WO2016119670A1 - 生物质循环流化床锅炉掺烧燃煤飞灰方法及其设备 - Google Patents

生物质循环流化床锅炉掺烧燃煤飞灰方法及其设备 Download PDF

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WO2016119670A1
WO2016119670A1 PCT/CN2016/072082 CN2016072082W WO2016119670A1 WO 2016119670 A1 WO2016119670 A1 WO 2016119670A1 CN 2016072082 W CN2016072082 W CN 2016072082W WO 2016119670 A1 WO2016119670 A1 WO 2016119670A1
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fly ash
coal
fluidized bed
circulating fluidized
fired
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PCT/CN2016/072082
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English (en)
French (fr)
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朱德辉
张岩丰
周大庆
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武汉凯迪工程技术研究总院有限公司
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Publication of WO2016119670A1 publication Critical patent/WO2016119670A1/zh

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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
    • 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
    • F23C10/18—Details; Accessories
    • F23C10/22—Fuel feeders specially adapted for fluidised bed combustion apparatus

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  • the invention relates to a technology for recycling and energy saving and emission reduction of waste ash generated in a boiler combustion power generation process, in particular to a biomass circulating fluidized bed boiler mixed with a coal-fired fly ash method and a device thereof.
  • coal-fired boiler power plants With the increasing demand for energy in modern society, the construction of coal-fired boiler power plants is also increasing. Although China has a vast territory and a wide distribution of coal resources, there are many different types of coal, especially in the south and southwest regions of China. Many provinces have a large number of low-volatility coals such as anthracite and lean coal. When burning coal-fired boilers, these low-grade coals generally have problems such as high carbon content and unsatisfactory burnout of coal-fired fly ash, which not only wastes a lot of coal resources, but also brings a serious environment. Pollution.
  • the outer part of the dilute phase combustion zone of the boiler is made of a gray shell layer which is not easy to conduct heat and burn, so that the internal flammable residual carbon core cannot reach the temperature required for combustion in the coal-fired boiler, and on the other hand, the gas
  • the slip speed between the solid two phases is low, the heat transfer rate is small, the heating process is slow, and it flies out of the furnace of the coal-fired boiler when it has not yet reached a sufficient combustion temperature, that is, the coal-fired fly ash particles are only in The coal-fired boiler has gone through a game and has not been recycled and burned.
  • biomass fuel has developed rapidly as a renewable alternative energy source.
  • the total installed capacity of power plants using biomass fuel direct-fired power generation is also increasing.
  • many biomass boiler power plants have reduced the design production load due to the lack of acquisition of biomass fuel, especially when the power plant adopts various biomass fuels.
  • the amount of biomass fuel required to sustain power generation is extremely large, and even if the amount of acquisition cannot be ensured, it can only be discontinued. How to effectively expand the source of raw materials for biomass boiler power plants and ensure their production scale and power generation efficiency has been recognized as a difficult problem and a direction for efforts by those skilled in the art, but so far no satisfactory technical solutions have been introduced.
  • the object of the present invention is to provide a biomass circulating fluidized bed boiler mixed with coal-fired fly ash and a device thereof, which can ensure that the coal-fired fly ash produced by the coal-fired boiler is again in the biomass circulating fluidized bed boiler Fully burned for secondary power generation; at the same time, it can effectively reduce the use of biomass fuel, reduce fuel input costs, increase power generation hours, and reduce pollutant emissions.
  • the biomass circulating fluidized bed boiler designed by the invention is mixed with the coal-fired fly ash method, which is to re-deliver the fly ash discharged from the coal-fired boiler to the biomass circulating fluidized bed boiler for recycling.
  • the process is unique in that it includes the following steps:
  • coal-fired fly ash particles are in a suspended flow state by airflow, and are sprayed into the bottom of the dense phase combustion zone bed above the air distribution plate in the biomass circulating fluidized bed boiler;
  • the blending amount of the coal-fired fly ash particles and the mass percentage of the biomass fuel in the biomass circulating fluidized bed boiler are controlled at 10 to 30% of the coal-fired fly ash particles,
  • the material fuel is 70-90%; among them, the best mass percentage is controlled by: 15-20% of coal-fired fly ash particles and 80-85% of biomass fuel.
  • Biomass circulating fluidized bed boilers are characterized by high efficiency of combustion and low content of fly ash residues (the amount of fly ash produced according to the type of biomass fuel is generally in the range of 3 to 5%, and the special case does not exceed 10%) Therefore, the addition of 30% or less of coal-fired fly ash particles will not cause a burden on the biomass circulating fluidized bed boiler, and the circulation amount is moderate.
  • the fluidized environment of the biomass circulating fluidized bed boiler can be fully utilized to fly the coal. The ash particles are burned out.
  • the flow rate of the suspended mixture of the coal fly ash particles and the air is controlled to be 12 to 18 m/s.
  • the optimum flow rate is controlled at 14 to 16 m/s, for example, 15 m/s.
  • Appropriate flow rate ensures that coal-fired fly ash particles are injected into the bottom of the dense phase combustion zone at a certain pressure to increase the disturbance, contact and mixing with the hot biomass bed particles, creating conditions for subsequent intense combustion reactions. .
  • the mass ratio of the coal-fired fly ash particles to the air is controlled to be 2.0 to 3.5:1.
  • the optimum mass ratio is controlled at 2.5 to 3.0:1.
  • the proper mass ratio can ensure the concentration of coal-fired fly ash particles into the bottom of the dense phase combustion zone, and can simultaneously supplement the oxygen through pneumatic conveying, so as to cooperate with the oxygen delivered by the primary air to make most of the coal-fired fly ash particles.
  • the charcoal in the burning is exhausted.
  • the residual carbon content in the coal fly ash particles is 8-15% of the total weight.
  • most of the coal-fired fly ash particles have a residual carbon content of 10 to 14% of the total weight.
  • the calorific value of the coal-fired fly ash particles has a calorific value of about 800 to 1200 kcal/kg, which can effectively supplement the low heat value of the biomass fuel power generation, and burns in the dense phase by burning coal fly ash particles.
