CN108105761B - Ultra-low emission cooperative control method and system integration device for circulating fluidized bed boiler - Google Patents
Ultra-low emission cooperative control method and system integration device for circulating fluidized bed boiler Download PDFInfo
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- CN108105761B CN108105761B CN201810032019.2A CN201810032019A CN108105761B CN 108105761 B CN108105761 B CN 108105761B CN 201810032019 A CN201810032019 A CN 201810032019A CN 108105761 B CN108105761 B CN 108105761B
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- fluidized bed
- circulating fluidized
- bed boiler
- limestone
- hearth
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- 238000000034 method Methods 0.000 title claims abstract description 17
- 230000010354 integration Effects 0.000 title abstract description 7
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 81
- 230000023556 desulfurization Effects 0.000 claims abstract description 81
- 235000019738 Limestone Nutrition 0.000 claims abstract description 46
- 239000006028 limestone Substances 0.000 claims abstract description 46
- 239000000428 dust Substances 0.000 claims abstract description 24
- 239000004744 fabric Substances 0.000 claims abstract description 16
- 239000003245 coal Substances 0.000 claims abstract description 13
- 239000000463 material Substances 0.000 claims abstract description 13
- 238000003860 storage Methods 0.000 claims abstract description 12
- 238000002485 combustion reaction Methods 0.000 claims abstract description 11
- 239000002356 single layer Substances 0.000 claims abstract description 8
- 239000003344 environmental pollutant Substances 0.000 claims abstract description 7
- 231100000719 pollutant Toxicity 0.000 claims abstract description 7
- 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
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 10
- 239000000446 fuel Substances 0.000 claims description 8
- 239000000779 smoke Substances 0.000 claims description 8
- 230000003213 activating effect Effects 0.000 claims description 7
- 229910021529 ammonia Inorganic materials 0.000 claims description 5
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 238000001514 detection method Methods 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 238000005728 strengthening Methods 0.000 claims description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 2
- 239000004202 carbamide Substances 0.000 claims description 2
- 238000005260 corrosion Methods 0.000 abstract description 4
- 230000007797 corrosion Effects 0.000 abstract description 4
- 238000003912 environmental pollution Methods 0.000 abstract description 3
- 239000002956 ash Substances 0.000 description 20
- 239000000203 mixture Substances 0.000 description 8
- 239000002245 particle Substances 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000000738 capillary electrophoresis-mass spectrometry Methods 0.000 description 1
- 238000005536 corrosion prevention Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
Classifications
-
- 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
- F23C10/24—Devices for removal of material from the bed
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
- F23C10/24—Devices for removal of material from the bed
- F23C10/26—Devices for removal of material from the bed combined with devices for partial reintroduction of material into the bed, e.g. after separation of agglomerated parts
-
- 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
Landscapes
- 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 discloses a cooperative control method and a system integration device for ultralow emission of a circulating fluidized bed boiler, and relates to a cooperative control method for combustion and an auxiliary system integration device, which are used for solving the problems of environmental pollution and equipment corrosion caused by the fact that the emission of the existing circulating fluidized bed boiler does not reach the standard. The invention comprises a circulating fluidized bed boiler, a denitration device, a limestone desulfurization system, a dry desulfurization system and a cloth bag dust removal system; the top of a hearth of the circulating fluidized bed boiler is communicated with a separator, a material returning device is communicated with the bottom of the hearth of the circulating fluidized bed boiler, a denitration device is arranged between the material returning device and the hearth, the hearth and a tail flue are respectively communicated with a limestone desulfurization system, a coal feeding device and a single-layer overgrate air device are respectively arranged at the bottom of the hearth, the tail flue and a cloth bag dust removal system are respectively communicated with a dry desulfurization system, and the cloth bag dust removal system is communicated with the dry desulfurization system through an ash storage bin. The invention is suitable for controlling the pollutant emission of the circulating fluidized bed boiler.
