitated, and the heating surface of the secondary reheater can be effectively protected during the low load operation and start-stop process of the boiler, avoiding the secondary reheater Dry burning to ensure the normal operation of the equipment;
  • the inner diameter of the secondary high temperature reheater is at least 1. 7 mm larger than the inner diameter of the secondary low temperature reheater ; this is because the secondary reheat steam pressure is more than the primary reheat steam pressure.
  • a lower steam flow rate is required.
  • the low steam flow rate also makes the cooling capacity of the steam to the wall of the heated surface very limited, that is, the wall temperature of the heated surface tube is closer to the temperature of the medium outside the tube, so the steam flow rate cannot be considered in consideration of the heat carrying capacity of the tube on the heated surface. Take too low.
  • the inner diameter of the tube of the secondary reheater is as above, so that the steam flow rate of the two places is relatively high.
  • the obvious difference can meet the needs of both sides.
  • the 5% -2% of the efficiency of the unit can be further increased on the basis of the existing large-scale circulating fluidized bed boiler;
  • the high temperature superheater can be a U-shaped screen type superheater; facilitating heat exchange with the flue gas in the central portion of the furnace having a higher temperature, and improving heat exchange efficiency;
  • the invention can effectively improve the heat transfer intensity in the furnace without significantly increasing the fuel, and cooperate with the preferred heating surface arrangement to realize the effective combination of the secondary reheating and the circulating fluidized bed boiler, thereby improving
  • the purpose of coal-fired power generation coexistence with low-emission emissions is to ensure the long-term efficient operation of the equipment.
  • FIG. 1 is a schematic structural view of Embodiment 1 of the present invention.
  • FIG. 2 is a schematic structural view of a second embodiment of the present invention.
  • Figure 3 is a left side view of Figure 2.
  • FIG. 4 is a schematic top plan view of a third embodiment of the present invention.
  • this embodiment is a circulating fluidized bed boiler with secondary reheating, including a plenum 14, a single furnace 11, a ventilating panel 15 and a plurality of hoods (not shown).
  • the device the primary air system with the fan 16 and the air duct, the secondary air system with the fan 17 and the air duct, the horizontal flue 18, the three cyclones 1, the three external heat exchangers 2, the tail smoke Lane 3, the cyclone separator 1 is connected to the horizontal flue 18, the tail flue 3 and the lower portion of the furnace 11, and the two ends of the three external heat exchangers 2 are respectively connected to the respective cyclone 1 and the lower portion of the furnace 11, the furnace
  • the circumference of the 11 and the top of the furnace are composed of a water-cooling wall 19 with upper and lower headers, and the contraction ratio of the lower part of the furnace 11 in the depth direction (ie, L1/L2 in the figure) is 0.3;
  • An economizer 13 and an air preheater 21 are provided, which are provided in a parallel flue 20
  • the temperature superheater 4 is provided with a low temperature reheater 7 in another parallel flue 20, and other heating surfaces in the remaining parallel flue 20; and an intermediate temperature heat exchanger 2 is provided in an external heat exchanger 2 5, in the other external heat exchanger 2 is provided a primary high temperature reheater 8, in the other external heat exchanger 2 is provided with a secondary low temperature reheater 9 and a secondary high temperature reheater 10;
  • a high temperature superheater 6 is arranged in the furnace 11; the upper header of the water wall 19, the low temperature superheater 4, the intermediate temperature superheater 5 and the high temperature superheater 6 are sequentially connected through the pipeline, and the primary low temperature reheater 7 and the high temperature reheating
  • the device 8 is connected through a pipeline, and the secondary low temperature reheater 9 is connected to the secondary high temperature reheater 10 through a pipeline.
  • the boiler steam with a certain degree of superheat flows out of the water wall 19 and then flows through the low temperature superheater 4, the intermediate temperature superheater 5 and the high temperature superheater 6 to enter the steam turbine high pressure cylinder to work;
  • the steam from the steam turbine high pressure cylinder flows sequentially After a low temperature reheater 7 and a high temperature reheater 8, the steam enters the first intermediate cylinder of the steam turbine to work;
  • the steam from the first intermediate cylinder of the steam turbine flows through the secondary low temperature reheater 9 and the secondary high temperature.
