CN111102565A - Method for controlling emission of pollutants generated by mixed combustion of coal slime - Google Patents

Method for controlling emission of pollutants generated by mixed combustion of coal slime Download PDF

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Publication number
CN111102565A
CN111102565A CN201911292364.0A CN201911292364A CN111102565A CN 111102565 A CN111102565 A CN 111102565A CN 201911292364 A CN201911292364 A CN 201911292364A CN 111102565 A CN111102565 A CN 111102565A
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coal slime
coal
temperature
boiler
bed
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CN201911292364.0A
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刘彦鹏
高智溥
张孝勇
白公宝
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Thermal Power Generation Technology Research Institute of China Datang Corporation Science and Technology Research Institute Co Ltd
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Thermal Power Generation Technology Research Institute of China Datang Corporation Science and Technology Research Institute Co Ltd
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Priority to CN201911292364.0A priority Critical patent/CN111102565A/en
Publication of CN111102565A publication Critical patent/CN111102565A/en
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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
    • 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
    • F22B31/0069—Systems therefor
    • 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
    • F22B31/08—Installation of heat-exchange apparatus or of means in boilers for heating air supplied for combustion
    • 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
    • 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
    • F23C10/20—Inlets for fluidisation air, e.g. grids; Bottoms
    • 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
    • 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
    • F23C10/28—Control devices specially adapted for fluidised bed, combustion apparatus
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
    • 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

Abstract

The invention relates to a method for controlling emission of pollutants generated by mixed combustion of coal slime, which comprises the following steps: the method comprises the steps of adopting a 300MW circulating fluidized bed boiler to mix and burn coal slime for power generation, controlling the bed temperature to be 850-900 ℃, and controlling SO (sulfur oxide) content by micro-adjusting limestone input quantity after the coal slime is input2Discharge capacityWithin the specified range; secondary air is injected into the hearth along different positions of the bed height for grading air distribution to reduce NOxDischarging; and an electric dust collector is adopted for dust removal so as to ensure that the final smoke dust emission concentration is in a specified range. The invention can improve the coal slime treatment capacity, reduce the pollutant discharge and obviously improve the energy-saving and emission-reducing effects.

Description

Method for controlling emission of pollutants generated by mixed combustion of coal slime
Technical Field
The invention belongs to the technical field of thermal power generation, and particularly relates to a method for controlling emission of pollutants generated by coal slime mixed combustion power generation.
Background
Coal slurry is a waste product of coal washing processes and, because of its difficult handling and utilization, is deposited or filled into abandoned mines in many situations. The stacked coal slime occupies a large amount of land resources, and the coal slime can be lost when meeting water, is air-dried and flies, causes serious pollution to the environment, and has a harm degree larger than that of coal gangue which is washing waste; the coal slime filled in the mine causes the waste of a large amount of low-quality energy.
The coal slime is used for generating power, so that the problem of environmental pollution caused in the process of accumulating and storing the coal slime can be solved, and low-quality energy waste caused by filling the coal slime into a waste mine can be avoided.
Circulating Fluidized Bed (CFB) boilers serve as a new generation clean power generation technology and have the characteristics of wide fuel adaptability and low pollutant emission. The coal slime mixed burning clean power generation technology of the large circulating fluidized bed boiler is developed, the coal slime treatment capacity is large, the pollutant discharge is low, the energy-saving and emission-reducing effects are more obvious, huge economic benefits and good social benefits can be brought to coal mine enterprises, and the method has strategic significance for building resource-saving and environment-friendly power generation enterprises.
Disclosure of Invention
The invention aims to provide a method for controlling emission of pollutants generated by blending and burning coal slime so as to improve the coal slime treatment capacity, reduce the emission of pollutants and obviously improve the effects of energy conservation and emission reduction.
The invention provides a method for controlling emission of pollutants generated by mixed combustion of coal slime, which comprises the following steps:
the method comprises the steps of adopting a 300MW circulating fluidized bed boiler to mix and burn coal slime for power generation, controlling the bed temperature to be 850-900 ℃, and controlling SO (sulfur oxide) content by micro-adjusting limestone input quantity after the coal slime is input2The discharge amount is in a specified range;
secondary air is injected into the hearth along different positions of the bed height for grading air distribution to reduce NOxDischarging;
and an electric dust collector is adopted for dust removal so as to ensure that the final smoke dust emission concentration is in a specified range.
Further, the power generation by blending and burning the coal slime by adopting the 300MW circulating fluidized bed boiler comprises the following steps:
the circulating fluidized bed boiler with a double-air-distribution plate structure is adopted to increase the penetration capacity of secondary air;
4 external heat exchangers are arranged to facilitate the arrangement of a heating surface and the adjustment of bed temperature;
the evaporation heating surface of the boiler adopts a membrane type water-cooled wall and a water-cooled wall extension wall structure, and a high-temperature superheater, a low-temperature reheater, a high-low temperature economizer and a rotary air preheater are sequentially arranged on a tail convection flue;
a conical valve is arranged at the inlet of the external heat exchanger, and the distribution of the circulating material separated by the heat-insulating cyclone separator is controlled by adjusting the opening degree of the conical valve so as to adjust the bed temperature and the reheated steam temperature;
arranging a high-temperature reheater and a low-temperature superheater in the two external heat exchangers close to the front of the furnace for adjusting the temperature of reheated steam;
arranging a medium-temperature superheater I and a medium-temperature superheater II in the two external heat exchangers close to the furnace to adjust the bed temperature;
each boiler is provided with 4 wind-water combined slag coolers for recovering heat.