Description
Technical Field
The invention particularly relates to a cooperative control method and a system integration device for ultralow emission of a circulating fluidized bed boiler.
Background
The combustion technology of the circulating fluidized bed boiler is rapidly developed due to the environment-friendly and energy-saving performance of the circulating fluidized bed boiler, and the development and the application of the integrated ultralow emission technology of the cooperative control and auxiliary system of the circulating fluidized bed boiler are accelerated along with the implementation of the emission standard of the new boiler atmospheric pollutants, so that the ultralow emission, the efficient combustion and the safe operation are realized. At present, various environmental protection treatment devices are required to be arranged in an external treatment system of the existing circulating fluidized bed boiler, the problem that the emission does not reach the standard is solved, and the adopted wet desulfurization, SCR denitration, wet dust removal or wet electric dust removal equipment and other devices have the problems of high investment cost and high operation cost in the treatment mode, and the equipment corrosion can be caused, so that the environmental pollution such as wastewater emission, ammonia escape, colored smoke plume, gypsum rain, haze and the like is further caused.
Disclosure of Invention
The invention provides a cooperative control method and a system integration device for ultralow emission of a circulating fluidized bed boiler, which aim to solve the problems of environmental pollution and equipment corrosion caused by the fact that the emission of the existing circulating fluidized bed boiler does not reach the standard.
The technical scheme adopted for solving the technical problems is as follows:
1. a part of limestone with a certain granularity, which comes out of the limestone desulfurization system, enters a hearth to carry out primary desulfurization in the hearth, the primary desulfurization enters a separator to carry out secondary desulfurization, flue gas is separated out by the separator, and limestone and ash enter the hearth through a returning charge device to be recycled;
2. the material circulation quantity is changed by controlling the granularity of the fuel entering the hearth by the coal feeding device and controlling a return valve on the return feeder; adopting a single-layer structure of the secondary air device, and strengthening the reducing atmosphere of fuel combustion by adjusting the size of an air door of the secondary air device; so as to realize low-nitrogen combustion and complete denitration in the furnace;
3. the other part of limestone from the limestone desulfurization system enters a tail flue, and enters a dry desulfurization system for desulfurization after being humidified and desulfurized with ash and flue gas by a humidifying and activating device;
4. after desulfurization of the dry desulfurization system, limestone and ash enter a cloth bag dust removal system to separate out smoke, the limestone and ash enter an ash storage bin, the ash storage bin sends the limestone and ash into the dry desulfurization system for secondary desulfurization, the limestone and the ash are circulated and reciprocated in this way, and the purified smoke is discharged through a chimney;
5. before being discharged from a chimney, the purified flue gas passes through a flue gas concentration detection device to detect NOx and SO 2 And the discharge contents of pollutants such as PM, ammonia and the like are respectively transmitted to each automatically-adjusted valve on the limestone desulfurization system, the denitrification device, the dry desulfurization system and the bag-type dust removal system to change the feed quantity so as to ensure that the discharge reaches the standard.
An ultra-low emission system integrated device of a circulating fluidized bed boiler is characterized in that:
the system comprises a circulating fluidized bed boiler, a limestone desulfurization system, a dry desulfurization system and a cloth bag dust removal system;
the top of a hearth of the circulating fluidized bed boiler is communicated with a separator, a material returning device is communicated with the bottom of the hearth of the circulating fluidized bed boiler, a denitration device is arranged between the material returning device and the hearth of the circulating fluidized bed boiler, the hearth and a tail flue are respectively communicated with a limestone desulfurization system, and a coal feeding device and a single-layer overgrate air device are respectively arranged at the bottom of the hearth;
the tail flue and the cloth bag dust removing system are respectively communicated with the dry desulfurization system, the cloth bag dust removing system is communicated with the ash storage bin, and the ash storage bin is communicated with the dry desulfurization system.
Preferably, the denitration device is an SNCR denitration device.
Further, a humidifying and activating device is arranged between the tail flue and the dry desulfurization system.