  • the heater 10 and then enters the second intermediate cylinder of the steam turbine and the low pressure cylinder of the steam turbine to perform work;
  • the particles in the furnace of the circulating fluidized bed boiler are towed by gas.
  • the required wind pressure of the furnace is approximately equal to the weight of the particles in the furnace, that is, the stock of materials per unit area, which can be expressed in pressure units. Calculated by the particle concentration in this area.
  • the heat transfer in the furnace is mainly the convective heat transfer between the gas-solid two-phase fluid and the heated surface. This convective heat transfer is related to the concentration of solid particles. The higher the concentration of solid particles, the higher the heat transfer effect. Well, the higher the heat transfer intensity.
  • the invention increases the total heat transfer amount due to the addition of the secondary reheat heating surface, so it is necessary to ensure a high heat transfer intensity in the furnace, that is, a higher particle concentration is required in the upper portion of the furnace; and since the power of the supporting material comes from The fan head, in order to increase the energy consumption of the fan at least can not exceed the energy saving of the secondary reheat system to improve the efficiency of the unit, it is necessary to maintain the particle concentration at a reasonable level. 5 ⁇
  • the shrinkage ratio of the lower part of the furnace in the depth direction of the present embodiment is 0. 5-0. 7, the shrinkage ratio of the lower part of the furnace in the depth direction is 0.3, the two fans 16, 17 can be changed in the indenter Under small conditions, the drag effect on the particles in the furnace 1 1 is more obvious.
  • the particle concentration in the upper part of the furnace can be significantly increased, and the pressure drop per unit height in the furnace exit area and the average unit height drop of the furnace (bed)
  • the ratio of the ratio of lamination to the height of the furnace (usually between 0.2 and 0.5) is increased by about 0.1, thereby increasing the heat transfer intensity in the furnace and meeting the need for secondary reheating of the heated surface.
  • the low temperature superheater 4 and the primary low temperature reheater 7 are both disposed in the parallel flue 20 of the flue gas baffle 12 in the flow direction of the flue gas, and the particle concentration is low relative to the furnace 11, so the heat transfer intensity and the heating surface are The degree of wear is also lower than in the furnace, which reduces the grade of steel. In this way, not only the material cost is saved, but also the excessive heating surface is set in the furnace to greatly reduce the local flue gas temperature in the furnace, and the local smoke temperature can be prevented from falling below the fuel ignition point, which is not conducive to fuel burnout.
  • the intermediate temperature superheater 5, the primary high temperature reheater 8, the secondary low temperature reheater 9 and the secondary high temperature reheater 10 are all disposed in the external heat exchanger 2, and the high heat transfer intensity and the external furnace are integrated.
  • the high heat transfer strength characteristics of the bubbling fluidized bed within the heat exchanger 2 will meet the steam parameter requirements for achieving secondary reheat.
  • the amount of flue gas of each parallel flue 20 can be adjusted, thereby adjusting the heat absorption share of the low temperature superheater 4 and the primary low temperature reheater 7, and adjusting to enter the external heat exchange.
  • the flow rate of solid particles at different temperatures in the device 2 can adjust the steam temperature of the secondary reheater, so that the steam temperatures of the different heating surfaces are independently adjusted, that is, the steam parameters of the heating surfaces at all levels are ensured, and the unit efficiency is not reduced.
  • the secondary low temperature reheater 9 and the secondary high temperature reheater 10 are arranged in the external heat exchanger 2, which can greatly facilitate the steam switching of the secondary reheater system, and is effective in the low load operation and start and stop process of the boiler.
  • Protect the heating surface of the secondary reheater avoid dry burning of the secondary reheater, and ensure the normal operation of the equipment;
  • the secondary low temperature reheater 9 with smaller inner diameter makes the steam flow rate higher, which can effectively cool the heating surface pipe in the area.
  • the temperature of the secondary high-temperature reheater 10 with a larger inner diameter is slower, so that the steam pressure loss of the secondary reheater can be kept at a low level, so that the pressure and temperature of the secondary reheat steam are both Guaranteed.
