CN108105761A - Circulating fluidized bed boiler minimum discharge cooperative control method and system integration device - Google Patents
Circulating fluidized bed boiler minimum discharge cooperative control method and system integration device Download PDFInfo
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- CN108105761A CN108105761A CN201810032019.2A CN201810032019A CN108105761A CN 108105761 A CN108105761 A CN 108105761A CN 201810032019 A CN201810032019 A CN 201810032019A CN 108105761 A CN108105761 A CN 108105761A
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- China
- Prior art keywords
- fluidized bed
- bed boiler
- circulating fluidized
- burner hearth
- desulfurization
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 43
- 230000010354 integration Effects 0.000 title claims abstract description 12
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 79
- 230000023556 desulfurization Effects 0.000 claims abstract description 45
- 235000019738 Limestone Nutrition 0.000 claims abstract description 42
- 239000006028 limestone Substances 0.000 claims abstract description 42
- 239000000428 dust Substances 0.000 claims abstract description 23
- 239000000463 material Substances 0.000 claims abstract description 15
- 239000003245 coal Substances 0.000 claims abstract description 12
- 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 29
- 239000003546 flue gas Substances 0.000 claims description 29
- 230000008676 import Effects 0.000 claims description 13
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 10
- 230000004913 activation Effects 0.000 claims description 9
- 239000007788 liquid Substances 0.000 claims description 8
- 239000000446 fuel Substances 0.000 claims description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- 230000008859 change Effects 0.000 claims description 6
- 238000001514 detection method Methods 0.000 claims description 6
- 229910021529 ammonia Inorganic materials 0.000 claims description 5
- 239000010410 layer Substances 0.000 claims description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 3
- 239000005864 Sulphur Substances 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- 239000002356 single layer Substances 0.000 claims description 3
- 239000004575 stone Substances 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
- 239000000908 ammonium hydroxide Substances 0.000 claims description 2
- 239000004202 carbamide Substances 0.000 claims description 2
- 239000007787 solid Substances 0.000 claims description 2
- 238000005260 corrosion Methods 0.000 abstract description 5
- 230000007797 corrosion Effects 0.000 abstract description 3
- 238000003912 environmental pollution Methods 0.000 abstract description 3
- 239000000203 mixture Substances 0.000 description 8
- 239000002351 wastewater Substances 0.000 description 3
- 229910052925 anhydrite Inorganic materials 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 238000000738 capillary electrophoresis-mass spectrometry Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 230000003134 recirculating effect Effects 0.000 description 1
- 230000007480 spreading Effects 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 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
Abstract
A kind of circulating fluidized bed boiler minimum discharge cooperative control method and system integration device, it is related to a kind of burning cooperative control method and auxiliary system integrating device, the present invention environmental pollution and equipment corrosion caused by solve the problems, such as existing circulating fluidized bed boiler discharge not up to standard.The present invention includes circulating fluidized bed boiler, denitrification apparatus, limestone desulfurization system, dry method desulfuration system and bag-type dust removal system；The top of the burner hearth of circulating fluidized bed boiler is connected with separator, material returning device is connected with the bottom of the burner hearth of circulating fluidized bed boiler, denitrification apparatus is equipped between material returning device and burner hearth, burner hearth and back-end ductwork are connected respectively with limestone desulfurization system, the bottom of burner hearth is respectively equipped with coal feeder and individual layer overfire air device, back-end ductwork and bag-type dust removal system are connected respectively with dry method desulfuration system, and bag-type dust removal system is connected by ash-storing bin with dry method desulfuration system.The present invention is suitable for circulating fluidized bed boiler pollutant emission and controls.
Description
Technical field
Present invention relates particularly to a kind of circulating fluidized bed boiler minimum discharge cooperative control method and system integration devices.
Background technology
Circulating fluidized-bed boiler Combustion technology is because its environmental protection and energy saving performance having is rapidly developed, as new boiler is big
Gas pollutant emission standard is implemented, and accelerates burning in circulating fluid bed boiler Collaborative Control and auxiliary system integrates minimum discharge skill
The exploitation and application of art, and then minimum discharge and efficient burning and safe operation.Current existing circulating fluidized bed boiler,
A variety of environment-friendly processing units need to be arranged in governing system outside stove, solve the problems, such as that discharge is not up to standard, and the wet desulphurization of use,
The devices such as SCR denitration, wet dust removal or wet-esp equipment, there are cost of investment is big, operating cost is high for the mode of processing
The problem of, equipment corrosion can be also caused, further results in environmental pollution, such as discharge of wastewater, the escaping of ammonia and coloured plume, gypsum
Rain, haze etc..