Further, the power generation by adopting the mixed burning of the coal slime of the 300MW circulating fluidized bed boiler further comprises the following steps:
the coal slime is conveyed by adopting a double-cylinder plunger pump with an S pendulum and a coal slime gun with an atomization function, compressed air is introduced to atomize the coal slime when the coal slime gun runs so as to burn off the coal slime, and wall box sealing air is arranged so as to prevent the gun head from being burnt out;
controlling the water content of the coal slurry entering the coal slurry conveying system to be about 30%;
the conveying pipeline of the coal slime conveying system is provided with a discharging spiral device and a coal slime bin stirring device, and the discharging spiral device and the coal slime bin stirring device are used for homogenizing the water content of coal slime to improve discharging spiral output.
Further, the power generation by adopting the mixed burning of the coal slime of the 300MW circulating fluidized bed boiler further comprises the following steps:
adopting a low-position coal slime feeding mode, and driving coal slime into a hearth through a coal slime gun on a side wall or a front wall with a set height away from an air distribution plate;
and primary cold air is injected into the coal slime gun when the coal slime gun is stopped, so that the coal slime gun is prevented from being blocked.
Further, the power generation by adopting the mixed burning of the coal slime of the 300MW circulating fluidized bed boiler further comprises the following steps:
after the coal slime is put into the circulating fluidized bed boiler to operate, adjusting the opening degree of a conical valve, adjusting the proportion of primary air and secondary air and controlling the bed temperature to be about 880 ℃ so as to reduce the carbon content of bottom slag;
when the pressure difference at the upper part of the hearth is detected to be higher than a set value, the fine ash is discharged by an external bed or a material return valve for control;
the opening degree of the external bed conical valve is adjusted, so that the smoke temperature at the outlet of the cyclone separator is in a normal value range, and the temperature of the return valve is in a normal value range, and the coking of the return valve is avoided.
By means of the scheme, the coal slime treatment capacity can be improved, the pollutant emission can be reduced, and the energy-saving and emission-reducing effects can be obviously improved through the coal slime mixed combustion power generation pollutant emission control method.
The foregoing is a summary of the present invention, and in order to provide a clear understanding of the technical means of the present invention and to be implemented in accordance with the present specification, the following is a detailed description of the preferred embodiments of the present invention.
Detailed Description
The following examples are given to further illustrate the embodiments of the present invention. The following examples are intended to illustrate the invention but are not intended to limit the scope of the invention.
The embodiment provides a method for controlling emission of pollutants generated by mixed combustion of coal slime, which comprises the following steps:
the method comprises the steps of adopting a 300MW circulating fluidized bed boiler to mix and burn coal slime for power generation, controlling the bed temperature to be 850-900 ℃, and controlling SO (sulfur oxide) content by micro-adjusting limestone input quantity after the coal slime is input2The discharge amount is in a specified range;
secondary air is injected into the hearth along different positions of the bed height for grading air distribution to reduce NOxDischarging;
and an electric dust collector is adopted for dust removal so as to ensure that the final smoke dust emission concentration is in a specified range.
In this embodiment, the power generation by using the mixed burning of coal slime of the 300MW circulating fluidized bed boiler comprises:
the circulating fluidized bed boiler with a double-air-distribution plate structure is adopted to increase the penetration capacity of secondary air;
4 external heat exchangers are arranged to facilitate the arrangement of a heating surface and the adjustment of bed temperature;
the evaporation heating surface of the boiler adopts a membrane type water-cooled wall and a water-cooled wall extension wall structure, and a high-temperature superheater, a low-temperature reheater, a high-low temperature economizer and a rotary air preheater are sequentially arranged on a tail convection flue;
a conical valve is arranged at the inlet of the external heat exchanger, and the distribution of the circulating material separated by the heat-insulating cyclone separator is controlled by adjusting the opening degree of the conical valve so as to adjust the bed temperature and the reheated steam temperature;
arranging a high-temperature reheater and a low-temperature superheater in the two external heat exchangers close to the front of the furnace for adjusting the temperature of reheated steam;
arranging a medium-temperature superheater I and a medium-temperature superheater II in the two external heat exchangers close to the furnace to adjust the bed temperature;
each boiler is provided with 4 wind-water combined slag coolers for recovering heat.
In this embodiment, the power generation by using the mixed burning of the coal slime of the 300MW circulating fluidized bed boiler further comprises:
the coal slime is conveyed by adopting a double-cylinder plunger pump with an S pendulum and a coal slime gun with an atomization function, compressed air is introduced to atomize the coal slime when the coal slime gun runs so as to burn off the coal slime, and wall box sealing air is arranged so as to prevent the gun head from being burnt out;
controlling the water content of the coal slurry entering the coal slurry conveying system to be about 30%;
the conveying pipeline of the coal slime conveying system is provided with a discharging spiral device and a coal slime bin stirring device, and the discharging spiral device and the coal slime bin stirring device are used for homogenizing the water content of coal slime to improve discharging spiral output.
In this embodiment, the power generation by using the mixed burning of the coal slime of the 300MW circulating fluidized bed boiler further comprises:
adopting a low-position coal slime feeding mode, and driving coal slime into a hearth through a coal slime gun on a side wall or a front wall with a set height away from an air distribution plate;
and primary cold air is injected into the coal slime gun when the coal slime gun is stopped, so that the coal slime gun is prevented from being blocked.