  • the introduction of the secondary reheating of the present invention can further increase the efficiency of the unit by 1.5%-2%;
  • the difference between this embodiment and the first embodiment is that the furnace 26 is a single furnace double cloth wind plate structure, and the lower part is provided with two air distribution plates 22 and two air distribution plates 22
  • Each of the furnaces 26 is provided with a plurality of hoods (not shown), and a lower ratio of the lower portion of the furnace 26 in the depth direction (ie, L3/L4 in the figure) is 0.20, and three cyclones 1 are disposed on each side of the furnace 26 and Three external heat exchangers 2, in which two intermediate heat exchangers 2 are provided with a medium temperature superheater 5, and in the other two external heat exchangers 2, a high temperature reheater 8 is provided, in another The secondary heat exchanger 2 is provided with a secondary low temperature reheater 9, and in the other external heat exchanger 2, a secondary high temperature reheater 10 is provided; the secondary low temperature reheater 9 has an inner diameter of 46 mm. The inner diameter of the tube used in the secondary high temperature reheater 10 is 48 mm.
  • the working principle of this embodiment is similar to that of the first embodiment.
  • the shrinkage ratio of the lower part of the furnace 26 in the depth direction is 0.2, the pressure drop per unit height of the furnace exit area and the average unit height drop of the furnace (bed lamination drop and furnace height)
  • the ratio of the ratio (usually between 0.2 and 0.5) is further increased by about 0.13, so that the secondary reheating can be effectively combined with the circulating fluidized bed boiler of the furnace structure to improve the power generation efficiency and low pollutant of the coal-fired power unit. Emissions coexist for the purpose of ensuring long-term efficient operation of the equipment.
  • the difference between this embodiment and the second embodiment is that the furnace 27 is an annular furnace, and the lower portion is provided with an annular air distribution plate, and the air distribution plate is provided with a plurality of hoods; 27
  • the ratio of the lower part of the lower direction in the depth direction is 0.49, the ratio of the pressure drop per unit height in the furnace exit area to the average unit height pressure drop of the furnace (the ratio of the bed lamination drop to the furnace height) (usually between 0.2 and 0.5) and then increased by about 0.06, thereby increasing the heat transfer intensity in the furnace and meeting the needs of the secondary reheating surface.
  • the present invention increases the particle concentration in the upper portion of the furnace to a reasonable level by changing the shrinkage ratio of the lower portion of the furnace in the depth direction, and the pressure drop per unit height in the furnace outlet region and the average unit height pressure drop in the furnace (bed lamination)
  • the ratio of the ratio of the drop to the height of the furnace (usually between 0.2 and 0.5) is increased by about 0.05 to 0.15, without increasing the fuel. It can effectively improve the heat transfer intensity in the furnace, and cooperate with the preferred heating surface arrangement and the inner diameter of the secondary reheater tubes to achieve an effective combination of secondary reheating and circulating fluidized bed boilers.
  • the purpose of co-existing power generation efficiency and low pollutant emissions is to ensure long-term and efficient operation of the equipment.

