CN114923170A - Method for adjusting bed temperature of circulating fluidized bed boiler - Google Patents
Method for adjusting bed temperature of circulating fluidized bed boiler Download PDFInfo
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- CN114923170A CN114923170A CN202210690279.5A CN202210690279A CN114923170A CN 114923170 A CN114923170 A CN 114923170A CN 202210690279 A CN202210690279 A CN 202210690279A CN 114923170 A CN114923170 A CN 114923170A
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- 238000000034 method Methods 0.000 title claims abstract description 42
- 239000003245 coal Substances 0.000 claims abstract description 339
- 239000002002 slurry Substances 0.000 claims abstract description 204
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 202
- 238000002485 combustion reaction Methods 0.000 claims abstract description 53
- 230000008569 process Effects 0.000 claims abstract description 7
- 238000002156 mixing Methods 0.000 claims abstract description 5
- 230000002596 correlated effect Effects 0.000 claims abstract description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 21
- 239000003546 flue gas Substances 0.000 claims description 21
- 239000007921 spray Substances 0.000 claims description 21
- 238000006477 desulfuration reaction Methods 0.000 claims description 19
- 230000023556 desulfurization Effects 0.000 claims description 19
- 239000000463 material Substances 0.000 claims description 12
- 239000002245 particle Substances 0.000 claims description 9
- 239000004071 soot Substances 0.000 claims description 9
- 235000019738 Limestone Nutrition 0.000 claims description 7
- 239000000446 fuel Substances 0.000 claims description 7
- 239000006028 limestone Substances 0.000 claims description 7
- 239000007789 gas Substances 0.000 claims description 6
- 239000012071 phase Substances 0.000 claims description 6
- 239000007790 solid phase Substances 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 5
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 claims description 3
- 239000003830 anthracite Substances 0.000 claims description 3
- 238000010531 catalytic reduction reaction Methods 0.000 claims description 3
- 239000002737 fuel gas Substances 0.000 claims description 3
- 230000004927 fusion Effects 0.000 claims description 3
- 239000003077 lignite Substances 0.000 claims description 3
- 238000002360 preparation method Methods 0.000 claims description 3
- 238000005086 pumping Methods 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 238000001035 drying Methods 0.000 claims 1
- 239000003344 environmental pollutant Substances 0.000 abstract description 13
- 231100000719 pollutant Toxicity 0.000 abstract description 13
- 239000000779 smoke Substances 0.000 abstract description 4
- 239000002585 base Substances 0.000 description 12
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 11
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 11
- 239000011575 calcium Substances 0.000 description 11
- 229910052791 calcium Inorganic materials 0.000 description 11
- 239000011593 sulfur Substances 0.000 description 11
- 229910052717 sulfur Inorganic materials 0.000 description 11
- 239000002802 bituminous coal Substances 0.000 description 7
- 239000003250 coal slurry Substances 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 5
- 239000002956 ash Substances 0.000 description 3
- 230000000875 corresponding effect Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 238000006722 reduction reaction Methods 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000006978 adaptation Effects 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 239000012458 free base Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
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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
-
- 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
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The invention provides a method for adjusting the bed temperature of a circulating fluidized bed boiler. The method comprises the following steps: mixing optional coal water slurry and raw coal in a circulating fluidized bed boiler and carrying out combustion reaction; in the combustion reaction process, the ratio of the coal water slurry to the raw coal is adjusted according to the load value of the circulating fluidized bed boiler, and the load value of the circulating fluidized bed boiler is positively correlated with the ratio of the coal water slurry to the raw coal, so that the bed temperature of the circulating fluidized bed boiler is maintained at 800-900 ℃. The invention realizes the flexible adjustment of the bed temperature by adjusting the proportion of the coal water slurry and the raw coal. The bed temperature can be controlled to be 800-900 ℃ in the range of full load to 25% load, the high combustion efficiency is ensured, and meanwhile, the emission of smoke pollutants can be reduced and the cost is reduced; in addition, the method is not limited by the operation load of the circulating fluidized bed boiler, has good bed temperature adjusting capability, is simple and easy to operate, and can reduce the operation risk.
Description
Technical Field
The invention relates to the technical field of clean coal power generation, in particular to a method for adjusting bed temperature of a circulating fluidized bed boiler.
Background
The circulating fluidized bed combustion technology has the advantages of wide fuel adaptation, high utilization rate, low pollutant discharge and the like, and is rapidly popularized and applied in China in recent years. Bed temperature restriction is an important control parameter of the operating economy and environmental protection of the circulating fluidized bed boiler, generally, the suitable bed temperature of the circulating fluidized bed boiler is considered to be in the range of 800-900 ℃, but is influenced by factors such as coal quality and regulation characteristics, the bed temperature of the circulating fluidized bed boiler which is actually operated is bipolarized, namely the bed temperature is high (up to 1050 ℃), the combustion efficiency is high when the load is high, but the pollutant emission is relatively high, and the coking risk exists; the bed temperature is low (the lowest temperature is even only 700 ℃) at the low load, the combustion efficiency is low, and the consumption of limestone desulfurizer and denitration reducer is large.