In this embodiment, the power generation by using the mixed burning of the coal slime of the 300MW circulating fluidized bed boiler further comprises:
after the coal slime is put into the circulating fluidized bed boiler to operate, adjusting the opening degree of a conical valve, adjusting the proportion of primary air and secondary air and controlling the bed temperature to be about 880 ℃ so as to reduce the carbon content of bottom slag;
when the pressure difference at the upper part of the hearth is detected to be higher than a set value, the fine ash is discharged by an external bed or a material return valve for control;
the opening degree of the external bed conical valve is adjusted, so that the smoke temperature at the outlet of the cyclone separator is in a normal value range, and the temperature of the return valve is in a normal value range, and the coking of the return valve is avoided.
By the method for controlling the emission of the pollutants generated by the coal slime mixed combustion power generation, the coal slime treatment capacity can be improved, the emission of the pollutants can be reduced, and the energy-saving and emission-reducing effects can be obviously improved.
The present invention is described in further detail below.
1. Coal slime conveying system
Coal slime is a high-moisture emission substance which is separated in the coal washing process and mainly comprises coal particles and contains various impurities, and generally is poor-quality bituminous coal. Coal slime generally has the characteristics of fine granularity, high water content, strong water retention, high ash content, lower calorific value and larger viscosity. The coal washing slurry is a slurry between solid and liquid, and the flow in the pipe has the characteristics of non-Newtonian fluid, so that the conveying is difficult, and secondary pollution is easily caused.
The main function of the coal slime conveying system is to continuously and stably convey the coal slime into a hearth without pollution. The coal slurry transport system generally comprises: the system for feeding the side wall low-level coal slime is also provided with a special coal slime (spraying) gun. The coal slurry pretreatment system, the coal slurry pump and the coal slurry gun become key components of the whole coal slurry conveying system.
The pumping of the coal slurry is difficult due to the characteristics of high water-holding capacity and high viscosity of the coal slurry. The CFB unit burning coal slime generally adopts a screw pump, an extrusion pump and a plunger pump for pumping. The pumping system of the coal slime plunger pump consists of a coal slime bin, a bin bottom sliding frame, a washing water pressurizing pump and four coal slime pumping pipelines. Each pipeline comprises a discharge screw, a mixing hopper, a coal slime moisture adjusting system, a coal slime pump, an impurity removing device, a coal slime gun and the like. The plunger pump has higher outlet pump pressure and stronger coal slime conveying capacity.
The water content of the coal slime has great influence on the flow resistance of the coal slime in a pipeline, and is an important parameter related to whether a coal slime conveying system can normally operate. The lower limit that the moisture content of coal slime should be controlled under the condition that can guarantee conveying system normal work, and the coal slime moisture content that this embodiment will get into the coal slime pump is about 30% usually.
The coal slime gun is generally directed at a low-position coal slime feeding system, and is a coal slime conveying pipeline generally for a high-position coal slime feeding system, so that the specially designed coal slime gun is not needed. The coal slurry gun mainly comprises a gun body, a ball valve, a gate valve, a safety valve and the like. Compressed air is introduced to atomize the coal slime during the operation of the coal slime gun, so that the coal slime is burnt out conveniently, and wall box sealing air is further arranged to prevent the gun head from being burnt out. The embodiment adopts a double-cylinder plunger pump with an S pendulum and a coal slime spray gun with an atomization function to convey coal slime.
The output of the discharging screw is directly related to the water content of the coal slime in the coal slime bin. Can even coal slime moisture content through increasing coal slime storehouse agitating unit to improve the spiral of unloading and exert oneself, also greatly reduced because the excessive risk of leaking of the spiral of unloading that leads to of adding water in the coal slime storehouse. The water content of the coal slime is also an important parameter for commissioning the coal slime. The high water content can cause the boiler loss to increase, which is not economical; too low water content can result in unsmooth coal slime delivery and gun blockage. The water content of the coal slime after being added with water through the small storage bin is controlled to be 30 percent, which is more suitable.
2. Coal slurry feeding mode
The difference of the coal slime feeding inlet positions has great influence on whether the coal slime can normally and stably participate in combustion in the furnace. The boiler that burns the coal slime at present mainly has two kinds of coal slime modes of giving into: a high-position coal slime feeding mode and a low-position coal slime feeding mode.
The high-position coal slime is fed into the furnace from the top of the boiler to form block falling. The lump coal slime falls, is dried and bursts while being combusted, and becomes small blocks when falling to a dense-phase zone with higher particle concentration to participate in the different-weight combustion in the furnace. The high-order coal slime feeding mode is in the negative pressure area at the outlet of the hearth, and the requirement on sealing is not high. The high-position coal slime feeding mode is to prevent the coal slime from being too large, and if the large coal slime cannot be cracked into fine coal slime clusters after reaching a dense-phase region, the coal slime clusters are directly accumulated on an air distribution plate, and finally the fluidization problem is caused.
The low-position coal slime feeding mode is relative to the high-position coal slime feeding mode. In a general low-position coal slime feeding mode, a coal slime feeding inlet is arranged on a side wall or a front wall which is at a certain height away from an air distribution plate, and the coal slime is pumped into a hearth through a special coal slime gun. Because the coal slurry gun is usually arranged in the dense-phase region of the hearth and is positioned in the positive pressure section of the hearth, certain requirements are required for the sealing air of the coal slurry gun penetrating through the wall.
The coal slime gun adopting the low-position coal slime feeding mode needs to take anti-blocking measures when the operation is stopped, such as driving primary cold air and the like, so that the blockage of the coal slime gun is prevented. The atomized air of the coal slime gun can be scattered into the coal slime, and the deficiency of the feeding mode of the furnace top is avoided.