Abstract

一种带二次再热的循环流化床锅炉，包括风室（14）、布风装置、炉膛（11）、一次风系统、二次风系统、水平烟道（18）、数台旋风分离器（1）和外置式热交换器（2）、以及尾部烟道（3）。炉膛（11）下部的收缩比为0.2-0.49。尾部烟道（3）内设烟气挡板（12）,尾部烟道（3）包含至少两条平行烟道（20）,在一平行烟道（20）内设有低温过热器（4）,在另一平行烟道（20）内设有一次低温再热器（7）；在至少一外置式热交换器（2）内设有中温过热器（5），在至少一外置式热交换器（2）内设有一次高温再热器（8），在至少一外置式热交换器（2）内设有二次低温再热器（9）和二次高温再热器（10）。在炉膛（11）上部设有高温过热器（6）。该锅炉将二次再热与循环流化床锅炉有效结合并提高了炉内传热强度。

Description

种带二次再热的循环流化床锅炉 技术领域
本发明涉及一种循环流化床锅炉， 特别是带二次再热的循环流化床锅炉。
背景技术
我国现已成为世界第一的能源生产国和消费国， 近十年煤炭在能源结构中所占比重一直 在 70%左右， 并预计将持续至本世纪中叶。 然而， 我国煤炭资源中， 高硫份和高灰份的劣质 煤所占比重较高， 为此， 提高机组发电效率， 降低污染物排放是电力行业的中心任务。
循环流化床燃烧技术是近三十年发展起来的在现阶段唯一实现商业化和大型化的低品位 燃料高效清洁燃烧利用技术， 以其无与伦比的低污染物排放优势， 有效解决了节能与环保两 方面的问题， 代表了当今燃烧技术的一大进步。
目前， 提高蒸汽参数、 增加再热次数是提高机组发电效率的有效方法， 但循环流化床锅 炉在进一步提高机组发电效率方面遇到较大的困难。 这是因为， 循环流化床锅炉在额定负荷 下， 炉内正常燃烧温度通常不超过 930°C， 相对于其它燃烧方式如煤粉锅炉或旋风燃烧炉等 锅炉， 其燃烧温度偏低， 加之高参数受热面金属材料的问题， 导致在进一步提高蒸汽参数方 面遇到较大的瓶颈； 若增加再热次数， 则需考虑受热面的布置位置， 煤粉锅炉有将二次再热 受热面布置在烟温较高的炉膛出口水平烟道内的先例， 但由于气固两相流动上的差异， 循环 流化床锅炉的炉膛出口处烟气携带大量的固体颗粒， 且烟气速度可高达约 30m/s， 若此区域 布置二次再热受热面， 其磨损必然严重， 使得锅炉难于安全运行； 如将二次再热器全布置在 尾部烟道内， 则由于尾部烟道内还布置其它受热面， 各受热面的吸热份额难于同步调节， 在 气温调节上难于布置。 此外， 更为重要的是， 二次再热蒸汽压力比一次再热蒸汽压力更低， 为使二次再热蒸汽压力损失不致过大， 需要采用较低的蒸汽流速， 然而， 低蒸汽流速也使蒸 汽对受热面管壁的冷却能力非常有限， 即受热面管子壁温更接近于管外介质的温度， 因此为 考虑受热面管子的热承载能力， 又不能将蒸汽流速取的过低， 二者难以平衡； 同时， 在锅炉 启动过程中， 为保护再热器不致超温干烧， 往往会采用如引入主蒸汽冷却等方法保护再热 器。 二次再热器的引入增加了再热受热面面积， 使再热器的吸热份额超过了过热器的吸热份 额， 在采取主蒸汽冷却时， 将需要更多的蒸汽量， 即原有蒸汽量难于满足同时保护一次再热 器和二次再热器； 以上均限制了二次再热与循环流化床燃烧技术的结合， 使循环流化床锅炉 机组效率的进一步提高难于实现。
发明内容
本发明的目的是针对现有技术存在的上述不足并克服上述二次再热与循环流化床锅炉相 结合的难点， 提供一种带二次再热的循环流化床锅炉， 它在不显著增加燃料的情况下能有效 提高炉内传热强度和热量利用率， 从而实现二次再热与循环流化床锅炉的有效结合， 达到进 一步提高煤电机组发电效率与低污染物排放共存的目的， 且保证设备长期高效运行。