Engineering practices show that combustion adjustment is carried out by optimizing bed pressure, optimizing primary air and secondary air proportion and other measures, the bed temperature can be adjusted only in a small range, generally only 5-10 ℃, if higher-range bed temperature reduction is to be realized, an external heat exchanger is needed, and corresponding investment is huge.
Disclosure of Invention
The invention mainly aims to provide a method for adjusting the bed temperature of a circulating fluidized bed boiler, which aims to solve the problems that the bed temperature of the circulating fluidized bed boiler can not be adjusted in a large range and more pollutants are generated in the prior art.
In order to accomplish the above object, according to one aspect of the present invention, there is provided a method of adjusting a bed temperature of a circulating fluidized bed boiler, the method comprising: mixing optional coal water slurry and raw coal in a circulating fluidized bed boiler and carrying out combustion reaction; in the combustion reaction process, the ratio of the coal water slurry to the raw coal is adjusted according to the load value of the circulating fluidized bed boiler, and the load value of the circulating fluidized bed boiler is positively correlated with the ratio of the coal water slurry to the raw coal, so that the bed temperature of the circulating fluidized bed boiler is maintained at 800-900 ℃.
Further, in the process of mixing optional coal water slurry and raw coal, the adding amount of the coal water slurry at full load is controlled to be 24-36% of the mass of the raw coal, the adding amount of the coal water slurry at 75-100% of the load is 18-24% of the mass of the raw coal, the adding amount of the coal water slurry at 50-75% of the load is 6-18% of the mass of the raw coal, and the adding amount of the coal water slurry at 25-50% of the load is controlled to be 0-6% of the mass of the raw coal, so that the bed temperature is 850-900 ℃ at full load to 50% of the load and 800-850 ℃ at 50% of the load to 25% of the load.
Furthermore, the adding amount of the coal water slurry at full load is 24-36 percent of the mass of the raw coal, the adding amount of the coal water slurry at 75 percent of the load is 18-24 percent of the mass of the raw coal, the adding amount of the coal water slurry at 50 percent of the load is 6-18 percent of the mass of the raw coal, and the adding amount of the coal water slurry at 25 percent of the load is 0-6 percent of the mass of the raw coal.
Further, the circulating fluidized bed boiler includes: the device comprises a hearth 1, a separator 2, a material returning device 3, a tail flue 4 and an air distribution device 6, wherein the bottom of the hearth 1 is provided with an air inlet, and the side wall of the hearth is provided with a coal feeding port 5, a coal water slurry feeding port 7 and a combustion flue gas outlet; the coal feeding port 5 is used for adding raw coal, the coal water slurry feeding port 7 is used for adding coal water slurry, and the combustion flue gas outlet is used for discharging combustion flue gas generated by combustion reaction; wherein, the coal water slurry feeding port 7 and a secondary air port on the upper layer of the circulating fluidized bed boiler are positioned at the same height; the secondary air port is arranged in the reverse region at the lower part of the hearth 1; the separator 2 is provided with a separator inlet, a separator gas phase outlet and a separator solid phase outlet, the separator inlet is connected with the combustion flue gas outlet, and the separator 2 is used for carrying out gas-solid separation on the combustion flue gas to obtain fuel and flue gas; the material returning device 3 is positioned below the separator 2 and is connected with the solid phase outlet of the separator; the material returning device 3 is also provided with a material returning port which is connected with the lower part of the hearth 1 so as to return the fuel to the hearth 1; the tail flue 4 is connected with a gas phase outlet of the separator; the air distribution device 6 is arranged at the air inlet.
Furthermore, the circulating fluidized bed boiler also comprises a soot blower 8, and the soot blower 8 is arranged on one side of the tail flue 4 and communicated with the tail flue; preferably the sootblowers 8 are acoustic sootblowers.
Further, the method comprises the following steps: storing the coal water slurry in a stokehole slurry storage tank, sending the optional coal water slurry into a hearth 1 in a pumping mode through a stokehole conveying system and a coal water slurry spray gun, and sending raw coal into the hearth 1 from a coal feeding port 5 in a belt conveying mode to perform combustion reaction; the preferable furnace-front conveying system comprises a coal water slurry preparation system, a finished product tank, a slurry conveying pump, a buffer tank and a feeding pump, and a preferable coal water slurry spray gun is arranged in the coal water slurry feeding port 7.
Further, the number of the coal water slurry spray guns is 2-6; the preferable coal water slurry feeding port 7 is formed by sequentially connecting and surrounding a first side wall, a second side wall, a third side wall and a fourth side wall, 1 coal water slurry spray gun is preferably arranged on each of the first side wall and the third side wall, and 0-4 coal water slurry spray guns are preferably arranged on the second side wall.
Further, the conveying amount of the coal water slurry is adjusted through a coal water slurry control system.
Further, after the coal water slurry is added, limestone is added into the circulating fluidized bed boiler to carry out combustion desulfurization, preferably, wet or semi-dry desulfurization is carried out outside the boiler at the tail part, and the preferential method adopts a selective non-catalytic reduction technology to carry out denitration.