  • the two-stage combustion of the zone and the dilute phase combustion zone is used to further improve the power generation efficiency of the biomass circulating fluidized bed boiler.
  • the reaction residence time of the coal-fired fly ash particles in the dense phase combustion zone is controlled to be 0.8 to 1.5 s.
  • the best reaction residence time is controlled at 1.0 to 1.2 s. Appropriately prolonging the reaction residence time of coal-fired fly ash particles in the dense phase combustion zone can promote the full contact and mixed combustion with the oxygen in the primary air to ensure that the coal-fired fly ash particles are burned as much as possible at this stage.
  • the reaction residence time of the remaining carbon black core remaining in the coal-fired fly ash particles in the dilute phase combustion zone is controlled to be 5.2 to 6.5 s.
  • the optimal reaction residence time is controlled at 5.5 to 6.0 s. In this way, the total residence time of the coal-fired fly ash particles in the biomass circulating fluidized bed boiler can be effectively extended to ensure that all of the coal-fired fly ash particles are completely burned out at this stage.
  • the invention relates to a biomass circulating fluidized bed boiler specially designed for realizing the above method, which comprises a coal-fired fly ash equipment, comprising a coal-fired fly ash storage bin used in combination with a biomass circulating fluidized bed boiler, the special features of which are:
  • the bottom discharge port of the coal-fired fly ash storage bin is connected to the powder input end of the injector through a rotary feeding device, and the air input end of the injector is connected to the blower through a check valve, the suspension of the injector
  • the material nozzle is connected to one end of the transmission pipeline, and the other end of the transmission pipeline enters from the bottom air chamber of the biomass circulating fluidized bed boiler, and is connected to the bottom feed wear-resistant nozzle through the air distribution plate uniformly distributed with the wind hood.
  • the bottom feed wear nozzle is located in the dense phase combustion zone above the air distribution plate.
  • the position of the injection port of the bottom feed wear nozzle is higher than the position of the air outlet of the hood on the air distribution plate by 500 to 800 mm.
  • the primary air with a high oxygen concentration ejected from the hood directly acts on the coal-fired fly ash particles sprayed from the bottom-feeding wear-resistant nozzle above it, on the one hand, the coal-fired fly ash particles can be promoted in the dense phase combustion zone. Produce violent tumbling and friction, remove the gray shell and expose the black core of the carbon residue; on the other hand, ensure the black core and oxygen of the carbon residue Fully in contact with the mixture, a violent combustion reaction occurs, and most of the carbon black core is burned out.
  • a preferred angle between the injection direction of the bottom feed wear-resistant nozzle and the horizontal plane is 0 to 25°.
  • the coal-fired fly ash particles are sprayed at a nearly horizontal angle, which can enhance the disturbance between the coal-fired fly ash particles and the particles of the hot biomass bed material, and increase the contact area with the oxygen in the primary air, thereby improving the coal-fired fly ash particles.
  • the burning rate of the residual carbon black core is 0 to 25°.
  • the number of the bottom-feeding wear-resistant nozzles is 2-6, which may be 2, 4 or 6, evenly arranged above the air distribution plate, and each bottom-feeding wear-resistant nozzle passes through the branch pipe and the transmission pipe. The other end is connected. In this way, the coal-fired fly ash particles entering the bottom of the dense phase combustion zone in the biomass circulating fluidized bed boiler can be evenly distributed to ensure stable, efficient and reliable operation of the biomass circulating fluidized bed boiler.
  • the transmission pipe includes a horizontal pipe section and a vertical pipe section, and the horizontal pipe section and the vertical pipe section are connected by a wear-resistant elbow. In this way, it is possible to ensure the wear resistance of the transmission pipe subjected to the most severe bending portion, prolong the service life of the entire transmission pipe, and ensure that the coal-fired fly ash particles can be quickly and smoothly turned to the bottom of the biomass circulating fluidized bed boiler.
  • the blower is a Roots blower, and two sets are arranged in parallel, and one set of Roots blower is provided with a venting valve.
  • the Roots blower is a positive displacement fan that uses two leaf-shaped rotors to move relative to each other in the cylinder to compress and deliver gas. It is well suited for low-pressure air transport of coal-fired fly ash particles.
  • One or two sets of Roots blowers can be turned on according to actual needs, and the amount of air supply can be adjusted by the venting valve to meet the needs of pneumatic conveying of various coal ash particles.
  • the rotary dosing device is a rotary feed valve remotely controlled by the frequency converter.
  • Rotary feed valve can be widely used in the transportation of powder, granular materials and powder mixture. It can remotely adjust and control the speed through the frequency converter, especially suitable for the quantitative transportation of coal fly ash particles, so as to meet the circulation of biomass. Accurate control of the percentage content of coal-fired fly ash particles in a chemical bed boiler.
  • the invention carefully studies and analyzes the low ash content of the biomass fuel combustion power generation, the small pollutant discharge, and the high carbon residue and the environmental pollution caused by the coal-fired fly ash particles discharged from the coal-fired boiler, combined with the biomass.
  • the operating characteristics of the circulating fluidized bed boiler subtly inject the coal-fired fly ash particles into the bottom of the dense phase combustion zone bed in the biomass circulating fluidized bed boiler.
  • the coal-fired fly ash particles enter the bottom of the dense phase combustion zone bed, which can be fully squeezed into contact with a large number of hot biomass bed material particles, carry out strong heat and mass transfer, rapidly heat up and start to burn, effectively overcome The problem of the combustion temperature cannot be reached by feeding the coal-fired fly ash particles into the furnace by means of surface feeding.
  • the dense phase combustion zone is not burned out. After a small amount of residual carbon black core enters the relatively low temperature dilute phase combustion zone, it can still maintain high temperature and high heat state under the action of inertia, which is beneficial to continue burning.