为达到上述目的， 本发明的一种带二次再热的循环流化床锅炉， 包括风室、 包含布风板 和风帽的布风装置、 炉膛、 一次风系统、 二次风系统、 水平烟道、 至少三台旋风分离器、 至 少三台外置式热交换器、 尾部烟道， 炉膛内设有带上、 下集箱的水冷壁， 其特征在于所述炉 膛下部沿深度方向的收缩比为 0. 2-0. 49 ; 所述尾部烟道采用平行多烟道结构， 至少包含两 条平行烟道， 每条烟道内设有烟气调节挡板， 在至少一平行烟道内的烟气调节挡板沿烟气流 动方向之前设有低温过热器， 在至少另一平行烟道内的烟气调节挡板沿烟气流动方向之前设 有一次低温再热器， 在所有烟气挡板沿烟气流动方向之后的尾部烟道内布置省煤器和空预 器； 在至少一外置式热交换器内设有中温过热器， 在至少一外置式热交换器内设有一次高温 再热器， 在至少一外置式热交换器内设有二次低温再热器， 在至少一外置式热交换器内设有 二次高温再热器； 在炉内设有高温过热器； 水冷壁的上集箱、 低温过热器、 中温过热器和高 温过热器通过管路依次连通， 一次低温再热器与一次高温再热器通过管路连通， 二次低温再 热器与二次高温再热器通过管路连通。
上述炉膛可以为单炉膛， 其下部设有一布风板， 布风板上设有数个风帽。
上述炉膛也可以采用单炉膛双布风板结构， 其下部设有两布风板， 每块布风板上设有数个 风帽。
上述炉膛也可以为环形炉膛， 其下部设有环形的布风板， 该布风板上设有数个风帽。 使用时， 已有一定过热度的锅炉蒸汽从水冷壁出来后依次流经低温过热器、 中温过热器和 高温过热器， 进入汽轮机高压缸做功； 从汽轮机高压缸出来的蒸汽依次流经一次低温再热器 和一次高温再热器后进入汽轮机第一中压缸做功； 从汽轮机第一中压缸出来的蒸汽又依次流 经二次低温再热器和二次高温再热器， 之后依次进入汽轮机第二中压缸和汽轮机低压缸做 功；
为实现二次再热与循环流化床燃烧技术的有效结合， 需考虑传热强度、 受热面布置位置、 汽温调节与受热面保护等方面因素：
在炉内传热方面， 对于循环流化床锅炉而言， 由于承托燃料及床料颗粒的动力来自风机 压头， 为使风机能耗的增量至少不能超过二次再热系统使机组效率提高的能耗节约量， 因此 需要将颗粒浓度维持在合理水平。 相比于目前循环流化床锅炉炉膛下部炉膛深度方向的收缩 比通常为 0. 5-0. 7， 本发明将炉膛下部沿深度方向的收缩比控制为 0. 2-0. 49， 在一次风机和 二次风机压头变化不大的条件下， 对炉内颗粒的拖曳及夹带能力更强， 可提高炉膛上部区域 的颗粒浓度， 从而增加炉膛上部区域气固两相流的对流传热强度， 使得汽水侧吸热量得以提 高， 满足二次再热受热面引入循环流化床锅炉的需要。 且大收缩比结构使得一次风量占总风 量份额更小， 二次风量占总风量份额更大， 为二次风的风量调节提供了更宽裕的调节范围。
在受热面布置方面， 低温过热器和一次低温再热器均设于烟气挡板沿烟气流动方向之前 的平行烟道内， 相对于炉膛， 此处颗粒浓度低， 因此传热强度和受热面磨损程度也低于炉 内， 可降低钢材等级。 这样， 既节约材料成本， 又避免在炉内设置过多受热面而大幅拉低炉 内局部烟气温度的情况发生， 可防止局部烟温降至燃料着火点以下而不利于燃料燃尽的现象 出现； 中温过热器、 一次高温再热器、 二次低温再热器和二次高温再热器均布置于外置式热 交换器内， 外置式换热器由于其内部鼓泡流化床的高传热强度特性而使受热面管子温度更接 近于颗粒温度， 综合炉内的高传热强度和外置式热交换器内鼓泡流化床的高传热强度特性将 满足可实现二次再热的蒸汽参数需要。
在汽温调节方面， 通过调节各组烟气调节挡板的开度与进出外置式热交换器不同温度灰 流量比例的共同作用， 使过热器、 一次再热器与二次再热器的蒸汽温度分别独立调节， 在各 级受热面蒸汽参数得到保证的同时， 不降低机组效率， 又保证省煤器和空预器正常工作； 此 外， 二次低温再热器和二次高温再热器布置在外置式热交换器内， 可极大的方便各级二次再 热器的蒸汽切换， 在锅炉低负荷运行及启停过程中可有效保护二次再热器受热面， 避免二次 再热器的干烧， 保证设备的正常运行；