3. Influence of coal slurry mixing and burning on boiler operation parameters
The circulating fluidized bed boiler for burning coal slime with 300MW in the embodiment adopts the Alstom double air distribution plate technology, so that the problem of insufficient penetration capacity of secondary air is solved; 4 external heat exchangers are arranged to solve the problem that the arrangement of a heating surface and the adjustment of bed temperature are difficult along with the increase of the capacity of the boiler. The boiler evaporation heating surface is a membrane type water-cooled wall and a water-cooled wall extension wall structure, and a high-temperature superheater, a low-temperature reheater, a high-low temperature economizer and a rotary air preheater are sequentially arranged on a tail convection flue. The inlet of the external heat exchanger is provided with a conical valve, and the distribution of the circulating material separated by the heat-insulating cyclone separator is controlled by adjusting the opening degree of the conical valve, so that the temperature of the bed and the temperature of the reheated steam are adjusted. A high-temperature reheater and a low-temperature superheater are arranged in the two external heat exchangers close to the front of the furnace and used for adjusting the temperature of reheated steam; middle temperature superheaters I and II are arranged in the two external heat exchangers close to the rear of the furnace to adjust the bed temperature. Each boiler is provided with 4 wind-water combined slag coolers for recycling part of heat. The coal is designed to be gangue, coal slime, medium coal 45 percent, medium coal 15 percent and medium coal 40 percent.
1) Influence and control of mixed burning coal slime on bed temperature
The bed temperature is the material bed temperature of the fluidized material in the dense phase zone of the CFB boiler, reflects the relationship between heat absorption and heat release in the boiler and is an important parameter in the operation of the CFB boiler. When the temperatures of the lower part, the middle part and the upper part of the dense-phase zone are uniformly and stably between 850-920 ℃, the fluidization quality in the whole furnace is good, and the combustion working condition is normal; when the local temperature is too high or too low, the fluidization condition in the furnace is poor, and the adjustment of parameters such as air quantity and the like needs to be paid attention. The low bed temperature can cause the efficiency of the boiler to be reduced, the boiler is unstable to operate and is easy to extinguish fire; the over-high bed temperature is easy to cause coking at the hearth, the material return valve and other parts and stop the furnace. Too low or too high bed temperature also leads to a decrease in desulfurization efficiency in the furnace, and too high bed temperature also leads to a rapid increase in the amount of NOx produced. Therefore, the method has important significance for stable, low-pollution and efficient combustion of the CFB boiler by mastering the bed temperature change characteristic of the coal slime after the coal slime is sprayed.
When the coal slurry enters the fluidized bed boiler, the coal slurry undergoes water evaporation, volatile matter separation, ignition and coke combustion. It can be seen from the combustion process of the coal slime after entering the furnace that the negative pressure of the furnace chamber changes due to the rapid evaporation of the water at the moment of the coal slime input, and then the bed temperature drops. For a large-scale circulating fluidized bed boiler, because more materials are in the boiler, when the coal slime input amount is small, the instantaneous reduction amplitude of the bed temperature is small; however, for small CFB boilers, this effect is significant, and can be reduced by up to 100 ℃. When the bed temperature rises again and the oxygen content begins to drop, the coal slime is shown to be driven into the hearth and begins to burn.
The field test was performed on a 300MWCFB boiler. The test is carried out under 260MW load, the opening degree of the conical valve is kept unchanged, the negative pressure of the hearth outlet is stabilized at minus 100 +/-50 Pa, the oxygen content is stabilized at 3.35% +/-1%, and the bed pressure is stabilized at 9-11 kPa. The bed temperature at the lower part, the middle part and the upper part of the dense-phase region are all reduced along with the increase of the sprayed amount of the coal slime. The bed temperature was reduced from 880 ℃ to 850 ℃ when a coal slurry quantity of 40m3/h (corresponding to 30% of the coal charge) was injected, compared with when no coal slurry was injected.
Therefore, the coal slime entering a hearth is not favorable to bursting rapidly due to the temperature difference effect at a lower bed temperature, and the quantity of the agglomerated coal slime is increased, so that the carbon content of bottom slag is increased. Therefore, after the coal slurry is put into the reactor, the operator needs to adjust and control the bed temperature within a normal range through combustion, for example, means such as adjusting the opening of a conical valve and the proportion of primary air and secondary air are adopted. Tests show that when the bed temperature is controlled to be about 880 ℃, the carbon content of the bottom slag can be obviously reduced.
2) Influence and control of mixed burning coal slime on bed pressure
Bed pressure is another important monitored parameter in the operation of a CFB boiler. The bed pressure generally refers to the pressure installed at a position about 300mm above the grid plate, and the value can represent the height of the bed material in the furnace. The bed pressure is high, which indicates that the bed material in the furnace is more, and is beneficial to stable combustion, reducing the influence of coal breakage on the stable operation of the boiler and reducing the content of slag-discharging combustible substances; but the bed height can increase the primary air pressure head, the power consumption is increased, and the possibility of the bed turnover of the split hearth is greatly increased. Thin bed material, low bed pressure, poor boiler load capacity, high bed temperature and easy coking. Therefore, the method has important significance for stable and efficient combustion of the CFB boiler by mastering the bed pressure change characteristic of the coal slime after being sprayed.
The bed pressure of the CFB boiler is mainly controlled by means of adjusting the slag discharge. After the coal slime is put into the boiler, the raw coal amount entering the boiler is reduced, and the generated bottom slag amount is correspondingly reduced, so that the slag discharge amount of the boiler is reduced. The coal slime system in stable operation can alleviate the pressure of the boiler deslagging system, and can even realize the continuous and stable operation of zero-deslagging for a small-sized different-weight CFB boiler in a high-position coal slime feeding mode. Therefore, the ash-slag ratio is changed after the coal slime is put into the device.