  • the dense phase combustion zone of the biomass circulating fluidized bed boiler is usually in the state of a bubbling fluidized bed or a turbulent fluidized bed, and a large amount of hot biomass bed material particles can be combined with the coal fly ash particles injected therein.
  • the ash shell of the outer layer of the coal-fired fly ash particles can be worn away in an instant, so that the exposed internal carbon black core is in full contact with the oxygen in the primary air, thereby greatly improving the efficiency of the combustion reaction.
  • the residence time of the bed in the dense phase combustion zone can be effectively increased under the hindrance and envelopment of a large amount of hot biomass bed material particles, thereby Extend the total residence time in the biomass circulating fluidized bed boiler to ensure that the coal-fired fly ash particles are completely burned out.
  • the coal-fired fly ash particles are sprayed into the bottom of the bed of the dense phase combustion zone, just above the primary air blown by the hood on the air distribution plate.
  • the oxygen concentration in the primary air is relatively high, which is convenient for coal-fired fly ash.
  • a sufficiently vigorous combustion reaction of the particles is very advantageous for increasing the burning rate of the black core of the carbon residue.
  • biomass circulating fluidized bed boilers to blend coal-fired fly ash particles does not require major modifications to the original biomass circulating fluidized bed boiler, only adding storage bins, injectors, blowers and corresponding piping
  • the system can be used, the amount of reconstruction works is small, the construction is convenient, and it is easy to promote and apply.
  • FIG. 1 is a schematic view showing the structure of a biomass circulating fluidized bed mixed with coal-fired fly ash equipment.
  • FIG. 2 is a partially enlarged schematic structural view of the air distribution plate of FIG. 1.
  • FIG. 2 is a partially enlarged schematic structural view of the air distribution plate of FIG. 1.
  • coal-fired fly ash storage bin 1 coal-fired fly ash storage bin 1
  • rotary feeding device 2 ejector 3, check valve 4, blower 5, conveying pipe 6, wear-resistant elbow 7, bottom feeding wear-resistant nozzle 8, biomass circulation
  • the chemical bed boiler 9 the bottom plenum 10, the air distribution plate 11, the hood 12, the dense phase combustion zone 13, the dilute phase combustion zone 14, and the vent valve 15.
  • the biomass circulating fluidized bed boiler shown in the figure is mixed with a coal-fired fly ash plant, and has a coal-fired fly ash storage bin 1 for use with the biomass circulating fluidized bed boiler 9.
  • the bottom discharge port of the coal-fired fly ash storage bin 1 is connected to the powder input end of the injector 3 through the rotary feeding device 2, and the rotary feeding device 2 uses a rotary feed valve remotely controlled by the frequency converter to precisely control the coal burning. The amount of fly ash delivered.
  • the air input end of the ejector 3 is connected to the blower 5 through the check valve 4, the blower 5 is a Roots blower, and the Roots blower is arranged in parallel with two sets, wherein a set of Roots blower is provided with a venting valve 15 which can be partially required Or all of the Roots blower is turned on, and the amount of air supplied by the vent valve is adjusted to obtain the required air volume.
  • the suspension nozzle of the ejector 3 is connected to one end of the transmission pipe 6, and the transmission pipe 6 is composed of a horizontal pipe section and a vertical pipe section, and the horizontal pipe section and the vertical pipe section are connected by a wear-resistant elbow 7 to enhance the most severe impact.
  • the wear resistance of the bent portion improves the working life of the entire transfer pipe 6, and the other end of the transfer pipe 6 enters from the bottom plenum 10 of the biomass circulating fluidized bed boiler 9 and passes through the cloth uniformly distributed with the hood 12.
  • the plate 11 is connected to the bottom feed wear nozzle 8 which is located in the dense phase combustion zone 13 above the air distribution plate 11.
  • the position of the injection port of the bottom feed wear-resistant nozzle 8 is higher than the position of the air outlet of the wind cap 12 on the air distribution plate 11 by 650 mm, so as to facilitate the full contact and mixing of the coal-fired fly ash particles with the primary air, and the bottom feed wear-resistant
  • the angle between the injection direction of the nozzle 8 and the horizontal plane is 0 to 10° to further increase the contact disturbance between the coal-fired fly ash particles and the primary air.
  • the bottom feeding wear-resistant nozzles 8 are preferably arranged in pairs, and the number may be two, four or six.
  • bottom-feeding wear-resistant nozzles 8 are used, which are evenly arranged above the air-distributing plate 11, each The bottom feed wear-resistant nozzles 8 are all connected to the other end of the transfer pipe 6 through the branch pipe, so that the coal-fired fly ash particles output from the ejector 3 can be uniformly injected into the dense phase combustion zone in the biomass circulating fluidized bed boiler 9. 13 bed bottom.
  • coal-fired fly ash particles discharged from the coal-fired boiler having a residual carbon content of 10 to 14% of the total weight are loaded into the coal-fired fly ash storage bin 1.
  • the rotary feeding device 2 is turned on, and the rotating feed rate is controlled by the frequency converter, so that the coal-fired fly ash particles in the coal-fired fly ash storage bin 1 are delivered to the injector 3 according to the set feed amount.
  • the blower 5 is turned on to deliver air to the ejector 3, the check valve 4 is used to prevent air and coal fly ash particles from flowing back to the blower 5, and the vent valve 15 is used to adjust the air flow output from the blower 5 through the above device
  • the synergistic effect is that the coal-fired fly ash particles injected from the injector 3 to one end of the transmission pipe 6 are in a floating flow state, wherein the mass ratio of the coal-fired fly ash particles to the air is preferably controlled within a range of 2.5 to 3.0:1. .
  • the suspended mixture of coal-fired fly ash particles and air passes through the transfer pipe 6 at a flow rate of 14 to 16 m/s, and is sprayed by the bottom feed wear-resistant nozzle 8 at the other end of the transfer pipe 6.
  • the mixture is incorporated into the bottom of the dense phase combustion zone 13 above the air distribution plate 11 in the biomass circulating fluidized bed boiler 9 at an angle of 0 to 10° from the horizontal plane.