Furthermore, the average particle size of the coal water slurry is 15-75 mu m, the total moisture content of the coal water slurry is preferably 25-40%, and the low-level calorific value of the received base of the coal water slurry is preferably 10-16 MJ/kg.
Further, the raw coal is selected from one or two of anthracite, bituminous coal, lean coal and lignite; the average particle size of the raw coal is preferably 0-13 mm, the median average particle size of the raw coal is preferably 1.25-3 mm, the dry ashless volatile matter content of the raw coal is preferably 5-45%, the as-received-base ash content of the raw coal is preferably 10-40%, and the as-received-base low-calorific value of the raw coal is preferably 12-28 MJ/kg.
Further, the apparent viscosity of the coal water slurry is 950-1350 mPa & s, and the coal ash fusion softening temperature of the coal water slurry is preferably larger than 1250 ℃.
By applying the technical scheme of the invention, the bed temperature can be flexibly adjusted by adjusting the ratio of the coal water slurry to the raw coal (namely the slurry-coal ratio). The bed temperature can be controlled to be 800-900 ℃ in the range of full load to 25% load, the high combustion efficiency is ensured, and meanwhile, the emission of smoke pollutants can be reduced and the cost is reduced; in addition, the method is not limited by the operation load of the circulating fluidized bed boiler, has good bed temperature adjusting capability, is simple and easy to operate, and can reduce the operation risk.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiment(s) of the invention and together with the description serve to explain the invention and not to limit the invention. In the drawings:
FIG. 1 is a schematic representation of slurry coal ratio versus load and operating bed temperature for one embodiment of the present invention;
fig. 2 shows a schematic view of a circulating fluidized bed boiler according to an embodiment of the present invention.
Wherein the figures include the following reference numerals:
1. a hearth; 2. a separator; 3. a material returning device; 4. a tail flue; 5. a coal feeding port; 6. an air distribution device; 7. a coal water slurry feeding port; 8. and a soot blower is additionally arranged.
Detailed Description
It should be noted that, in the present application, the embodiments and features of the embodiments may be combined with each other without conflict. The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings.
The full load represents the maximum steam quantity which can be reached when the boiler is operated safely and continuously under the conditions of rated steam parameters, rated feed water temperature and use of designed fuel, namely 100 percent of load; the 75% load refers to 75% maximum steam, with other percent loads having similar definitions.
As analyzed in the background art of the present application, when only raw coal is used, the bed temperature at full load of the circulating fluidized bed boiler is 950 to 1000 ℃, the bed temperature at 75% load is 900 to 950 ℃, the bed temperature at 50% load is 850 to 900 ℃, and the bed temperature at 25% load is 800 to 850 ℃. The problems that the bed temperature of the circulating fluidized bed boiler can not be adjusted in a large range and more pollutants are generated exist in the prior art. To solve these problems, the present application provides a method of adjusting a bed temperature of a circulating fluidized bed boiler.
In an exemplary embodiment of the present application, there is provided a method of adjusting bed temperature of a circulating fluidized bed boiler, the method including: in a circulating fluidized bed boiler, optional coal water slurry and raw coal are mixed and subjected to combustion reaction; in the combustion reaction process, the ratio of the coal water slurry to the raw coal is adjusted according to the load value of the circulating fluidized bed boiler, and the load value of the circulating fluidized bed boiler is positively correlated with the ratio of the coal water slurry to the raw coal, so that the bed temperature of the circulating fluidized bed boiler is maintained at 800-900 ℃.
In the application, the water coal slurry can be evaporated and then combusted, and the time difference of heat absorption and heat release exists, so that the bed temperature can be flexibly adjusted by adjusting the ratio of the water coal slurry to the raw coal (namely the slurry-coal ratio). The bed temperature can be controlled to be 800-900 ℃ in the range of full load to 25% load, the high combustion efficiency is ensured, and meanwhile, the emission of smoke pollutants can be reduced and the cost is reduced; in addition, the method is not limited by the operation load of the circulating fluidized bed boiler, has good bed temperature adjusting capability, is simple and easy to operate, and can reduce the operation risk.
According to a schematic diagram (figure 1) of the relationship between the boiler load and the operating bed temperature, the boiler load is reduced, and the addition amount of the coal water slurry is correspondingly reduced. Bed temperature is too high or low all is unfavorable for reducing the fume pollutants and discharges, reduces the bed temperature and avoids the bed temperature to hang down to be unfavorable for reducing fume emission for higher range, and this application needs adjust the addition of coal slurry according to circulating fluidized bed boiler's load value. In order to avoid the reduction of the combustion efficiency while reducing the bed temperature, in some embodiments, in the process of mixing optional coal water slurry and raw coal, the adding amount of the coal water slurry at full load is controlled to be 24-36% of the raw coal mass, the adding amount of the coal water slurry at 75-100% of load is controlled to be 18-24% of the raw coal mass, the adding amount of the coal water slurry at 50-75% of load is controlled to be 6-18% of the raw coal mass, the adding amount of the coal water slurry at 25-50% of load is controlled to be 0-6% of the raw coal mass, so that the bed temperature is 850-900 ℃ when the load is 50% of the full load, and the bed temperature is 800-850 ℃ when the load is 50% of the raw coal.