The content of the invention
The present invention in order to solve the discharge of existing circulating fluidized bed boiler it is not up to standard and caused by environmental pollution and equipment
The problem of corrosion, and a kind of circulating fluidized bed boiler minimum discharge cooperative control method and system integration device are provided.
The present invention adopts the technical scheme that solve above-mentioned technical problem：
First, a part of lime stone of the certain particle size come out from limestone desulfurization system enters burner hearth, is carried out in burner hearth
Once desulfurization, once desulfurization enter separator and carry out secondary desulfuration, and flue gas is separated by separator, and lime stone and ash are through returning charge
Device enters burner hearth, such iterative cycles；
2nd, material is changed by the returning charge valve that coal feeder is controlled to enter on the fuel granularity and control material returning device of burner hearth
Internal circulating load；Using the single layer structure of overfire air device, burnt by adjusting the size of air door of overfire air device come enhanced fuel
Reducing atmosphere；To realize low nitrogen burning, denitration in the stove is completed；
3rd, another part lime stone come out from limestone desulfurization system enters back-end ductwork, and passes through with ash and flue gas
After cao activation reactor carries out humidification desulfurization, desulfurization again is carried out into dry method desulfuration system；
4th, after dry method desulfuration system desulfurization, lime stone, into bag-type dust removal system, flue gas is separated, lime with ash
With ash into ash-storing bin, lime stone and ash are sent to dry method desulfuration system and carry out desulfurization again, so cycled past stone by ash-storing bin
Multiple, purified flue gas is discharged by chimney；
5th, purified flue gas before chimney discharge through, by flue gas concentration detection device, detecting NOx, SO2, PM and ammonia etc.
The discharge content of pollutant, the feedback signal of generation are transferred to limestone desulfurization system, denitrification apparatus, dry method desulfuration system respectively
Change the amount of feeding so that emission compliance with the valve of each automatic adjustment on bag-type dust removal system.
A kind of circulating fluidized bed boiler minimum discharge system integration device, it is characterised in that：
It includes circulating fluidized bed boiler, limestone desulfurization system, dry method desulfuration system and bag-type dust removal system；
The top of the burner hearth of circulating fluidized bed boiler is connected with separator, the burner hearth of material returning device and circulating fluidized bed boiler
Bottom be connected, be provided with denitrification apparatus between material returning device and the burner hearth of circulating fluidized bed boiler, burner hearth and back-end ductwork point
It is not connected with limestone desulfurization system, the bottom of burner hearth is respectively equipped with coal feeder and individual layer overfire air device；
Back-end ductwork and bag-type dust removal system are connected respectively with dry method desulfuration system, bag-type dust removal system and ash-storing bin phase
Connection, ash-storing bin are connected with dry method desulfuration system.
Preferably, the denitrification apparatus is SNCR denitration device.
Further, cao activation reactor is provided between back-end ductwork and dry method desulfuration system.
The present invention has the advantages that compared with prior art：
First, afterbody of the present invention is integrated using humidification activation dry desulfurization and bag-type dust removal system, realizes SO2The ultralow row of flue dust
It puts, cost free removing SO3, heavy metal and wastewater zero discharge, and anti-corrosion is not required in flue and chimney, the flue gas blackness finally discharged
≤ 1 grade, PM ＜ 10mg/Nm3。
2nd, spare SNCR denitration device under special circumstances (such as boiler start-stop, sudden load change and coal fluctuation),
Ensure the emission compliance and stabilization of the wide coal NOx of full load.
3rd, the preferably optimal lime stone species of limestone desulfurization device, provides the lime stone that fluidized state in stove matches
Grain size and Spreading requirements, ensure optimal desulfuration efficiency, and conveying is simple and reliable, can meet boiler 8000 it is small when more than long-term connect
It is continuous steadily to run, and can realize that the accurate of lime stone conveying capacity adjusts and control.