  • the blending amount of coal-fired fly ash particles and the mass percentage of biomass fuel in the biomass circulating fluidized bed boiler 9 are preferably controlled to be 15-20% of coal-fired fly ash particles and 80-85% of biomass fuel.
  • the coal-fired fly ash particles can stay therein for a sufficient period of time, and a large amount in the bubbling fluidization state or the turbulent fluidization state.
  • the hot biomass bed material particles are intertwined and mixed to produce strong heat and mass transfer and temperature rise, and violent tumbling and friction occur together.
  • the outer shell of the coal-fired fly ash particles is not easily burned, and the unburned residue is removed. The carbon black core is exposed.
  • the black carbon core exposed in the dense phase combustion zone 13 is in full contact with the primary air output from the hood 12 on the air distribution plate 11, and a rapid and intense combustion reaction occurs, and most of the carbon residue is removed.
  • the black core burned out.
  • the reaction residence time of the coal-fired fly ash particles in the dense phase combustion zone 13 is preferably controlled to be 1.0 to 1.2 s.
  • the remaining carbon black core enters the relatively low temperature dilute phase combustion zone 14 in the dense phase combustion zone 13 under the action of fluidizing wind in the biomass circulating fluidized bed boiler 9, and the inertia of high temperature and high heat Continue to maintain the combustion reaction.
  • the reaction residence time of the residual carbon black core remaining in the coal-fired fly ash particles in the dilute phase combustion zone 14 is preferably controlled at 5.5 to 6.0 s until the remaining residue The carbon black core is completely burned, thereby achieving secondary combustion power generation of coal-fired fly ash particles.
  • the coal-fired fly ash particles discharged from the coal-fired boiler are recycled by the method and the device of the invention, and the doped coal-fired fly ash particles can reach 30% of the total fuel amount.
  • the calculation shows that the coal-fired power plant of a 300-600MW unit (including circulating fluidized bed boiler and pulverized coal boiler power plant) has far more than 71,400 tons of coal, which can fully meet the biomass circulation of a 30MW unit.