Compared with the prior art, the invention has the following beneficial effects:
1. the tail part of the invention adopts the integration of humidifying and activating dry desulfurization and a cloth bag dust removing system to realize SO 2 Ultra-low emission of smoke dust and no cost for removing SO 3 Zero discharge of heavy metals and wastewater, no corrosion resistance of a flue and a chimney, less than or equal to 1 grade of blackness of finally discharged flue gas, and less than 10mg/Nm of PM 3 。
2. The standby SNCR denitration device ensures that the emission of the full-load wide coal NOx reaches the standard and is stable under special conditions (such as start and stop of a boiler, abrupt load change, fluctuation of coal types and the like).
3. The limestone desulfurization device is preferably an optimal limestone type, provides limestone particle size and distribution requirements matched with the fluidization state in the furnace, ensures optimal desulfurization efficiency, is simple and reliable in conveying, can meet long-term continuous and stable operation of the boiler for more than 8000 hours, and can realize accurate adjustment and control of limestone conveying capacity.
4. The present invention can make the NOx emission concentration from 100 to 250mg/Nm 3 Down to 50mg/Nm 3 Within the inner part.
5. The invention can improve the desulfurization efficiency in the furnace from the existing lower than 95% to 99%, SO 2 The discharge concentration is less than 100mg/m 3 Down to less than 35mg/m 3 。
Drawings
FIG. 1 is a schematic illustration of the present invention;
FIG. 2 is a diagram showing the connection structure of the separator and the return device;
FIG. 3 is an overall block diagram of a separator;
fig. 4 is a cross-sectional view A-A of fig. 3.
Detailed Description
The first embodiment is as follows: the present embodiment is described with reference to fig. 1, and includes a circulating fluidized bed boiler 1, a limestone desulfurization system 2, a denitrification device 3, a dry desulfurization system 4, and a bag-type dust removal system 5;
the top of a hearth 1-1 of the circulating fluidized bed boiler 1 is communicated with a separator 1-2, a material returning device 1-3 is communicated with the bottom of the hearth 1-1 of the circulating fluidized bed boiler 1, a denitration device 3 is arranged between the material returning device 1-3 and the hearth 1-1 of the circulating fluidized bed boiler 1, the hearth 1-1 and a tail flue 1-6 are respectively communicated with a limestone desulfurization system 2, and a coal feeding device 1-5 and a single-layer overgrate air device 1-4 are respectively arranged at the bottom of the hearth 1-1;
the tail flue 1-6 and the cloth bag dust removing system 5 are respectively communicated with the dry desulfurization system 4, the cloth bag dust removing system 5 is communicated with the ash storage bin 5-1, and the ash storage bin 5-1 is communicated with the dry desulfurization system 4.
The circulating fluidized bed boiler 1, the limestone desulfurization system 2, the dry desulfurization system 4 and the bag-type dust removal system 5 are mutually and cooperatively controlled in terms of ultra-low emission of pollutants, and are connected and integrated together through pipelines to form an integrated device of the ultra-low emission system of pollutants.
The single-layer overgrate air device 1-4 adopted by the invention is a technology disclosed in the prior patent CN201610052478.8, and has the same structure as the overgrate air described in the prior patent CN 201610052478.8.
The second embodiment is as follows: the present embodiment will be described with reference to fig. 1, in which the denitration device 3 according to the present embodiment is an SNCR denitration device.
The method has low cost and less influence on the normal operation of the boiler.
Other compositions and connection relationships are the same as those of the first embodiment.
And a third specific embodiment: referring to fig. 1, a humidifying and activating device 4-1 is provided between the back flue 1-6 and the dry desulfurization system 4.
In the embodiment, caO which does not undergo chemical reaction in the furnace and SO in the flue gas can be reacted 2 Reaction to produce CaSO 4 The desulfurization is deeply utilized, the treatment of waste by waste is realized, and the humidification and the activity are realizedThe chemical device 4-1 can ensure SO under the condition of fluctuation of desulfurization working conditions in the furnace 2 The emission is stable and reaches the standard.