4th, the present invention can be by existing NOx emission concentration from 100~250mg/Nm3Drop to 50mg/Nm3Within.
5th, desulfuration in furnace efficiency can be less than 95% and is increased to 99%, SO by the present invention from existing2Concentration of emission is from small
In 100mg/m3It drops to less than 35mg/m3。
Description of the drawings
Fig. 1 is the schematic diagram of the present invention；
Fig. 2 is the connection structure diagram of separator and material returning device；
Fig. 3 is the overall structure figure of separator；
Fig. 4 is the A-A sectional views of Fig. 3.
Specific embodiment
Specific embodiment one：Illustrate present embodiment with reference to Fig. 1, present embodiment it include circulating fluidized bed boiler
1st, limestone desulfurization system 2, denitrification apparatus 3, dry method desulfuration system 4 and bag-type dust removal system 5；
The top of the burner hearth 1-1 of circulating fluidized bed boiler 1 is connected with separator 1-2, material returning device 1-3 and recirculating fluidized bed
The bottom of the burner hearth 1-1 of boiler 1 is connected, and denitration is provided between the burner hearth 1-1 of material returning device 1-3 and circulating fluidized bed boiler 1
Device 3, burner hearth 1-1 and back-end ductwork 1-6 are connected respectively with limestone desulfurization system 2, the bottom of burner hearth 1-1 be respectively equipped with to
Device for coal 1-5 and individual layer overfire air device 1-4；
Back-end ductwork 1-6 and bag-type dust removal system 5 are connected respectively with dry method desulfuration system 4, bag-type dust removal system 5 and storage
Ash cellar 5-1 is connected, and ash-storing bin 5-1 is connected with dry method desulfuration system 4.
Circulating fluidized bed boiler 1, limestone desulfurization system 2, dry method desulfuration system 4 and bag-type dust removal system 5 are to pollutant
The mutual Collaborative Control of minimum discharge, and integrate to form pollutant minimum discharge system integration device by pipeline connection.
Individual layer overfire air device 1-4 of the present invention is the published skills of existing patent CN201610052478.8
Art is identical with Secondary Air structure recorded in existing patent CN201610052478.8.
Specific embodiment two：Illustrate present embodiment with reference to Fig. 1, denitrification apparatus 3 described in present embodiment is SNCR
Denitrification apparatus.
Present embodiment is at low cost, is influenced for boiler normal operation smaller.
Other compositions and connection relation are same as the specific embodiment one.
Specific embodiment three：Illustrate present embodiment with reference to Fig. 1, present embodiment back-end ductwork 1-6 takes off with dry method
Cao activation reactor 4-1 is provided between sulphur system 4.
Present embodiment can make the SO in the CaO and flue gas that are not chemically reacted in stove2This raw CaSO of reaction4So that
Desulfurization is able to deep exploitation, realizes the treatment of wastes with processes of wastes against one another, and cao activation reactor 4-1 may insure the situation in desulfuration in furnace fluctuation of operating conditions
Under, SO2Discharge stably reaching standard.
Present embodiment realizes the circulation desulfurization outside stove, further reduces the discharge of sulphur.It is other composition and connection relation and
Specific embodiment one or two is identical.
Specific embodiment four：Illustrate present embodiment with reference to Fig. 1, bag-type dust removal system 5 described in present embodiment with
Chimney 6 is connected, and flue gas concentration detection device 7 is provided in chimney 6.
Flue gas concentration detection device 7 is CEMS.
Flue gas inspection device 7 can detect chimney 6 and discharge SO in flue gas in real time2、NOx, PM and ammonia concentration of emission.
Other compositions and connection relation are identical with specific embodiment three.