  • the biomass circulating fluidized bed boiler designed according to the present invention is blended with the coal-fired fly ash method to reform the biomass power plant, and the fly ash of the coal-fired power plant can be recovered in combination with the treatment, thereby not only saving a large amount of biomass fuel, but also Greatly reduce the hazards of coal-fired fly ash and achieve a win-win situation for power generation and environmental protection.

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Abstract

一种生物质循环流化床锅炉（9）掺烧燃煤飞灰的方法及其设备。该方法将燃煤飞灰喷射到生物质循环流化床锅炉（9）内的密相燃烧区（13）床层底部，使其与鼓泡或湍动流化状态的炽热生物质床料混合，生产强烈的传热传质和升温，并发生剧烈的翻滚和摩擦，将燃煤飞灰外层的灰壳磨掉，露出其中未燃尽的残炭黑芯，最终使燃煤飞灰在密相燃烧区（13）和稀相燃烧区（14）燃烧殆尽。该设备主要由与生物质循环流化床锅炉（9）配套使用的燃煤飞灰储存仓（1）、旋转给料装置（2）、喷射器（3）、鼓风机（5）、传输管道（6）和底饲耐磨喷嘴（8）等组成。此设备可使燃煤飞灰回收到生物质循环流化床锅炉（9）中再次充分燃烧，进行二次发电，可有效减少生物质燃料用量，提高单位燃料的发电量，并可减少燃煤污染物排放。

Description

生物质循环流化床锅炉掺烧燃煤飞灰方法及其设备 技术领域
本发明涉及对锅炉燃烧发电过程中产生的废弃灰渣进行回收利用和节能减排的技术，具体地指一种生物质循环流化床锅炉掺烧燃煤飞灰方法及其设备。
背景技术
随着现代社会对能源需求的日益增长，燃煤锅炉发电厂的建设也越来越多。虽然我国地域广阔、煤炭资源分布广泛，但煤炭种类众多不一，尤其是在我国的南方和西南地区，许多省份拥有大量的无烟煤、贫煤等低挥发份煤种。燃煤锅炉电厂在燃用这些低等级煤种时，普遍存在所排放的燃煤飞灰含炭量高、燃尽程度不理想等问题，不仅浪费了大量煤炭资源，而且带来了严重的环境污染。为了解决上述问题，本领域技术人员也试尝将未燃尽的燃煤飞灰颗粒重新输送到燃煤锅炉中循环利用，但这些燃煤飞灰颗粒是通过面饲的方式直接送回燃煤锅炉上部稀相燃烧区的，一方面因其外部为不易导热和燃烧的灰壳层，使得其内部的可燃残炭黒芯在燃煤锅炉内无法达到燃烧所需的温度，另一方面因气固两相之间的滑移速度低、传热速率小、升温过程缓慢，在其还没来得及上升到足够的燃烧温度时就飞出了燃煤锅炉的炉膛，即燃煤飞灰颗粒只是在燃煤锅炉中走了个过场，实际上并没有被回收燃烧利用。
另一方面，随着煤炭等传统化石能源储量的日益减少，生物质燃料作为一种可再生的替代能源得到了迅速的发展。采用生物质燃料直燃发电的电厂总装机容量也越来越多。但受生物质燃料资源收购半径和总量的制约，目前已经有许多生物质锅炉发电厂因收购不到生物质燃料而降低设计的生产负荷，特别是当发电厂采用能适应各种生物质燃料高效充分燃烧、且产生的残渣灰分低、环保性能好的生物质循环流化床锅炉时，维持发电连续进行的生物质燃料需要量极大，在无法确保收购量的情况下甚至只能停产。如何有效扩大生物质锅炉发电厂的原料来源、保证其生产规模和发电效益，这一直是本领域技术人员公认的难题和努力探索的方向，但至今为止尚无令人满意的技术方案问世。
发明内容
本发明的目的就是要提供一种生物质循环流化床锅炉掺烧燃煤飞灰方法及其设备，该技术可以确保燃煤锅炉生产的燃煤飞灰在生物质循环流化床锅炉中再次充分燃烧，进行二次发电；同时可有效减少生物质燃料的使用量，降低燃料投入成本，提高发电小时数，且减少污染物排放。
为实现上述目的，本发明所设计的生物质循环流化床锅炉掺烧燃煤飞灰方法，它是将燃煤锅炉排放的飞灰重新输送到生物质循环流化床锅炉中进行回收利用的过程，其特殊之处在于：该方法包括如下步骤：
1)通过气流输送使燃煤飞灰颗粒处于悬浮流动状态，并喷射到生物质循环流化床锅炉内位于布风板上方的密相燃烧区床层底部；
2)使燃煤飞灰颗粒与密相燃烧区中处于鼓泡流化状态或湍动流化状态的大量炽热生物质床料颗粒混合，生产强烈的传热传质和升温，并一起发生剧烈的翻滚和摩擦，将燃煤飞灰颗粒外层的灰壳磨掉，露出其中未燃尽的残炭黑芯；
3)利用从布风板上的风帽中输出的一次风含氧浓度高的特点，使密相燃烧区中的残炭黑芯与氧气发生迅速和充分的燃烧反应，其中绝大部分残炭黑芯被燃尽；
4)随后剩余的残炭黑芯在生物质循环流化床锅炉内流化风的作用下进入密相燃烧区上方温度相对较低的稀相燃烧区，在高温高热的惯性作用下继续保持燃烧反应，最终将剩余的残炭黑芯全部燃尽，从而实现燃煤飞灰颗粒的二次燃烧发电。
作为优选方案，所说的步骤1)中，燃煤飞灰颗粒的掺入量与生物质循环流化床锅炉内生物质燃料的质量百分比控制在：燃煤飞灰颗粒10～30％，生物质燃料70～90％；其中，最佳的质量百分比控制在：燃煤飞灰颗粒15～20％，生物质燃料80～85％。由于生物质循环流化床锅炉具有燃烧充分高效、飞灰残渣含量少的特点(根据生物质燃料种类不同所产生的飞灰量一般在3～5％的范围内，特殊情况不超过10％)，因此额外添加30％以下的燃煤飞灰颗粒不会造成生物质循环流化床锅炉的负担，且循环量适中，可充分利用生物质循环流化床锅炉的流态化环境将燃煤飞灰颗粒燃尽。