The embodiment realizes the cyclic desulfurization outside the furnace and further reduces the sulfur emission. Other compositions and connection relationships are the same as those of the first or second embodiment.
The specific embodiment IV is as follows: referring to fig. 1, in the present embodiment, a bag-type dust removing system 5 is connected to a chimney 6, and a flue gas concentration detecting device 7 is disposed in the chimney 6.
The flue gas concentration detection device 7 is CEMS.
The flue gas detection device 7 can detect SO in flue gas discharged by the chimney 6 in real time 2 、NO x Emission concentration of PM and ammonia.
Other compositions and connection relationships are the same as those of the third embodiment.
Fifth embodiment: in the present embodiment, referring to FIGS. 2 to 4, the separator 1-2 includes an inlet long flue 1-2-1, a cylinder 1-2-2, a cone 1-2-3, a riser 1-2-4, and a center cylinder 1-4-5, an inlet of the inlet long flue 1-2-1 is communicated with the furnace 1, an outlet of the inlet long flue 1-2-1 is communicated with an upper side wall of the cylinder 1-2-2, a height h of the inlet long flue 1-2-1 in a length direction thereof is equal, a width of the inlet long flue 1-2-1 in a length direction thereof is gradually reduced, an inlet width w1 of the inlet long flue 1-2-1 is larger than an outlet width w2, the cylinder 1-2-2, the cone 1-2-3 and the vertical pipe 1-2-4 are sequentially communicated from top to bottom and are made into a whole, the center cylinder 1-4-5 is of a circular cylindrical structure with an upper opening and a lower opening, the upper end of the center cylinder 1-4-5 is fixedly connected with the top of the cylinder 1-2-2, the center cylinder 1-4-5 is in double offset arrangement, a plane formed by an x axis and a y axis perpendicular to the x axis coincides with the upper surface of the cylinder 1-2-2, the intersection point of the x axis and the y axis is the center o of the upper surface of the cylinder 1-2-2, the x axis is perpendicular to the inlet of the inlet long flue 1-2-1, the center o1 of the upper surface of the center cylinder 1-4-5 is offset by a distance in the negative direction of the x axis relative to the center o of the upper surface of the cylinder 1-2-2, and is offset a distance in the positive direction of the y-axis.
Other compositions and connection relationships are the same as those of the fourth embodiment.
Specific embodiment six: the control method according to the present embodiment will be described with reference to fig. 1 as follows:
1. part of limestone with certain granularity which comes out of the limestone desulfurization system 2 enters the hearth 1-1, primary desulfurization is carried out in the hearth 1-1, the primary desulfurization enters the separator 1-2 for secondary desulfurization, flue gas is separated out by the separator 1-2, and limestone and ash enter the hearth 1-1 through the material returning device 1-3, and the process is repeatedly circulated;
the flow rate of the flue gas in the hearth 1-1 is controlled to be less than or equal to 5m/s, so that the abrasion of the heating surface of the hearth 1-1 can be prevented;
2. the material circulation quantity is changed by controlling the granularity of the fuel entering the hearth 1-1 from the coal feeding device 1-5 and controlling a return valve on the return feeder 1-3; adopting a single-layer structure of the secondary air device 1-4, and strengthening the reducing atmosphere of fuel combustion by adjusting the size of an air door of the secondary air device 1-4; so as to realize low-nitrogen combustion and complete denitration in the furnace;
preferably, the particle size of the fuel entering the furnace 1-1 from the coal feeder 1-5 is in the range of 0-8mm.