In order to improve the combustion efficiency and prevent pollutant discharge and coking, in some embodiments, the adding amount of the coal water slurry at full load is 24-36% of the mass of the raw coal, the adding amount of the coal water slurry at 75% of the load is 18-24% of the mass of the raw coal, the adding amount of the coal water slurry at 50% of the load is 6-18% of the mass of the raw coal, and the adding amount of the coal water slurry at 25% of the load is 0-6% of the mass of the raw coal; so that the bed temperature is 850 to 900 ℃ when the load is 50% full and 800 to 850 ℃ when the load is 25% 50% full.
The circulating fluidized bed boiler in the application needs to have the capability of simultaneously burning raw coal and coal water slurry, and can keep good operation bed temperature adjusting capability. In some embodiments, as shown in fig. 2, the circulating fluidized bed boiler comprises: the device comprises a hearth 1, a separator 2, a material returning device 3, a tail flue 4 and an air distribution device 6, wherein the bottom of the hearth 1 is provided with an air inlet, and the side wall of the hearth is provided with a coal feeding port 5, a coal water slurry feeding port 7 and a combustion flue gas outlet; the coal feeding port 5 is used for adding raw coal, the coal water slurry feeding port 7 is used for adding coal water slurry, and the combustion flue gas outlet is used for discharging combustion flue gas generated by combustion reaction; wherein, the coal water slurry feeding port 7 and a secondary air port on the upper layer of the circulating fluidized bed boiler are positioned at the same height; the secondary air port is arranged in the reverse region at the lower part of the hearth 1; the separator 2 is provided with a separator inlet, a separator gas phase outlet and a separator solid phase outlet, the separator inlet is connected with the combustion flue gas outlet, and the separator 2 is used for carrying out gas-solid separation on the combustion flue gas to obtain fuel and flue gas; the material returning device 3 is positioned below the separator 2 and is connected with the solid phase outlet of the separator; the material returning device 3 is also provided with a material returning port which is connected with the lower part of the hearth 1 so as to return the fuel to the hearth 1; the tail flue 4 is connected with a gas phase outlet of the separator; the air distribution device 6 is arranged at the air inlet.
In order to reduce the influence caused by the increase of the flue gas amount and the fly ash portion, in some embodiments, the circulating fluidized bed boiler further comprises a soot blower 8, and the soot blower 8 is arranged on one side of the tail flue 4 and communicated with the tail flue; preferably the sootblowers 8 are acoustic sootblowers.
To improve the efficiency of fuel delivery, in some embodiments, the method comprises: the coal water slurry is stored in a stokehole slurry storage tank, the optional coal water slurry is sent into the hearth 1 in a pumping mode through a stokehole conveying system and a coal water slurry spray gun, and meanwhile, raw coal is sent into the hearth 1 from a coal feeding port 5 in a belt conveying mode to carry out combustion reaction. The stokehole conveying system of the application can refer to stokehole conveying systems commonly used in the prior art. The preferable furnace-front conveying system comprises a coal water slurry preparation system, a finished product tank, a slurry conveying pump, a buffer tank and a feeding pump, and a preferable coal water slurry spray gun is arranged in the coal water slurry feeding port 7.
In some embodiments, to reduce SO in flue gas 2 And NO x Discharging, arranging a coal water slurry spray gun in the coal water slurry feeding port 7 to promote calcium oxide and SO 2 And (4) reacting. The number of the coal water slurry spray guns is 2-6; the coal water slurry feeding port 7 is formed by sequentially connecting and surrounding a first side wall, a second side wall, a third side wall and a fourth side wall, 1 coal water slurry spray gun is preferably arranged on each of the first side wall and the third side wall, and 0-4 coal water slurry spray guns are preferably arranged on the second side wall. The fourth side wall is arranged close to the coal feeding port 5.
In some embodiments, the amount of coal-water slurry delivered is regulated by a coal-water slurry control system to provide for adequate combustion of the coal-water slurry within the furnace 1.
In order to reduce SO in flue gas 2 And NO x And (4) discharging concentration, adding limestone into the circulating fluidized bed boiler after adding the coal water slurry for combustion desulfurization, and preferably performing external desulfurization on the tail part by adopting a wet method or a semi-dry method. Denitration by selective non-catalytic reduction (SNCR) technology to ensure SO 2 The discharge concentration is lower than 30mg/m 3 ，NO x The discharge concentration is lower than 45mg/m 3 。
In some embodiments, in order to ensure that the coal water slurry has a certain concentration and fluidity, the average particle size of the coal water slurry is controlled to be 15-75 μm, because the coal water slurry completes water evaporation and then burns in the hearth 1, the total water content of the coal water slurry is not too low, and the combustion efficiency is prevented from being influenced by too high total water content, preferably, the total water content of the coal water slurry is 25-40%, and preferably, the received base low-level calorific value of the coal water slurry is 10-16 MJ/kg.