作为优选方案，所说的步骤1)中，燃煤飞灰颗粒与空气的悬浮混合物的流速控制在12～18m/s。其中，最佳的流速控制在14～16m/s，例如15m/s。适当的流速可以确保燃煤飞灰颗粒以一定的压力喷入密相燃烧区床层底部，加大其与炽热生物质床料颗粒之间的扰动、接触和混合，为后续剧烈燃烧反应创造条件。
作为优选方案，所说的步骤1)中，燃煤飞灰颗粒与空气的质量比控制在2.0～3.5∶1。其中，最佳的质量比控制在2.5～3.0∶1。适当的质量比既可以确保燃煤飞灰颗粒进入密相燃烧区床层底部的浓度，又可以通过气力输送同步补充氧气，从而与一次风输送的氧气协同作用，使大部分燃煤飞灰颗粒中的残炭燃烧殆尽。
作为优选方案，所说的步骤1)中，燃煤飞灰颗粒中的残炭含量占其总重量的8～15％。其中，大部分燃煤飞灰颗粒中的残炭含量占其总重量的10～14％。一般而言，这种残炭含量的燃煤飞灰颗粒的热值约在800～1200kcal/kg，可以有效补充生物质燃料发电热值偏低的不足，通过燃煤飞灰颗粒在密相燃烧区和稀相燃烧区的两级燃烧回用，最终进一步提高生物质循环流化床锅炉的发电效率。
作为优选方案，所说的步骤2)和步骤3)中，燃煤飞灰颗粒在密相燃烧区的反应停留时间控制在0.8～1.5s。其中，最好的反应停留时间控制在1.0～1.2s。适当延长燃煤飞灰颗粒在密相燃烧区的反应停留时间，可促使其与一次风中的氧气充分接触混合燃烧，确保燃煤飞灰颗粒在此阶段尽量燃尽。
作为优选方案，所说的步骤4)中，燃煤飞灰颗粒中剩余的残炭黑芯在稀相燃烧区的反应停留时间控制在5.2～6.5s。其中，最佳的反应停留时间控制在5.5～6.0s。这样，可以有效延长燃煤飞灰颗粒在生物质循环流化床锅炉内的总停留时间，确保所有的燃煤飞灰颗粒在此阶段完全燃尽。
本发明为实现上述方法而专门设计的生物质循环流化床锅炉掺烧燃煤飞灰设备，包括与生物质循环流化床锅炉配套使用的燃煤飞灰储存仓，其特殊之处在于：
所述燃煤飞灰储存仓的底部出料口通过旋转给料装置与喷射器的粉料输入端相连，所述喷射器的空气输入端通过止回阀与鼓风机相连，所述喷射器的悬浮物喷口与传输管道的一端相连，所述传输管道的另一端从生物质循环流化床锅炉的底部风室进入其中、并穿过均布有风帽的布风板与底饲耐磨喷嘴相连，所述底饲耐磨喷嘴位于布风板上方的密相燃烧区中。
作为优选方案，所述底饲耐磨喷嘴的喷射口位置高于所述布风板上的风帽的出风口位置500～800mm。这样，从风帽喷出的含氧浓度较高的一次风直接作用在其上方从底饲耐磨喷嘴喷出的燃煤飞灰颗粒上，一方面可以促使燃煤飞灰颗粒在密相燃烧区生产剧烈的翻滚和摩擦，脱除灰壳而露出其中的残炭黑芯；另一方面可以确保该残炭黑芯与氧气 充分接触混合，发生剧烈的燃烧反应，从而将绝大部分的残炭黑芯燃尽。
进一步地，所述底饲耐磨喷嘴的喷射方向与水平面的优选夹角为0～25°。这样，使燃煤飞灰颗粒以近乎水平的角度喷出，可增强其与炽热生物质床料颗粒之间的扰动，加大其与一次风中氧气的接触面积，从而提高燃煤飞灰颗粒中残碳黑芯的燃烧速率。
进一步地，所述底饲耐磨喷嘴的数量为2～6个，可以是2个、4个或6个，均匀布置在所述布风板上方，各个底饲耐磨喷嘴通过支管与传输管道的另一端相连。这样，可以均匀分配进入生物质循环流化床锅炉内密相燃烧区床层底部的燃煤飞灰颗粒，确保生物质循环流化床锅炉运行平稳、高效、可靠。
更进一步地，所述传输管道包括水平管段和垂直管段，所述水平管段和垂直管段之间通过耐磨弯头过渡相连。这样，可以确保传输管道受冲击最严重的弯曲部位的抗磨损性能，延长整个传输管道的使用寿命，保证燃煤飞灰颗粒能够快捷顺利地转向生物质循环流化床锅炉的底部。
再进一步地，所述鼓风机为罗茨风机，并列设置有两套，其中一套罗茨风机上设置有放空阀。罗茨风机为容积式风机，其利用两个叶形转子在气缸内作相对运动来压缩和输送气体，十分适于燃煤飞灰颗粒的低压空气输送。可以根据实际需要开启一套或两套罗茨风机，并通过放空阀调节其送风量的大小，从而满足各种不同性能的燃煤飞灰颗粒气力输送的需要。
还进一步地，所述旋转给料装置为变频器远程控制的旋转给料阀。旋转给料阀可广泛应用于粉沫、颗粒物料、粉粒混合物的输送，其通过变频器可以远程调节和控制转速，特别适于燃煤飞灰颗粒的定量输送，从而满足对生物质循环流化床锅炉掺烧燃煤飞灰颗粒百分比含量的精准控制。
本发明在仔细研究和分析生物质燃料燃烧发电灰分量低、排放污染物小，以及燃煤锅炉所排放燃煤飞灰颗粒含残炭量高、环境污染严重等特性的基础上，结合生物质循环流化床锅炉的运行特点，巧妙地将燃煤飞灰颗粒喷射到生物质循环流化床锅炉内的密相燃烧区床层底部，其优点主要体现在如下几方面：
其一，燃煤飞灰颗粒进入密相燃烧区床层底部，可与大量炽热的生物质床料颗粒发生充分的挤压接触，进行强烈的传热传质，迅速升温而开始燃烧，有效克服了通过面饲方式将燃煤飞灰颗粒送入炉内而无法达到燃烧温度的问题。同时，密相燃烧区未燃尽的 少量残炭黑芯进入温度相对较低的稀相燃烧区后，仍能在惯性作用下保持高温高热状态，从而有利于继续燃尽。
其二，生物质循环流化床锅炉的密相燃烧区通常处于鼓泡流化床或湍动流化床状态，大量炽热的生物质床料颗粒可与喷入其中的燃煤飞灰颗粒一起产生剧烈的翻滚和摩擦，瞬间即可将燃煤飞灰颗粒外层的灰壳磨掉，从而使暴露出的内部残炭黑芯与一次风中的氧气充分接触，大幅提高燃烧反应的效率。
其三，燃煤飞灰颗粒喷入密相燃烧区床层底部后，在大量炽热生物质床料颗粒的阻碍和包围作用下，可有效增加其在密相燃烧区床层的滞留时间，从而延长其在生物质循环流化床锅炉内的总停留时间，进而确保燃煤飞灰颗粒完全燃尽。
其四，燃煤飞灰颗粒喷入密相燃烧区床层底部的区域，正好位于布风板上风帽喷射一次风的上方，此时一次风中的氧气浓度相对较高，便于燃煤飞灰颗粒发生充分剧烈的燃烧反应，对提高残炭黑芯的燃烧速率十分有利。