3. The other part of limestone from the limestone desulfurization system 2 enters a tail flue 1-6, and enters a dry desulfurization system 4 for desulfurization after being humidified and desulfurized with ash and flue gas by a humidifying and activating device 4-1; the chemical reaction equation is as follows:
CaO+SO 2 +1/2O 2 ＝CaSO 4
Ca(OH) 2 +SO 3 ＝CaSO 4 +H 2 O
compared with wet desulfurization. Desulfurization by adopting a humidifying and activating device 4-1 can realize the removal of SO without cost 3 The zero emission of heavy metal Hg and wastewater can be realized, and meanwhile, the flue and the chimney are not corroded, and corrosion prevention is not needed;
4. after desulfurization by the dry desulfurization system 4, limestone and ash enter a cloth bag dust removal system 5 to separate out smoke, the limestone and ash enter an ash storage bin 5-1, the ash storage bin 5-1 sends the limestone and ash into the dry desulfurization system 4 for desulfurization again, the limestone and ash are circularly reciprocated, and the purified smoke is discharged through a chimney 6;
5. purified flue gas is passed through the flue gasBefore the chimney 6 is discharged, NOx and SO are detected by a flue gas concentration detection device 7 2 The discharge content of pollutants such as PM, ammonia and the like, and the generated feedback signals are respectively transmitted to each automatically-adjusted valve on the limestone desulfurization system 2, the denitrification device 3, the dry desulfurization system 4 and the cloth bag dust removal system 5 to change the feed amount so as to ensure that the discharge reaches the standard (NO X <50mg/Nm 3 、SO 2 <35mg/Nm 3 、PM<10mg/Nm 3 )。
Seventh embodiment: the control method according to the present embodiment will be described with reference to fig. 1 as follows:
the dry desulfurization system 4 may be replaced with a semi-dry desulfurization system. Other compositions and connection relationships are the same as those of the sixth embodiment.
Eighth embodiment: the present embodiment will be described with reference to fig. 1, in which the combustion temperature at the time of desulfurization and denitration of the circulating fluidized bed boiler 1 is controlled to be 850 to 880 ℃.
The embodiment ensures the residence time of the flue gas, ash and limestone in the hearth 1-1 and the separator 1-2 so as to enhance the desulfurization efficiency in the furnace and realize the high-efficiency desulfurization in the furnace. Other compositions and connection relationships are the same as those of the seventh embodiment.
Detailed description nine: referring to fig. 1, in the present embodiment, when the circulating fluidized bed boiler 1 is started and stopped, the load is suddenly changed, and the coal is fluctuated, the NOx is removed by chemical reaction after the denitration liquid enters the inlet of the separator 1-2 through the denitration device 3 by using ammonia water or urea solution as the denitration liquid by the SNCR denitration device; other compositions and connection relationships are the same as those of embodiment eight.
Detailed description ten: the present embodiment will be described with reference to fig. 1, in which the limestone particle size is 0 to 0.5mm.
Other compositions and connection relationships are the same as those of the embodiment nine.
Claims (4)
1. The method is applied to an integrated device of an ultralow emission system of the circulating fluidized bed boiler, and the device comprises a circulating fluidized bed boiler (1), a limestone desulfurization system (2), a denitration device (3), a dry desulfurization system (4) and a cloth bag dust removal system (5); the top of a hearth (1-1) of the circulating fluidized bed boiler (1) is communicated with a separator (1-2), a material returning device (1-3) is communicated with the bottom of the hearth (1-1) of the circulating fluidized bed boiler (1), a denitration device (3) is arranged between the material returning device (1-3) and the hearth (1-1) of the circulating fluidized bed boiler (1), the hearth (1-1) and a tail flue (1-6) are respectively communicated with a limestone desulfurization system (2), and a coal feeding device (1-5) and a single-layer overgrate air device (1-4) are respectively arranged at the bottom of the hearth (1-1); the tail flue (1-6) and the cloth bag dust removing system (5) are respectively communicated with the dry desulfurization system (4), the cloth bag dust removing system (5) is communicated with the Chu Huicang (5-1), and the ash storage bin (5-1) is communicated with the dry desulfurization system (4);