The application has no particular limitation on raw coal, and raw coal commonly used in the field can be applied to the application, so that the method has better fuel adaptability. In some embodiments, to further improve combustion efficiency, the raw coal is selected from one or both of anthracite, bituminous coal, lean coal, lignite; the average particle size of the raw coal is preferably 0-13 mm, the median average particle size of the raw coal is preferably 1.25-3 mm, the dry ashless volatile matter content of the raw coal is preferably 5-45%, the as-received-base ash content of the raw coal is preferably 10-40%, and the as-received-base low-calorific value of the raw coal is preferably 12-28 MJ/kg.
The application has no special limitation on the properties of the coal water slurry, and the coal water slurry commonly used in the field can be applied to the application. In some embodiments, the apparent viscosity of the water-coal-slurry is 950 to 1350mPa · s, and the ash fusion softening temperature of the water-coal-slurry is preferably greater than 1250 ℃.
The present application is described in further detail below with reference to specific examples, which should not be construed as limiting the scope of the invention as claimed.
Example 1
A circulating fluidized bed boiler as shown in fig. 2 was used, the boiler having a capacity rating of 135 MW. When in normal operation, the burning coal is bituminous coal, the low-grade calorific value of the received coal is 18MJ/kg, the average grain diameter is 2mm, the content of the dried ash-free base volatile component is 15%, the total moisture content of the used coal water slurry is 30%, the low-grade calorific value of the received coal is 12MJ/kg, and the average grain diameter is 30 mu m. The coal water slurry is stored in a front-of-furnace slurry storage tank, the coal water slurry is sent into a hearth 1 from a coal water slurry feeding port 7 through a front-of-furnace conveying system, meanwhile, raw coal is sent into the hearth 1 from a coal feeding port 5 in a belt conveying mode to carry out combustion reaction, then limestone is added into a boiler to carry out combustion desulfurization, and the conveying amount of the coal water slurry is adjusted through a coal water slurry control system. The number of the coal water slurry spray guns is 4, wherein the number of the first side wall and the third side wall is 1 respectively, and the number of the second side wall is 2.
When the usage amount of the coal water slurry is 25 percent of the mass of the raw coal, the bed temperature is 890 ℃ when the boiler is fully loaded, the molar ratio of desulfurization calcium to sulfur in the boiler is 3.2, and NO is not denitrated x The discharge concentration is 160mg/Nm 3 (ii) a Denitrated NO x Emission concentration of 45mg/Nm 3 (ii) a Desulfurized SO 2 The discharge concentration was 30mg/Nm 3 . At the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 90.6-91.6%.
When the usage amount of the coal water slurry is 30 percent of the mass of the raw coal, the bed temperature is 865 ℃ when the boiler is fully loaded, the molar ratio of desulfurization calcium to sulfur in the boiler is 2.8, and NO is not denitrated x The discharge concentration is 110mg/Nm 3 NO after denitration x Is 40mg/Nm 3 (ii) a Desulfurized SO 2 The discharge concentration was 30mg/Nm 3 . At the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 87.5-89.5%.
When the usage amount of the coal water slurry is 20 percent of the mass of the raw coal, the bed temperature is 875 ℃ when the boiler is 75 percent of the load; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 89.1-90.8%.
When the using amount of the coal water slurry is 10 percent of the mass of the raw coal, the bed temperature is 890 ℃ when the boiler is 50 percent of the load; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 86.5-88.5%.
The dosage of the coal water slurry is properly increased, and the SO can be reduced 2 And NO x The reduction range of the discharge amount of (3 to 8 mg/Nm) 3 But the efficiency of the corresponding boiler is reduced by 0.1-0.2%.
Example 2
A circulating fluidized bed boiler as shown in fig. 2 was used, the boiler having a capacity rating of 350 MW. When in normal operation, the burning coal is bituminous coal, the calorific value of the received base low level is 18MJ/kg, the total moisture content of the used coal water slurry is 30 percent, and the calorific value of the received base low level is 12 MJ/kg. The coal water slurry is stored in a stokehole slurry storage tank, the coal water slurry is sent into a hearth 1 from a coal water slurry feeding port 7 through a stokehole conveying system and a coal water slurry spray gun, meanwhile, raw coal is sent into the hearth 1 from a coal feeding port 5 in a belt conveying mode to carry out combustion reaction, then limestone is added into a boiler to carry out combustion desulfurization, and the conveying amount of the coal water slurry is adjusted through a coal water slurry control system. The number of the coal water slurry spray guns is 6, wherein the number of the first side wall and the number of the third side wall are respectively 1, and the number of the second side wall is 4.
When the usage amount of the coal water slurry is 30 percent of the mass of the raw coal, the bed temperature is 895 ℃ when the boiler is fully loaded; the mol ratio of calcium to sulfur in the desulfurization in the furnace is 3.0, and NO is generated when the denitration is not carried out x Emission concentration 180mg/Nm 3 NO after denitration x Is 40mg/Nm 3 SO after desulfurization 2 The discharge concentration is 20mg/Nm 3 . At the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 88-90%.