其五，燃煤飞灰颗粒在生物质循环流化床锅炉中的充分回燃利用，有效解决了燃煤锅炉发电厂飞灰高含碳量低燃尽度的致命缺陷，既充分利用了燃煤飞灰颗粒进行二次发电，又相应减少了生物质燃料的用量，还实现了节能减排，提高了单位原料的发电小时数，产生了一举多得的有益效果。
其六，采用生物质循环流化床锅炉掺烧燃煤飞灰颗粒，不需要对原有的生物质循环流化床锅炉进行重大改造，仅仅增加储存仓、喷射器、鼓风机和相应的管路***即可，改造工程量小，施工方便，易于推广应用。
附图说明
图1为一种生物质循环流化床掺烧燃煤飞灰设备的结构示意图。
图2为图1中布风板处的局部放大结构示意图。
图中：燃煤飞灰储存仓1，旋转给料装置2，喷射器3，止回阀4，鼓风机5，输送管道6，耐磨弯头7，底饲耐磨喷嘴8，生物质循环流化床锅炉9，底部风室10，布风板11，风帽12，密相燃烧区13，稀相燃烧区14，放空阀15。
具体实施方式
以下结合附图和具体实施例对本发明的设备和工艺作进一步的详细描述。
图中所示的生物质循环流化床锅炉掺烧燃煤飞灰设备，具有与生物质循环流化床锅炉9配套使用的燃煤飞灰储存仓1。燃煤飞灰储存仓1的底部出料口通过旋转给料装置2与喷射器3的粉料输入端相连，旋转给料装置2采用变频器远程控制的旋转给料阀，以精确控制燃煤飞灰的输送量。喷射器3的空气输入端通过止回阀4与鼓风机5相连，鼓风机5采用罗茨风机，罗茨风机并列设置有两套，其中一套罗茨风机上设置有放空阀15，可以根据需要部分或全部开启罗茨风机，并由放空阀调节其送风量的大小，以获得所需的输送风量。喷射器3的悬浮物喷口与传输管道6的一端相连，传输管道6由水平管段和垂直管段组成，水平管段和垂直管段之间通过耐磨弯头7过渡相连，以增强其受冲击最严重的弯曲部位的抗磨损性能，提高整个传输管道6的工作寿命，传输管道6的另一端从生物质循环流化床锅炉9的底部风室10进入其中、并穿过均布有风帽12的布风板11与底饲耐磨喷嘴8相连，底饲耐磨喷嘴8位于布风板11上方的密相燃烧区13中。
本实施例中，底饲耐磨喷嘴8的喷射口位置高于布风板11上的风帽12的出风口位置650mm，以利于燃煤飞灰颗粒与一次风充分接触混合，且底饲耐磨喷嘴8的喷射方向与水平面的夹角为0～10°，以进一步增加燃煤飞灰颗粒与一次风的接触扰动。同时底饲耐磨喷嘴8最好成对设置，数量可以为2个、4个或6个，本实施例中采用4个底饲耐磨喷嘴8，均匀布置在布风板11的上方，每个底饲耐磨喷嘴8均通过支管与传输管道6的另一端相连，这样可以将从喷射器3输出的燃煤飞灰颗粒均匀喷入生物质循环流化床锅炉9内的密相燃烧区13床层底部。
上述生物质循环流化床锅炉掺烧燃煤飞灰设备在实际运行时的工艺过程概括如下：
1)预先优选燃煤锅炉排放的残炭含量占其总重量10～14％的燃煤飞灰颗粒装载到燃煤飞灰储存仓1中。需要利用时，开启旋转给料装置2，通过变频器控制其旋转给料速率，使燃煤飞灰储存仓1内的燃煤飞灰颗粒按设定的进给量输送至喷射器3中。与此同时，开启鼓风机5，向喷射器3输送空气，止回阀4用于阻止空气和燃煤飞灰颗粒向鼓风机5回流，放空阀15用于调节鼓风机5输出的空气流量，通过以上装置的协同作用，使从喷射器3喷入至传输管道6一端的燃煤飞灰颗粒处于悬浮流动状态，其中燃煤飞灰颗粒与空气的质量比最好控制在2.5～3.0∶1的范围内。随后燃煤飞灰颗粒与空气的悬浮混合物以14～16m/s的流速通过传输管道6，并由传输管道6另一端的底饲耐磨喷嘴8喷 出，以与水平面夹角为0～10°的夹角掺入生物质循环流化床锅炉9内位于布风板11上方的密相燃烧区13床层底部。其中，燃煤飞灰颗粒的掺入量与生物质循环流化床锅炉9内生物质燃料的质量百分比最好控制在：燃煤飞灰颗粒15～20％，生物质燃料80～85％。
2)在上述密相燃烧区13中，由于循环流化床的风速较低，燃煤飞灰颗粒可以在其中停留足够长的时间，与处于鼓泡流化状态或湍动流化状态的大量炽热生物质床料颗粒交织混合，生产强烈的传热传质和升温，并一起发生剧烈的翻滚和摩擦，燃煤飞灰颗粒外层不易燃烧的灰壳被磨掉，其中未燃尽的残炭黑芯被暴露出来。
3)随后，密相燃烧区13中暴露的残炭黑芯与从布风板11上的风帽12中输出的一次风充分接触混合，发生迅速和剧烈的燃烧反应，将绝大部分的残炭黑芯燃烧殆尽。为了确保密相燃烧区13的燃尽效果，燃煤飞灰颗粒在密相燃烧区13的反应停留时间最好控制在1.0～1.2s。
4)最后，剩余的残炭黑芯在生物质循环流化床锅炉9内流化风的作用下进入密相燃烧区13上方温度相对较低的稀相燃烧区14，在高温高热的惯性作用下继续保持燃烧反应。同样，为了确保稀相燃烧区14的燃尽效果，燃煤飞灰颗粒中剩余的残炭黑芯在稀相燃烧区14的反应停留时间最好控制在5.5～6.0s，直至将剩余的残炭黑芯全部燃尽，从而实现燃煤飞灰颗粒的二次燃烧发电。
采用本发明的方法和设备对燃煤锅炉所排放的燃煤飞灰颗粒进行回收利用，其掺杂的燃煤飞灰颗粒可达到总燃料量的30％。按照燃煤飞灰颗粒30％、生物质燃料70％的质量百分比，以生物质发电厂年运行7000小时计算：一台30MW的生物质循环流化床锅炉掺烧的燃煤飞灰颗粒量可达7.14万吨，与其配合的生物质燃料量为17.6万吨。通过测算表明：一台300～600MW机组的燃煤电厂(包括循环流化床锅炉和煤粉锅炉电厂)的燃煤飞灰量远超过7.14万吨，完全可以满足一台30MW机组的生物质循环流化床锅炉对燃煤飞灰二次发电的需要。因此，按照本发明所设计的生物质循环流化床锅炉掺烧燃煤飞灰方法对生物质发电厂进行改造，配合处理回收燃煤电厂的飞灰，不仅可以节省大量生物质燃料，而且可以大幅降低燃煤飞灰的危害，实现发电和环保双赢。

Claims (20)