the method is characterized in that: the ultra-low emission cooperative control method of the circulating fluidized bed boiler comprises the following steps of;
1. part of limestone with certain granularity which comes out of a limestone desulfurization system (2) enters a hearth (1-1), primary desulfurization is carried out in the hearth (1-1), the primary desulfurization enters a separator (1-2) to carry out secondary desulfurization, flue gas is separated out by the separator (1-2), and limestone and ash enter the hearth (1-1) through a material returning device (1-3) to be recycled;
2. the material circulation quantity is changed by controlling the granularity of the fuel entering the hearth (1-1) from the coal feeding device (1-5) and controlling a return valve on the return device (1-3), and the granularity range of the fuel entering the hearth (1-1) from the coal feeding device (1-5) is 0-8mm; adopting a single-layer structure of the secondary air device (1-4), and strengthening the reducing atmosphere of fuel combustion by adjusting the size of an air door of the secondary air device (1-4); so as to realize low-nitrogen combustion and complete denitration in the furnace;
3. the other part of limestone coming out of the limestone desulfurization system (2) enters a tail flue (1-6), and enters a dry desulfurization system (4) for desulfurization after being humidified and desulfurized with ash and flue gas by a humidifying and activating device (4-1), wherein the granularity of the limestone is 0-0.5mm;
4. after desulfurization of the dry desulfurization system (4), limestone and ash enter a cloth bag dust removing system (5) to separate out smoke, the limestone and ash enter an ash storage bin (5-1), the ash storage bin (5-1) sends the limestone and ash into the dry desulfurization system (4) for desulfurization again, the limestone and ash are circulated and reciprocated in this way, and the purified smoke is discharged through a chimney (6);
5. the purified flue gas passes through a flue gas concentration detection device (7) before being discharged through a chimney (6) to detect NOx and SO 2 And the discharge contents of pollutants such as PM, ammonia and the like are respectively transmitted to a limestone desulfurization system (2), a denitrification device (3), a dry desulfurization system (4) and a bag-type dust removal system (5) by generated feedback signals, and the feed quantity of each automatically-adjusted valve is changed so as to enable the discharge to reach the standard.
2. The cooperative control method for ultra-low emission of a circulating fluidized bed boiler according to claim 1, wherein the method comprises the following steps: the dry desulfurization system (4) can be replaced by a semi-dry desulfurization system.
3. The cooperative control method for ultra-low emission of a circulating fluidized bed boiler according to claim 2, wherein: the combustion temperature of the circulating fluidized bed boiler (1) during desulfurization and denitration is controlled between 850 ℃ and 880 ℃.
4. A circulating fluidized bed boiler ultra-low emission cooperative control method according to claim 3, characterized in that: when the circulating fluidized bed boiler (1) starts and stops, the load suddenly changes, the coal fluctuation and other special conditions are needed, the SNCR denitration device is needed to be used for denitration, ammonia water or urea solution is used for denitration liquid, the denitration liquid enters the inlet of the separator (1-2) through the denitration device (3), and NOx is removed through chemical reaction after the denitration liquid and flue gas are mixed in the separator (1-2).
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| CN109718660A (en) * | 2019-01-09 | 2019-05-07 | 中国神华能源股份有限公司 | Circulating fluidized bed boiler and sulfur method |
| CN110793013A (en) * | 2019-12-16 | 2020-02-14 | 哈尔滨红光锅炉总厂有限责任公司 | High-temperature and high-pressure steam boiler of pure-burning biomass environment-friendly circulating fluidized bed |
| CN111536507A (en) * | 2020-05-20 | 2020-08-14 | 哈尔滨红光锅炉总厂有限责任公司 | Low-emission type circulating fluidized bed boiler separation return regulation and control system and integration method |
| CN114135865B (en) * | 2021-12-20 | 2024-02-27 | 重庆大学 | High-temperature ash storage device and circulating fluidized bed boiler with same |
| CN116892722B (en) * | 2023-07-10 | 2024-05-10 | 哈尔滨红光锅炉总厂有限责任公司 | Pure coal powder circulating fluidized bed system |
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