When the using amount of the coal water slurry is 20 percent of the mass of the raw coal, the bed temperature is 880 ℃ when the boiler is 75 percent of the load; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 87-89%.
When the usage amount of the coal water slurry is 15 percent of the mass of the raw coal, the bed temperature is 870 ℃ when the boiler is 50 percent of the load; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 86-88%.
When the using amount of the coal water slurry is 3 percent of the mass of the raw coal, the bed temperature is 850 ℃ when the boiler is 25 percent of the load; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 85.5-88.5%.
As the bed temperature of the embodiment 2 always belongs to the optimal range, the boiler parameter adjustment is flexible, and the pollutant emission is lower.
Example 3
A circulating fluidized bed boiler as shown in fig. 2 was used, the boiler having a capacity rating of 300 MW. When in normal operation, the burning coal is bituminous coal, the calorific value of the received base low level is 18MJ/kg, the total moisture content of the used coal water slurry is 30 percent, and the calorific value of the received base low level is 12 MJ/kg. The coal water slurry is stored in a front slurry storage tank, is sent into a hearth 1 from a coal water slurry feeding port 7 through a front conveying system and a coal water slurry spray gun, and is sent into the hearth 1 from a coal feeding port 5 by adopting a belt conveying mode for combustion reaction. 6 coal water slurry spray guns are provided, wherein the number of the first side wall and the number of the third side wall are respectively 1, the number of the second side wall is 4, limestone is added into a boiler for combustion desulfurization, and the conveying amount of the coal water slurry is adjusted by a coal water slurry control system.
When the usage amount of the coal water slurry is 30 percent of the mass of the raw coal, the bed temperature is 895 ℃ when the boiler is fully loaded; the mol ratio of calcium to sulfur in the desulfurization in the furnace is 3.0, and NO is generated when the denitration is not carried out x Emission concentration 170mg/Nm 3 NO after denitration x Has an emission concentration of 35mg/Nm 3 (ii) a Desulfurized SO 2 The discharge concentration was 25mg/Nm 3 . At the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 88-90%.
When the usage amount of the coal water slurry is 20 percent of the mass of the raw coal, the bed temperature is 880 ℃ when the boiler is 75 percent of the load; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 87-89%.
When the using amount of the coal water slurry is 15 percent of the mass of the raw coal, the bed temperature is 870 ℃ when the boiler is 50 percent loaded; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 86-88%.
When the using amount of the coal water slurry is 3 percent of the mass of the raw coal, the bed temperature is 850 ℃ when the boiler is 25 percent of the load; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 85.5-88.5%.
Example 4
Different from the embodiment 2, when the using amount of the coal water slurry is 36 percent of the mass of the raw coal, the bed temperature is 880 ℃ when the boiler is fully loaded; the mol ratio of calcium to sulfur in the desulfurization in the furnace is 2.8, and NO is generated when NO denitration is performed x Emission concentration 160mg/Nm 3 NO after denitration x Emission concentration of 38mg/Nm 3 (ii) a Desulfurized SO 2 The discharge concentration was 22mg/Nm 3 . At the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 87.5-89.5%.
When the usage amount of the coal water slurry is 24 percent of the mass of the raw coal, the bed temperature is 865 ℃ when the boiler is 75 percent of the load; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 86.5-88.5%.
When the usage amount of the coal water slurry is 18 percent of the mass of the raw coal, the bed temperature is 850 ℃ when the boiler is 50 percent of the load; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 85.5-88.5%.
When the using amount of the coal water slurry is 6 percent of the mass of the raw coal, the bed temperature is 815 ℃ when the boiler is 25 percent of the load; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 85-88%.
Example 5
Different from the embodiment 2, when the using amount of the coal water slurry is 24 percent of the mass of the raw coal, the bed temperature is 900 ℃ when the boiler is fully loaded; the mol ratio of calcium to sulfur in the desulfurization in the furnace is 3.3, and NO is generated when the denitration is not performed x The discharge concentration was 220mg/Nm 3 NO after denitration x Is 45mg/Nm 3 (ii) a Desulfurized SO 2 The discharge concentration was 30mg/Nm 3 And at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 87.5-89.5%.
When the usage amount of the coal water slurry is 18 percent of the mass of the raw coal, the bed temperature is 890 ℃ when the boiler is 75 percent of the load; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 86.5-88.5%;
when the usage amount of the coal water slurry is 6 percent of the mass of the raw coal, the bed temperature is 865 ℃ when the boiler is 50 percent of the load; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 85.5-88.5%;
no coal water slurry is added, and the bed temperature is 800 ℃ when the boiler is 25% loaded; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 85.5-88.5%.