Maximum blending combustion proportion of single-side coal slime
Considering the characteristic of the double-air-distribution-plate structure that a CFB unit has a turning bed, a single-side maximum coal slime mixing and burning proportion test is carried out to test the maximum mixing and burning proportion condition of the coal slime under the worst condition. Taking a 300MWCFB unit as an example, putting #3 and #4 coal slime guns into the unit at one side under the working condition of 200MW, wherein the output is 16.0m3H and 17.0m3H, total 33m3The ratio of the mixed combustion is 30% corresponding to 40 t/h. By means of adjusting the air distribution bias of the two beds, the opening degree of the conical valve, the opening degree of the slag discharge inlet valve and the like, the unit continuously and stably operates for 4 hours under the working condition of 200MW load, and the bed temperature, the bed pressure, the steam temperature and the steam pressure are stable.
Influence on differential pressure in upper part of furnace
For a large CFB boiler, the furnace head differential pressure △ P2Is also a very important monitoring parameter, the furnace upper differential pressure △ P2Representing the circulating ash flow from the combustion chamber to the separator, reflecting the grain size distribution in the furnace, which is an important parameter for guiding operation and power coal blending, △ P after coal slurry is put into the furnace2In the test process, the negative pressure at the outlet of a hearth is stabilized at minus 100 +/-50 Pa, the oxygen content is stabilized at 3.35 +/-1%, the bed temperature is maintained at 870-890 ℃, and the bed pressure is stabilized at 9-11 kPa2Stabilizes at about 0.85kPa, and △ P is carried out along with the increase of the coal slurry injection amount2Increased higher △ P2The heat transfer process in the boiler can be enhanced, and from the viewpoint of increasing the coal slime, the load carrying capacity of a unit is improved, but for a CFB boiler with a split hearth design, △ P is too high2Can cause the problem that the boiler is difficult to control when the bed turnover occurs, so when △ P2When the height is too high, the control is carried out by a means of putting fine ash through an external bed or a material returning valve.
3) Influence of coal slime mixing and burning on operation of induced draft fan
The coal slurry is a high-moisture fuel, and after entering the furnace, the moisture in the coal slurry is quickly evaporated and the volume of the coal slurry is reducedThe rapid expansion causes the increase of the total smoke gas quantity, thereby causing the increase of the current of the induced draft fan. The method is characterized in that a certain 300MWCFB boiler is taken as an example for testing, in the testing process, the negative pressure of the outlet of a hearth is stabilized at minus 100 +/-50 Pa, the oxygen content is stabilized at 3.35% +/-1%, the bed temperature is maintained between 870 and 890 ℃, the bed pressure is stabilized at 9 to 11kPa, an induced draft fan is automatically thrown, and the consistency of the output of the A, B induced draft fan is ensured. The test result shows that: under the working condition of 260MW, when the coal slime is not input, the current of the induced draft fan A is 186A, and when the input amount of the coal slime is 52m3When the current is increased to 198A by the induced draft fan A; the current of the draught fan is also increased almost linearly along with the increase of the amount of the coal slurry entering the furnace. The same rule exists in the 220MW condition. The phenomenon has reference significance for the selection of the type of the induced draft fan and the selection of the exhaust smoke temperature.
4) Influence of mixed burning coal slime on coal supply system
The coal slurry system which stably operates increases the reliability of a fuel supply system of the boiler and reduces the sensitivity of the boiler to coal breakage of a coal supply line. For the coal feeding mode of the long return leg of the coal feeding line, the coal slime system can also accelerate the response speed of the unit to the load change, and make up the defect of the response lag of the coal feeding line. Taking a certain 300MWCFB unit as an example, because a secondary coal supply line for feeding coal by adopting a return leg is long, about 8 minutes is required from the sending of a coal supply instruction to the change of steam pressure; the coal slurry is approximate to incompressible fluid, the working frequency of the plunger pump is immediately increased after the coal slurry adding instruction is sent out, the coal slurry can enter the furnace quickly, the time is shorter than that of a coal supply line, only about 4 minutes is needed from the instruction sending to the steam pressure changing, and the response load speed is much faster than that of the coal supply line. Therefore, the response quality of AGC can be greatly improved through the mutual cooperation of the air distribution, the coal slime and the coal supply line.
5) Influence of coal slime on separator outlet smoke temperature
The outlet smoke temperature of the cyclone separator is the most intuitive parameter for judging whether the material external circulation system is normal or not, and has important significance for the safe operation of the CFB boiler. The low-position coal slime feeding mode is different from the furnace top coal slime feeding mode, the coal slime has relatively long residence time in the furnace, and the continuous combustion share after entering the cyclone separator is relatively small, so that the phenomena of separator overtemperature and afterburning of a tail flue are not easily caused like the furnace top coal slime feeding mode. In this way, the relationship between the temperature of the flue gas at the outlet of the cyclone separator and the temperature of the bed is more close. Because the bed temperature can be adjusted through the opening degree of the conical valve of the external bed, the temperature of the smoke at the outlet of the cyclone separator can be ensured to be in a normal value range through operation adjustment, and the temperature of the feed back valve can not be over-heated, thereby avoiding the problem of coking of the feed back valve. The high-position coal slurry feeding mode may have the problems.