作为本发明的进一步改进， 所述二次高温再热器的管子内径至少比二次低温再热器的管子 内径大 1. 7mm; 这是因为二次再热蒸汽压力比一次再热蒸汽压力更低， 为使二次再热蒸汽压 力损失不致过大， 需要采用较低的蒸汽流速。 然而， 低蒸汽流速也使蒸汽对受热面管壁的冷 却能力非常有限， 即受热面管子壁温更接近于管外介质的温度， 因此为考虑受热面管子的热 承载能力， 又不能将蒸汽流速取的过低。 通过核算受热面管内工质的压力损失与管子所处环 境温度以及管子所能承受换热能力等多方面因素， 对二次再热器的管子内径做如上要求， 使 得两处的蒸汽流速有较为明显差别， 可同时满足两方面的需要。 本发明能实现二次再热与循环流化床锅炉的有效结合， 可在现有大型循环流化床锅炉的基 础上将机组效率再提高 1. 5%-2%；
作为本发明的进一步改进， 所述高温过热器可为 U型屏式过热器； 便于与温度较高的炉 膛中心区域的烟气换热， 提高换热效率；
综上所述， 本发明在不显著增加燃料的情况下能有效提高炉内传热强度， 并配合优选的 受热面布置方式以实现二次再热与循环流化床锅炉有效结合， 从而达到提高煤电机组发电效 率与低污染物排放共存的目的， 且保证设备长期高效运行。
附图说明
图 1为本发明实施例一的结构示意图。
图 2为本发明实施例二的结构示意图。
图 3为图 2的左视图。
图 4为本发明实施例三的俯视结构示意图。
具体实施方式
下面结合附图对本发明作进一步详细的说明。
实施例一
如图 1所示， 该实施例为带二次再热的循环流化床锅炉， 包括风室 14、 单炉膛 11、 设有 单布风板 15和数个风帽 （未示出） 的布风装置、 设有风机 16和风管的一次风系统、 设有风 机 17和风管的二次风系统、 水平烟道 18、 三台旋风分离器 1、 三台外置式热交换器 2、 尾 部烟道 3， 旋风分离器 1连接水平烟道 18、 尾部烟道 3和炉膛 11的下部， 三台外置式热交 换器 2的两端分别与各自的旋风分离器 1和炉膛 11的下部相连， 炉膛 11的四周及炉顶由带 上、 下集箱的水冷壁 19 组成， 所述炉膛 11 下部沿深度方向的收缩比 （即图中 L1/L2 ) 为 0. 3; 所述尾部烟道 3 内设有三组烟气挡板 12， 烟气挡板 12沿烟气流动方向之前的尾部烟 道 3包含三条平行烟道 20， 在烟气挡板 12沿烟气流动方向之后的尾部烟道 3内设有省煤器 13和空预器 21， 在一平行烟道 20 内设有低温过热器 4， 在另一平行烟道 20 内设有一次低 温再热器 7， 在所剩的平行烟道 20 内设有其他受热面； 在一外置式热交换器 2 内设有中温 过热器 5， 在另一外置式热交换器 2内设有一次高温再热器 8， 在另一外置式热交换器 2内 设有二次低温再热器 9和二次高温再热器 10; 在炉膛 11内设有高温过热器 6; 水冷壁 19的 上集箱、 低温过热器 4、 中温过热器 5和高温过热器 6通过管路依次连通， 一次低温再热器 7与一次高温再热器 8通过管路连通， 二次低温再热器 9与二次高温再热器 10通过管路连 通， 二次低温再热器 9所采用的管子内径为 48mm， 二次高温再热器 10所采用的管子内径 为 52.5mm。
使用时， 已有一定过热度的锅炉蒸汽从水冷壁 19 出来后依次流经低温过热器 4、 中温过 热器 5和高温过热器 6， 进入汽轮机高压缸做功； 从汽轮机高压缸出来的蒸汽依次流经一次 低温再热器 7和一次高温再热器 8后进入汽轮机第一中压缸做功； 从汽轮机第一中压缸出来 的蒸汽又依次流经二次低温再热器 9 和二次高温再热器 10， 之后依次进入汽轮机第二中压 缸和汽轮机低压缸做功；