Example 6
Different from the embodiment 2, when the using amount of the coal water slurry is 40 percent of the mass of the raw coal, the bed temperature is 865 ℃ when the boiler is fully loaded; the mol ratio of calcium to sulfur in the desulfurization in the furnace is 3.0, and NO is generated when the denitration is not carried out x Discharge concentration 220mg/Nm 3 NO after denitration x Is 45mg/Nm 3 (ii) a Desulfurized SO 2 The discharge concentration was 30mg/Nm 3 At the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 86-88%;
when the using amount of the coal water slurry is 27 percent of the mass of the raw coal, the bed temperature is 870 ℃ when the boiler is fully loaded; the mol ratio of calcium to sulfur in the desulfurization in the furnace is 2.8, and NO is generated when the denitration is not carried out x Discharge concentration 220mg/Nm 3 NO after denitration x Emission concentration of 45mg/Nm 3 (ii) a Desulfurized SO 2 The discharge concentration was 30mg/Nm 3 At the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 85-86%;
when the using amount of the coal water slurry is 23 percent of the mass of the raw coal, the bed temperature is 850 ℃ when the boiler is 50 percent of the load; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 84-87%;
when the using amount of the coal water slurry is 8 percent of the mass of the raw coal, the bed temperature is 810 ℃ when the boiler is 25 percent of the load; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 82-85%.
The dosage of the coal water slurry is properly increased, and the SO can be reduced 2 And NO x But the efficiency of the corresponding boiler is reduced by 0.1-0.2%. When the amount of the coal water slurry is too much, the efficiency of the boiler is reduced.
Comparative example 1
A circulating fluidized bed boiler with the capacity grade of 135MW is adopted, only raw coal is used for combustion, the raw coal is bituminous coal, and the received base low-level calorific value is 18 MJ/kg.
The bed temperature is 980 ℃ when the circulating fluidized bed boiler is fully loaded, the molar ratio of calcium to sulfur in the boiler is 4.5, and NO is not denitrated x The discharge concentration was 280mg/Nm 3 NO after denitration x Emission concentration of 90mg/Nm 3 (ii) a Desulfurized SO 2 The discharge concentration is 120mg/Nm 3 . At the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 90.9-91.9%;
the bed temperature at 75% load of the circulating fluidized bed boiler is 920 ℃; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 87.8-89.8%;
the bed temperature is 890 ℃ when the circulating fluidized bed boiler is 50% loaded; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 89.4-91.2%.
Comparative example 1 compared to example 1, the molar ratio of calcium to sulfur was high and ultra-low emissions could not be achieved. Example 1 compared with comparative example 1, when the bed temperature is reduced at full load of the boiler, the pollutant emission concentration and the environmental protection investment are obviously reduced, and meanwhile, the boiler efficiency is not obviously reduced.
Comparative example 2
A circulating fluidized bed boiler with the capacity grade of 350MW is adopted, only raw coal is used for combustion, the raw coal is bituminous coal, and the received base low-level heat productivity is 18 MJ/kg.
The bed temperature is 1020 ℃ when the circulating fluidized bed boiler is fully loaded; the mol ratio of calcium to sulfur in the desulfurization in the furnace is 5.0, and NO is generated when the denitration is not carried out x The discharge concentration was 320mg/Nm 3 NO after denitration x Has an emission concentration of 120mg/Nm 3 (ii) a Desulfurized SO 2 The discharge concentration was 150mg/Nm 3 . At the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 88.5-90.5%;
the bed temperature at 75% load of the circulating fluidized bed boiler was 960 ℃; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 87.5-89.5%;
the bed temperature is 920 ℃ when the circulating fluidized bed boiler is 50% loaded; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 86.5-88.5%;
the bed temperature is 860 ℃ when the circulating fluidized bed boiler is 25% loaded; at the moment, the thermal efficiency of the boiler burning the coal water slurry and the raw coal is 86-89%.
Compared with the comparative examples 1-2, the bed temperature of the example 2 always falls within the optimal range, the boiler parameters are flexibly adjusted, and the pollutant emission is lower.
From the above description, it can be seen that the above-described embodiments of the present invention achieve the following technical effects: the water coal slurry can be evaporated and then combusted in the hearth 1, and the time difference of heat absorption and heat release exists, so that the bed temperature can be flexibly adjusted by adjusting the ratio of the water coal slurry to the raw coal (namely the slurry coal ratio). The bed temperature can be controlled to be 800-900 ℃ in the range of full load to 25% load, the high combustion efficiency is ensured, and meanwhile, the emission of smoke pollutants can be reduced and the cost is reduced; in addition, the method is not limited by the operation load of the circulating fluidized bed boiler, has good bed temperature adjusting capability, is simple and easy to operate, and can reduce the operation risk.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (12)
1. A method of regulating bed temperature of a circulating fluidized bed boiler, the method comprising:
in a circulating fluidized bed boiler, optional coal water slurry and raw coal are mixed and subjected to combustion reaction;
in the combustion reaction process, the ratio of the coal water slurry to the raw coal is adjusted according to the load value of the circulating fluidized bed boiler, and the load value of the circulating fluidized bed boiler is positively correlated with the ratio of the coal water slurry to the raw coal, so that the bed temperature of the circulating fluidized bed boiler is maintained at 800-900 ℃.