4. Influence of coal slime mixing combustion on boiler economic operation
1) Influence of mixed burning coal slime on carbon content of fly ash
The carbon content of the fly ash can reflect the combustion condition in the boiler, directly influences the boiler efficiency and is data which is mainly concerned in the daily production of a power plant. The coal slime has high water content and volatile component content, and can be rapidly burst, volatilized and analyzed out and ignited after entering the furnace. One part of fine particles with small enough particle size are directly elutriated along with the flue gas and leave a hearth, or are captured by a cyclone separator and participate in external circulation, or directly enter a tail flue to become fly ash; the other part of particles with medium particle size participate in the circulation in the furnace; the remaining agglomerated coal slurry particles may remain in the dense phase zone to participate in fluidized combustion. For the low-position coal slime feeding mode, because the coal slime gun has a certain distance from the outlet of the hearth, the coal slime particles have relatively sufficient residence time in the furnace, and generally the combustion needs to be relatively complete. For the high-position coal slime feeding mode, a part of fine coal slime particles are directly fed into the cyclone separator after the coal slime bursts, and the coal particles which are not captured directly enter the tail flue to become fly ash. The short residence time in the furnace of the particles in the part and the incomplete combustion usually result in high carbon content in the fly ash.
Taking a certain power plant boiler as an example, tests are respectively carried out on three load working conditions of 180MW, 220MW and 260 MW. In the test process, the negative pressure at the outlet of the hearth is stabilized at minus 100 +/-50 Pa, the oxygen content is stabilized at 3.35% +/-1%, the bed temperature is maintained between 870 and 890 ℃, the bed pressure is stabilized at 9 to 11kPa, and the test result shows that: the influence of the coal slime input amount on the carbon content of the fly ash is not obvious, the carbon content of the fly ash is always kept between 1.2 and 2.0 percent under the conditions of different loads and different coal slime input amounts, and the combustion effect is good. For the boiler, the height of a coal slime gun from the top of the boiler is about 30m, the fluidizing air speed in the boiler is 5-5.5 m/s, the coal slime gun can fly out of a hearth at one time, the average residence time of coal slime particles which are not captured by a cyclone separator in the boiler is about 6s, the combustion time of the coal slime particles is relatively sufficient, and the oxygen supplement is timely and sufficient due to the design structure of a split hearth, so that the carbon content of fly ash is not high. Therefore, the low fly ash carbon content is benefited from the split hearth structure of the underpants legs on one hand, and is mainly benefited from the low-level coal slime feeding mode on the other hand. For the feeding mode of the high-position coal slime on the furnace roof, the carbon content of fly ash when the coal slime is mixed and burnt is different from that when the coal slime is not mixed and burnt by about 2 percent, which is mainly caused by insufficient residence time in the furnace.
2) Influence of mixed burning coal slime on carbon content of bottom slag
The carbon content of the bottom slag can also reflect the combustion condition in the boiler, directly influences the boiler efficiency and is data which is focused on in the daily production of the power plant. The slag discharge of the CFB boiler is closely related to the particle composition in the dense-phase area of the hearth. Generally, it is considered that coal slime agglomerates can "float" on the upper part of bed materials to participate in combustion due to relatively low density, but for the combustion of the fuel such as middlings and coal gangue, the density difference is relatively small, and is not as obvious as the density difference when the coal slime and the coal gangue are simply combusted, so that the agglomerated coal slime particles can be entrained on the upper part, the middle part and the lower part of the whole dense-phase region to be combusted in a boiling way, and can be also entrained out of a side wall slag discharge port of a hearth, therefore, when the bed temperature is low and the coal slime atomization effect is not good, the agglomerated coal slime proportion is increased, the coal slime discharged out of the hearth is also increased, and the carbon content of bottom slag is increased.
Taking a certain power plant boiler as an example, tests are respectively carried out on three load working conditions of 180MW, 220MW and 260 MW. In the test process, the negative pressure at the outlet of the hearth is stabilized at minus 100 +/-50 Pa, the oxygen content is stabilized at 3.35% +/-1%, the bed temperature is maintained between 870 and 890 ℃, the bed pressure is stabilized at 9 to 11kPa, and the test result shows that: for less than 20m3The coal slime input amount per hour and the carbon content of bottom slag are basically unchanged; along with the great increase of the amount of the coal sludge entering the furnace, the carbon content of the bottom slag also has a remarkable trend of increasing, particularly at 180MUnder the condition of W, coal slime is burnt under relatively low load, the carbon content of bottom slag is rapidly increased to 5.5 percent (corresponding to the coal slime content of 40 m) from 2.2 percent when the coal slime is not added3H). After entering the hearth, the coal slime is subjected to the processes of rapid evaporation of water, bursting of coal slime clusters, volatilization analysis to generate ignition, coke combustion and the like in sequence. As the amount of coal slime entering the furnace increases, more and more coal slime groups are not cracked and left in the dense-phase region to participate in fluidized combustion, and finally are discharged out of a hearth from an inlet of a slag cooler. The increase in the carbon content of the bottom ash is mainly due to this portion of unburnt agglomerated coal slurry. Because coal slime rifle position is perpendicular adjacent with row cinder notch position, consequently unburnt conglomeration coal slime is direct to be discharged from cold sediment ware, leads to the bottom sediment carbonaceous content to increase rapidly.
3) Influence of coal slime on smoke exhaust temperature
The influence of the coal slime on the exhaust gas temperature after the coal slime is put into the device is also very obvious. Because the ash content of the coal slime is high and the granularity of most particles is less than 0.5mm, the share of fly ash can be greatly increased after the coal slime is put into use. The ash content of the coal slime is generally very viscous, and the acceleration of the ash deposition on the heating surface can be caused after the coal slime enters a tail flue, so that the exhaust gas temperature is increased. In order to obtain a relatively ideal main steam temperature, the inlet flue gas temperature of the air preheater is reduced to ensure the safe operation of the air preheater, and the smoke exhaust temperature is reduced, so that the steam soot blowing frequency is obviously increased along with the increase of the coal slime. The rise of the exhaust gas temperature is also related to the fact that ash and moisture in the coal slime carry certain heat to enter the tail flue and change the heat load distribution relation between the heating surfaces in the furnace and the heating surfaces of the tail flue. Taking a power plant boiler as an example, under the working condition of 260MW, the unit is not thrown with coal slime and is thrown with 40m in the same soot blowing interval3The change of the exhaust gas temperature along with the time can be seen when coal slime is added, and coal slime is not added and 40m is added3And the exhaust gas temperature is increased by more than 5 ℃ under the condition of coal slime per hour. And after the coal slurry is put into the boiler, the exhaust gas temperature is difficult to recover to the condition before the coal slurry is put into the boiler even if the same soot blowing frequency and soot blowing strength are adopted.