  1. 一种生物质循环流化床锅炉掺烧燃煤飞灰方法，它是将燃煤锅炉排放的飞灰重新输送到生物质循环流化床锅炉(9)中进行回收利用的过程，其特征在于：该方法包括如下步骤：
    1)通过气流输送使燃煤飞灰颗粒处于悬浮流动状态，并喷射到生物质循环流化床锅炉(9)内位于布风板(11)上方的密相燃烧区(13)床层底部；
    2)使燃煤飞灰颗粒与密相燃烧区(13)中处于鼓泡流化状态或湍动流化状态的大量炽热生物质床料颗粒混合，生产强烈的传热传质和升温，并一起发生剧烈的翻滚和摩擦，将燃煤飞灰颗粒外层的灰壳磨掉，露出其中未燃尽的残炭黑芯；
    3)利用从布风板(11)上的风帽(12)中输出的一次风含氧浓度高的特点，使密相燃烧区(13)中的残炭黑芯与氧气发生迅速和充分的燃烧反应，其中绝大部分残炭黑芯被燃尽；
    4)随后剩余的残炭黑芯在生物质循环流化床锅炉(9)内流化风的作用下进入密相燃烧区(13)上方温度相对较低的稀相燃烧区(14)，在高温高热的惯性作用下继续保持燃烧反应，最终将剩余的残炭黑芯全部燃尽，从而实现燃煤飞灰颗粒的二次燃烧发电。
  2. 根据权利要求1所述的生物质循环流化床锅炉掺烧燃煤飞灰方法，其特征在于：所说的步骤1)中，燃煤飞灰颗粒的掺入量与生物质循环流化床锅炉(9)内生物质燃料的质量百分比控制在：燃煤飞灰颗粒10～30％，生物质床燃料70～90％。
  3. 根据权利要求1所述的生物质循环流化床锅炉掺烧燃煤飞灰方法，其特征在于：所说的步骤1)中，燃煤飞灰颗粒的掺入量与生物质循环流化床锅炉(9)内生物质燃料的质量百分比控制在：燃煤飞灰颗粒15～20％，生物质燃料80～85％。
  4. 根据权利要求1所述的生物质循环流化床锅炉掺烧燃煤飞灰方法，其特征 在于：所说的步骤1)中，燃煤飞灰颗粒与空气的悬浮混合物的流速控制在12～18m/s。
  5. 根据权利要求1所述的生物质循环流化床锅炉掺烧燃煤飞灰方法，其特征在于：所说的步骤1)中，燃煤飞灰颗粒与空气的悬浮混合物的流速控制在14～16m/s。
  6. 根据权利要求1所述的生物质循环流化床锅炉掺烧燃煤飞灰方法，其特征在于：所说的步骤1)中，燃煤飞灰颗粒与空气的质量比控制在2.0～3.5∶1。
  7. 根据权利要求1所述的生物质循环流化床锅炉掺烧燃煤飞灰方法，其特征在于：所说的步骤1)中，燃煤飞灰颗粒与空气的质量比控制在2.5～3.0∶1。
  8. 根据权利要求1所述的生物质循环流化床锅炉掺烧燃煤飞灰方法，其特征在于：所说的步骤1)中，燃煤飞灰颗粒中的残炭含量占其总重量的8～15％。
  9. 根据权利要求1所述的生物质循环流化床锅炉掺烧燃煤飞灰方法，其特征在于：所说的步骤1)中，燃煤飞灰颗粒中的残炭含量占其总重量的10～14％。
  10. 根据权利要求1所述的生物质循环流化床锅炉掺烧燃煤飞灰方法，其特征在于：所说的步骤2)和步骤3)中，燃煤飞灰颗粒在密相燃烧区(13)的反应停留时间控制在0.8～1.5s。
  11. 根据权利要求1所述的生物质循环流化床锅炉掺烧燃煤飞灰方法，其特征在于：所说的步骤2)和步骤3)中，燃煤飞灰颗粒在密相燃烧区(13)的反应停留时间控制在1.0～1.2s。
  12. 根据权利要求1所述的生物质循环流化床锅炉掺烧燃煤飞灰方法，其特 征在于：所说的步骤4)中，燃煤飞灰颗粒中剩余的残炭黑芯在稀相燃烧区(14)的反应停留时间控制在5.2～6.5s。
  13. 根据权利要求1所述的生物质循环流化床锅炉掺烧燃煤飞灰方法，其特征在于：所说的步骤4)中，燃煤飞灰颗粒中剩余的残炭黑芯在稀相燃烧区(14)的反应停留时间控制在5.5～6.0s。
  14. 一种为实现权利要求1所述方法而专门设计的生物质循环流化床锅炉掺烧燃煤飞灰设备，包括与生物质循环流化床锅炉(9)配套使用的燃煤飞灰储存仓(1)，其特征在于：
    所述燃煤飞灰储存仓(1)的底部出料口通过旋转给料装置(2)与喷射器(3)的粉料输入端相连，所述喷射器(3)的空气输入端通过止回阀(4)与鼓风机(5)相连，所述喷射器(3)的悬浮物喷口与传输管道(6)的一端相连，所述传输管道(6)的另一端从生物质循环流化床锅炉(9)的底部风室(10)进入其中、并穿过均布有风帽(12)的布风板(11)与底饲耐磨喷嘴(8)相连，所述底饲耐磨喷嘴(8)位于布风板(11)上方的密相燃烧区(13)中。
  15. 根据权利要求14所述的生物质循环流化床锅炉掺烧燃煤飞灰设备，其特征在于：所述底饲耐磨喷嘴(8)的喷射口位置高于所述布风板(11)上的风帽(12)的出风口位置500～800mm。
  16. 根据权利要求14或15所述的生物质循环流化床锅炉掺烧燃煤飞灰设备，其特征在于：所述底饲耐磨喷嘴(8)的喷射方向与水平面的夹角为0～25°。
  17. 根据权利要求14或15所述的生物质循环流化床锅炉掺烧燃煤飞灰设备，其特征在于：所述底饲耐磨喷嘴(8)的数量为2～6个，均匀布置在所述布风板(11)上方，各个底饲耐磨喷嘴(8)通过支管与传输管道(6)的另一端相连。
  18. 根据权利要求14或15所述的生物质循环流化床锅炉掺烧燃煤飞灰设备，其特征在于：所述传输管道(6)包括水平管段和垂直管段，所述水平管段和垂直管段之间通过耐磨弯头(7)过渡相连。
  19. 根据权利要求14或15所述的生物质循环流化床锅炉掺烧燃煤飞灰设备，其特征在于：所述鼓风机(5)为罗茨风机，并列设置有两套，其中一套罗茨风机上设置有放空阀(15)。
  20. 根据权利要求14或15所述的生物质循环流化床锅炉掺烧燃煤飞灰设备，其特征在于：所述旋转给料装置(2)为变频器远程控制的旋转给料阀。
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