2. The method as claimed in claim 1, wherein in the process of mixing the optional coal-water slurry and the raw coal, the addition amount of the coal-water slurry is controlled to be 24-36% of the mass of the raw coal at full load, 18-24% of the mass of the raw coal at 75-100% of load, 6-18% of the mass of the raw coal at 50-75% of load, 0-6% of the mass of the raw coal at 25-50% of load, such that the bed temperature is 850-900 ℃ at full load to 50% of load and 800-850 ℃ at 50-25% of load.
3. The method according to claim 1 or 2, wherein the amount of coal-water slurry added at full load is 24-36% of the mass of the raw coal, the amount of coal-water slurry added at 75% load is 18-24% of the mass of the raw coal, the amount of coal-water slurry added at 50% load is 6-18% of the mass of the raw coal, and the amount of coal-water slurry added at 25% load is 0-6% of the mass of the raw coal.
4. The method of claim 1, wherein the circulating fluidized bed boiler comprises:
the device comprises a hearth (1), wherein an air inlet is formed in the bottom of the hearth (1), and a coal feeding port (5), a coal water slurry feeding port (7) and a combustion flue gas outlet are formed in the side wall of the hearth; the coal feeding port (5) is used for adding the raw coal, the coal water slurry feeding port (7) is used for adding the coal water slurry, and the combustion flue gas outlet is used for discharging combustion flue gas generated by the combustion reaction; wherein the coal water slurry feeding port (7) and a secondary air port on the upper layer of the circulating fluidized bed boiler are positioned at the same height; the secondary air port is arranged in a reverse region at the lower part of the hearth (1);
the separator (2) is provided with a separator inlet, a separator gas phase outlet and a separator solid phase outlet, the separator inlet is connected with the combustion flue gas outlet, and the separator (2) is used for carrying out gas-solid separation on the combustion flue gas to obtain fuel and flue gas;
the material returning device (3) is positioned below the separator (2) and is connected with the solid phase outlet of the separator; the material returning device (3) is also provided with a material returning port which is connected with the lower part of the hearth (1) so as to return the fuel to the hearth (1);
the tail flue (4) is connected with the gas phase outlet of the separator;
and the air distribution device (6) is arranged at the air inlet.
5. A method according to claim 4, characterized in that the circulating fluidized bed boiler further comprises a soot blower (8), the soot blower (8) being arranged at one side of the back pass (4) and communicating therewith; preferably, the soot blower (8) is a sound wave soot blower.
6. The method according to claim 4 or 5, characterized in that it comprises:
the coal water slurry is stored in a stokehole slurry storage tank, the optional coal water slurry is sent into the hearth (1) in a pumping mode through a stokehole conveying system and a coal water slurry spray gun, and meanwhile, the raw coal is sent into the hearth (1) from the coal feeding port (5) in a belt conveying mode to perform the combustion reaction;
preferably, the furnace front conveying system comprises a coal water slurry preparation system, a finished product tank, a slurry conveying pump, a buffer tank and a feeding pump, and preferably, the coal water slurry spray gun is arranged in the coal water slurry feeding port (7).
7. The method according to claim 6, wherein the number of the coal-water slurry spray guns is 2-6; the coal water slurry feeding port (7) is formed by sequentially connecting and surrounding a first side wall, a second side wall, a third side wall and a fourth side wall, preferably, 1 coal water slurry spray gun is arranged on each of the first side wall and the third side wall, and 0-4 coal water slurry spray guns are arranged on the second side wall.
8. The method of any one of claims 1 to 7 wherein the delivery rate of the coal-water slurry is regulated by a coal-water slurry control system.
9. The method according to any one of claims 1 to 8, wherein after the addition of the coal-water slurry, limestone is added to the circulating fluidized bed boiler for combustion desulfurization, preferably for off-furnace desulfurization at the tail by a wet or semi-dry process, preferably for denitration by a selective non-catalytic reduction technique.
10. The method according to any one of claims 1 to 9, wherein the average particle size of the coal water slurry is 15-75 μm, the total moisture content of the coal water slurry is preferably 25-40%, and the received base lower calorific value of the coal water slurry is preferably 10-16 MJ/kg.
11. The method according to any one of claims 1 to 10, wherein the raw coal is selected from one or two of anthracite, bituminous, lean, lignite; the average particle size of the raw coal is preferably 0-13 mm, the median average particle size of the raw coal is preferably 1.25-3 mm, the dry ashless volatile matter content of the raw coal is preferably 5-45%, the received base ash content of the raw coal is preferably 10-40%, and the received base low-calorific value of the raw coal is preferably 12-28 MJ/kg.
12. The method according to any one of claims 1 to 11, wherein the apparent viscosity of the coal water slurry is 950 to 1350 mPa-s, preferably the ash fusion softening temperature of the coal water slurry is more than 1250 ℃.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN116481021A (en) * | 2023-05-17 | 2023-07-25 | 哈尔滨红光锅炉总厂有限责任公司 | Environment-friendly energy-saving circulating fluidized bed boiler capable of respectively burning coal and coal water slurry |
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