循环流化床锅炉炉膛内颗粒由气体拖曳而起， 按照流态化理论及实践证明， 炉膛所需风 压近似等于炉内颗粒重量， 即单位面积上的物料存量， 可用压力单位表示， 并可通过该区域 颗粒浓度来计算。 对于循环流化床锅炉而言， 炉内传热主要为气固两相流体与受热面间的对 流传热， 这种对流传热与固体颗粒浓度有关， 固体颗粒浓度越高， 传热效果越好， 传热强度 越高。 本发明由于二次再热受热面的加入， 总的传热量增加， 因此需保证炉内较高的传热强 度， 即炉膛上部区域需要有较高的颗粒浓度； 同时由于承托物料的动力来自风机压头， 而为 使风机能耗的增量至少不能超过二次再热系统使机组效率提高的能耗节约量， 因此需要将颗 粒浓度维持在合理水平。 相比于目前循环流化床锅炉炉膛下部的收缩比为 0. 5-0. 7， 本实施例炉膛下部沿深度方 向的收缩比为 0. 3， 可使两风机 16、 17在压头变化不大的条件下， 对炉膛 1 1 内颗粒的拖曳 效果更明显， 在实际工作时可显著提高炉膛上部区域的颗粒浓度， 将炉膛出口区域单位高度 的压降与炉膛平均单位高度压降 （床层压降与炉膛高度之比） 的比值 （通常在 0.2〜0.5 之 间） 再提高约 0.1， 从而增加了炉内的传热强度， 可满足二次再热受热面布置的需要。
低温过热器 4和一次低温再热器 7均设于烟气挡板 12沿烟气流动方向之前的平行烟道 20 内， 相对于炉膛 11， 此处颗粒浓度低， 因此传热强度和受热面磨损程度也低于炉内， 可 降低钢材等级。 这样， 既节约材料成本， 又避免在炉内设置过多受热面而大幅拉低炉内局部 烟气温度的情况发生， 并可防止局部烟温降至燃料着火点以下而不利于燃料燃尽的现象出 现； 中温过热器 5、 一次高温再热器 8、 二次低温再热器 9和二次高温再热器 10均设于外置 式热交换器 2内， 综合炉内的高传热强度和外置式热交换器 2内鼓泡流化床的高传热强度特 性将满足可实现二次再热的蒸汽参数需要。
通过调节各组烟气挡板 12 的开度， 可调节各平行烟道 20的烟气量， 从而调节低温过热 器 4、 一次低温再热器 7的吸热份额， 通过调节进入外置式热交换器 2内不同温度的固体颗 粒流量可以调节二次再热器的蒸汽温度， 从而使不同受热面的汽温均独立调节， 即在各级受 热面蒸汽参数得到保证的同时， 不降低机组效率。 二次低温再热器 9 和二次高温再热器 10 布置在外置式热交换器 2内， 可极大的方便二次再热器系统的蒸汽切换， 在锅炉低负荷运行 及启停过程中有效保护二次再热器受热面， 避免二次再热器的干烧， 保证设备的正常运行； 内径较小的二次低温再热器 9使得蒸汽流速较高， 可有效冷却该区域受热面管子的温度， 内 径较大的二次高温再热器 10 内蒸汽流速较慢， 可使二次再热器的蒸汽压力损失维持在很低 的水平， 从而使得二次再热蒸汽的压力和温度均有所保证。 与同蒸汽参数的一次再热循环流 化床锅炉机组相比， 本发明引入二次再热可将机组效率再提高 1. 5%-2%；
实施例二
如图 2、 图 3所示， 该实施例与实施例一相比， 其差别仅在于：其炉膛 26为单炉膛双布风 板结构， 下部设有两布风板 22， 两布风板 22上各设有数个风帽 （未示出）， 所述炉膛 26下 部沿深度方向的收缩比 （即图中 L3/L4) 为 0. 20， 在炉膛 26两侧各设有三台旋风分离器 1 和三台外置式热交换器 2， 在其中的两外置式热交换器 2 内设有中温过热器 5， 在另两外置 式热交换器 2 内设有一次高温再热器 8， 在另一外置式热交换器 2 内设有二次低温再热器 9， 在另一外置式热交换器 2内设有 ：次高温再热器 10; 二次低温再热器 9所采用的管子内 径为 46mm， 二次高温再热器 10所采用的管子内径为 48mm。