4) Influence of mixed burning coal slime on boiler thermal efficiency
The influence on the carbon content of ash and the exhaust gas temperature after the coal slime is mixed and burnt is finally shown on the influence on the thermal efficiency of the boiler. The influence of the coal slurry on the thermal efficiency of the boiler is greatly related to the characteristics of the fuel entering the boiler. The decrease in the thermal efficiency of the boiler results in an increase in the consumption of power coal, but this is not to say that less or no coal slurry is used in order to decrease the consumption of coal. The final benefit of the power plant is measured by the difference between the price of the fuel fed into the furnace and the price of the power generation cost, namely the final net profit. Because the price of the coal slime is far lower than the price of the coal mixture entering the boiler, the reduction of the price of the total fuel entering the boiler cannot be offset by the increase of the total fuel quantity entering the boiler, so the actual coal slime usage amount of the power plant needs to burn the coal slime as much as possible according to the actual operation condition of the boiler, and only the profit growth rate obtained by unit electric quantity is reduced along with the increase of the coal slime input proportion.
5. Influence of coal slurry on pollutant discharge characteristics
1) Sulfur dioxide emission control
As a new generation clean power generation technology, the circulating fluidized bed boiler has the main advantage that the desulfurizing agent can be added in the boiler for desulfurization. The fluidized bed combustion desulfurization is that coal and desulfurizer are added into the bed layer of combustion chamber, SO that the fuel and desulfurizer are fluidized and turbulently mixed, and the desulfurizer is calcined to form energy capable of mixing with SO2Sulfur fixing agent of reaction, reduction of S02And (5) discharging. In-furnace desulfurization as reduction S02An efficient way of discharging is particularly suitable for fluidized bed combustion, since this combustion mode provides an ideal desulfurization environment: desulfurizing agent and SO2Can be fully mixed and contacted, has proper combustion temperature, and contains desulfurizer and SO2The residence time in the furnace is long.
The coal slime has high ash content and the ash content contains abundant alkali metal oxides CaO, MgO and the like, SO the added coal slime has certain self-desulfurization capacity, and SO can be controlled by adjusting the input amount of limestone2The amount of emissions of (a) is within the range stipulated by the country. Taking a certain power plant boiler as an example, under the working condition of 50% -100% of the load input by coal slime, SO is added2The discharge concentration is not obviously changed, and the discharge amount is more closely related to the temperature of the operating bed. When the bed temperature is controlled to be 850-900 ℃, SO can be completely controlled by micro-adjusting the input amount of limestone after the coal slime is input2The discharge amount is 200mg/dNm3The following (according to GB13233-2003 Standard for emission of atmospheric pollutants for thermal Power plants, this type of units SO2The limiting value of the emission concentration is 400mg/dNm3) And the environmental protection requirement of the unit is met. For the coal slurry burning circulating fluidized bed boiler, the moisture content of the flue gas is high (about 10 percent), which can cause the dew point temperature of the flue gas to rise if SO in the flue gas2The high content of the corrosion inhibitor is easy to cause low-temperature corrosion of the heated surface at the tail part. Therefore, the SO is more strictly controlled for the units2The emission concentration of (c).
2) NOx emission control
Low nitrogen oxide (NOx) emissions is another important advantage of circulating fluidized bed boilers as a new generation of clean power generation technology. In the mechanism of NOx formation, in coal-fueled combustion plants, there are mainly 2 types of NOx formed: namely thermal NOx and fuel NOx. Wherein, thermal NOx is N in air2The fuel type NOx is generated by oxidation at high temperature, and is an organic nitrogen compound in the fuel and is generated by oxidation in the combustion process. The generation amount of nitrogen oxides is most closely related to the temperature of the hearth. Therefore, how to control the fuel type NO by means of combustion regulation or the likexIt is more important. The graded air distribution is low NO of CFB boilerxYet another important means of venting. The dense phase zone is basically in an anoxic combustion state, secondary air is injected into the hearth along different positions of the bed height to realize graded air distribution, which proves that NO is reducedxAn effective means of (1). Taking a certain power plant boiler as an example, the opening degree of a conical valve is adjusted to keep the temperature of an operating bed at about 880 ℃, primary air accounts for 30-40% of the total air volume, and outer secondary air accounts for about 30% of the total secondary air, so that NO can be convertedxThe discharge amount is stably controlled at 200mg/dNm3The following (according to GB13233-2003 'emission Standard for atmospheric pollutants for thermal Power plants', No for this type of unitsxThe emission concentration limit is 450mg/dNm3) And the environmental protection requirement of the unit is completely met.