本实施例的工作原理与实施例一类似， 炉膛 26下部沿深度方向的收缩比为 0. 2， 将炉膛 出口区域单位高度的压降与炉膛平均单位高度压降 （床层压降与炉膛高度之比） 的比值 （通 常在 0.2〜0.5之间） 再提高约 0.13， 从而实现二次再热与此种炉膛结构的循环流化床锅炉有 效结合， 达到提高煤电机组发电效率与低污染物排放共存的目的， 且保证设备长期高效运 行。
实施例三
如图 4所示， 该实施例与实施例二相比， 其差别仅在于：炉膛 27为环形炉膛， 其下部设有 环形的布风板， 该布风板上设有数个风帽； 所述炉膛 27 下部沿深度方向的收缩比 （即图中 L5/L6 ) 为 0. 49， 将炉膛出口区域单位高度的压降与炉膛平均单位高度压降 （床层压降与炉 膛高度之比） 的比值 （通常在 0.2〜0.5之间） 再提高约 0.06， 从而增加了炉内的传热强度， 可满足二次再热受热面的需要。 围绕炉膛 27设有六台旋风分离器 1和六台外置式热交换器 2；
综上所述， 本发明通过改变炉膛下部沿深度方向的收缩比， 提高炉膛上部区域的颗粒浓 度至合理的水平， 将炉膛出口区域单位高度的压降与炉膛平均单位高度压降 （床层压降与炉 膛高度之比） 的比值 （通常在 0.2〜0.5之间） 再提高约 0.05〜0.15， 在不增加燃料的情况下 能有效提高炉内传热强度， 并配合优选的受热面布置方式及各级二次再热器管子内径的关系 以实现二次再热与循环流化床锅炉的有效结合， 从而达到提高煤电机组发电效率与低污染物 排放共存的目的， 且保证设备长期高效运行。

Claims

权 利 要 求 书
1.一种带二次再热的循环流化床锅炉， 包括风室、 包含布风板和风帽的布风装置、 炉膛、 一次风系统、 二次风系统、 水平烟道、 至少三台旋风分离器、 至少三台外置式热交换器、 尾 部烟道， 炉膛内设有带上、 下集箱的水冷壁， 其特征在于所述炉膛下部沿深度方向的收缩比 为 0.2-0.49; 所述尾部烟道采用平行多烟道结构， 至少包含两条平行烟道， 每条烟道内设有 烟气调节挡板， 在至少一平行烟道内的烟气调节挡板沿烟气流动方向之前设有低温过热器， 在至少另一平行烟道内的烟气调节挡板沿烟气流动方向之前设有一次低温再热器，在所有烟 气挡板沿烟气流动方向之后的尾部烟道内布置省煤器和空预器;在至少一外置式热交换器内 设有中温过热器，在至少一外置式热交换器内设有一次高温再热器，在至少一外置式热交换 器内设有二次低温再热器，在至少一外置式热交换器内设有二次高温再热器；在炉内设有高 温过热器； 水冷壁的上集箱、 低温过热器、 中温过热器和高温过热器通过管路依次连通， 一 次低温再热器与一次高温再热器通过管路连通，二次低温再热器与二次高温再热器通过管路 连通。
2. 如权利要求 1所述的一种带二次再热的循环流化床锅炉， 其特征在于所述炉 膛为单炉膛单布风板结构， 其下部设有一布风板， 布风板上设有数个风帽。
3. 如权利要求 1所述的一种带二次再热的循环流化床锅炉， 其特征在于所述炉膛采用单炉 膛双布风板结构， 其下部设有两布风板， 每块布风板上设有数个风帽。
4. 如权利要求 1所述的一种带二次再热的循环流化床锅炉， 其特征在于所述炉 膛为环形炉膛， 其下部设有环形的布风板， 该布风板上设有数个风帽。
5. 如权利要求 1至 4任一所述的一种带二次再热的循环流化床锅炉， 其特征在于所述二次 高温再热器的管子内径至少比二次低温再热器的管子内径大 1.7mm。
6. 如权利要求 5所述的一种带二次再热的循环流化床锅炉， 其特征在于所述高 温过热器为 U型屏式过热器。
PCT/CN2014/082913 2013-08-01 2014-07-24 一种带二次再热的循环流化床锅炉 WO2015014233A1 (zh)

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