3) Soot emission concentration control
The smoke dust emission concentration is an important pollutant emission monitoring index in a boiler of a coal-fired power plant, so the performance of electric dust removal is more and more important. Coal (coal)The ash content in the mud is high, and most of the burnt ash escapes from the hearth in the form of fly ash, so that the dust concentration in the smoke can be increased. In addition, the moisture content in the flue gas is higher, and the electric dust removal operation can be influenced when a large proportion of coal slime is mixed and burned. Such as a coal powder furnace of a supercritical unit and a CFB boiler without coal slime, the concentration of the smoke dust at the inlet of the electric dust removal is 30g/Nm3On the left and right, and for a small coal slime CFB boiler without slag discharge and overflow, the concentration of the smoke dust at the inlet of the electric dust removal is as high as 40-50 g/Nm3The design and the type selection of the electric precipitation need to be fully considered.
For a large CFB boiler, the conditions of ash content increase and electric dust removal output increase also exist after coal slime is mixed and burnt. Taking a certain power plant boiler as an example, under the condition of not mixing and burning coal slime, the measured dust concentration of the flue gas at 90 percent of load is 25g/Nm3(ii) a After 30 percent of coal slime is mixed and burnt, the dust concentration of the flue gas reaches 40g/Nm under the same load3The ash amount captured by electric precipitation is obviously increased. Therefore, the model selection of the electric dust removal can meet the change, and the final smoke dust emission concentration can reach the national regulation.
The coal slime is combusted by adopting a large circulating fluidized bed boiler, SO that the treatment capacity of the coal slime is large and SO is high2Low emission of pollutants such as NOx and the like, and obvious energy-saving and emission-reducing effects.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, it should be noted that, for those skilled in the art, many modifications and variations can be made without departing from the technical principle of the present invention, and these modifications and variations should also be regarded as the protection scope of the present invention.

Claims (5)

1. A method for controlling emission of pollutants generated by mixed combustion of coal slime is characterized by comprising the following steps:
the method comprises the steps of adopting a 300MW circulating fluidized bed boiler to mix and burn coal slime for power generation, controlling the bed temperature to be 850-900 ℃, and controlling SO (sulfur oxide) content by micro-adjusting limestone input quantity after the coal slime is input2The discharge amount is in a specified range;
injecting secondary air into the hearth along different positions of the bed height for gradingWind to reduce NOxDischarging;
and an electric dust collector is adopted for dust removal so as to ensure that the final smoke dust emission concentration is in a specified range.
2. The method for controlling pollutant discharge in coal slurry blending combustion power generation according to claim 1, wherein the coal slurry blending combustion power generation by using a 300MW circulating fluidized bed boiler comprises the following steps:
the circulating fluidized bed boiler with a double-air-distribution plate structure is adopted to increase the penetration capacity of secondary air;
4 external heat exchangers are arranged to facilitate the arrangement of a heating surface and the adjustment of bed temperature;
the evaporation heating surface of the boiler adopts a membrane type water-cooled wall and a water-cooled wall extension wall structure, and a high-temperature superheater, a low-temperature reheater, a high-low temperature economizer and a rotary air preheater are sequentially arranged on a tail convection flue;
a conical valve is arranged at the inlet of the external heat exchanger, and the distribution of the circulating material separated by the heat-insulating cyclone separator is controlled by adjusting the opening degree of the conical valve so as to adjust the bed temperature and the reheated steam temperature;
arranging a high-temperature reheater and a low-temperature superheater in the two external heat exchangers close to the front of the furnace for adjusting the temperature of reheated steam;
arranging a medium-temperature superheater I and a medium-temperature superheater II in the two external heat exchangers close to the furnace to adjust the bed temperature;
each boiler is provided with 4 wind-water combined slag coolers for recovering heat.
3. The method for controlling emission of pollutants generated by blending and burning coal slime according to claim 2, wherein the generating by blending and burning coal slime by using a 300MW circulating fluidized bed boiler further comprises:
the coal slime is conveyed by adopting a double-cylinder plunger pump with an S pendulum and a coal slime gun with an atomization function, compressed air is introduced to atomize the coal slime when the coal slime gun runs so as to burn off the coal slime, and wall box sealing air is arranged so as to prevent the gun head from being burnt out;
controlling the water content of the coal slurry entering the coal slurry conveying system to be about 30%;
the conveying pipeline of the coal slime conveying system is provided with a discharging spiral device and a coal slime bin stirring device, and the discharging spiral device and the coal slime bin stirring device are used for homogenizing the water content of coal slime to improve discharging spiral output.
4. The method for controlling emission of pollutants generated by blending and burning coal slime according to claim 3, wherein the generating by blending and burning coal slime by using a 300MW circulating fluidized bed boiler further comprises:
adopting a low-position coal slime feeding mode, and driving coal slime into a hearth through a coal slime gun on a side wall or a front wall with a set height away from an air distribution plate;
and primary cold air is injected into the coal slime gun when the coal slime gun is stopped, so that the coal slime gun is prevented from being blocked.
5. The method for controlling emission of pollutants generated by blending and burning coal slime according to claim 3, wherein the generating by blending and burning coal slime by using a 300MW circulating fluidized bed boiler further comprises:
after the coal slime is put into the circulating fluidized bed boiler to operate, adjusting the opening degree of a conical valve, adjusting the proportion of primary air and secondary air and controlling the bed temperature to be about 880 ℃ so as to reduce the carbon content of bottom slag;
when the pressure difference at the upper part of the hearth is detected to be higher than a set value, the fine ash is discharged by an external bed or a material return valve for control;
the opening degree of the external bed conical valve is adjusted, so that the smoke temperature at the outlet of the cyclone separator is in a normal value range, and the temperature of the return valve is in a normal value range, and the coking of the return valve is avoided.
CN201911292364.0A 2019-12-16 2019-12-16 Method for controlling emission of pollutants generated by mixed combustion of coal slime Pending CN111102565A (en)

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