Specific embodiment five：Illustrate present embodiment with reference to Fig. 2~Fig. 4, present embodiment separator 1-2 include into
The long flue 1-2-1 of mouth, cylinder 1-2-2, cone cylinder 1-2-3, standpipe 1-2-4 and central tube 1-4-5, the long flue 1-2-1's of import enters
Mouth is connected with burner hearth 1, and the outlet of the long flue 1-2-1 of import is connected with the top side wall of cylinder 1-2-2, the long flue 1-2-1 of import
Height h along its length is equal, and the width of the long flue 1-2-1 of import along its length is gradually reduced, the long flue of import
The throat width w1 of 1-2-1 is more than exit width w2, and cylinder 1-2-2, cone cylinder 1-2-3 and standpipe 1-2-4 from top to bottom connect successively
Lead to and one is made, central tube 1-4-5 is the rounded cylindrical structure of upper and lower opening, the upper end of central tube 1-4-5 and cylinder 1-2-2
Top be fixedly communicated, central tube 1-4-5 is that double offset is set, plane that x-axis and perpendicular y-axis are formed and cylinder 1-
The upper surface center of circle o that the upper surface of 2-2 overlaps and the intersection point of x-axis and y-axis is cylinder 1-2-2, x-axis and the long flue 1-2-1 of import
Entrance it is vertical, the upper surface center of circle o1 of central tube 1-4-5 is compared with the upper surface center of circle o of cylinder 1-2-2 first to the losing side of x-axis
A distance is biased to biasing a distance, then to the positive direction of y-axis.
Other compositions and connection relation are identical with specific embodiment four.
Specific embodiment six：Illustrate present embodiment with reference to Fig. 1, the control method described in present embodiment is as follows：
First, a part of lime stone of the certain particle size come out from limestone desulfurization system 2 enters burner hearth 1-1, in burner hearth 1-1
Interior carry out once desulfurization, once desulfurization enter separator 1-2 and carry out secondary desulfuration, and flue gas is separated by separator 1-2, lime
Stone and ash enter burner hearth 1-1, such iterative cycles through material returning device 1-3；
Flue gas flow control in burner hearth 1-1 in≤5m/s, can prevent burner hearth 1-1 heating surface wears；
2nd, the returning charge valve by the way that coal feeder 1-5 is controlled to enter on the fuel granularity and control material returning device 1-3 of burner hearth 1-1
To change solid circulating rate；Using overfire air device 1-4 single layer structures, the size of the air door by adjusting overfire air device 1-4
Carry out the reducing atmosphere of enhanced fuel burning；To realize low nitrogen burning, denitration in the stove is completed；
Preferably, the fuel granularity scope that coal feeder 1-5 enters burner hearth 1-1 is 0-8mm.
3rd, another part lime stone come out from limestone desulfurization system 2 enters back-end ductwork 1-6, and with ash and flue gas
After carrying out humidification desulfurization by cao activation reactor 4-1, desulfurization again is carried out into dry method desulfuration system 4；It is chemically reacted
Equation is as follows：
CaO+SO2+1/2O2=CaSO4
Ca(OH)2+SO3=CaSO4+H2O
Compared with wet desulphurization.Using cao activation reactor 4-1 desulfurization, it can realize that cost free deviates from SO3, heavy metal Hg
And the zero-emission of waste water, while can also realize that flue and chimney are not corroded, anti-corrosion need not be done；
4th, after 4 desulfurization of dry method desulfuration system, lime stone, into bag-type dust removal system 5, flue gas is separated, stone with ash
Lime stone and ash are sent to dry method desulfuration system 4 and carry out desulfurization again by lime stone with ash into ash-storing bin 5-1, ash-storing bin 5-1, such as
This moves in circles, and purified flue gas is discharged by chimney 6；
5th, by flue gas concentration detection device 7 before purified flue gas is discharged through chimney 6, NOx, SO are detected2, PM and ammonia
The discharge content of pollutants is waited, the feedback signal of generation is transferred to limestone desulfurization system 2, denitrification apparatus 3, dry desulfurization respectively
The valve of each automatic adjustment in system 4 and bag-type dust removal system 5 changes the amount of feeding so that emission compliance (NOX<50mg/Nm3、
SO2<35mg/Nm3、PM<10mg/Nm3)。
Specific embodiment seven：Illustrate present embodiment with reference to Fig. 1, the control method described in present embodiment is as follows：
The dry method desulfuration system 4 can be substituted with semi-dry desulphurization system.Other compositions and connection relation and specific reality
It is identical to apply mode six.
Specific embodiment eight：Illustrate present embodiment, 1 desulfurization of present embodiment circulating fluidized bed boiler with reference to Fig. 1
And ignition temperature during denitration is controlled between 850 DEG C -880 DEG C.
Present embodiment ensures flue gas, the residence time of ash and lime stone in burner hearth 1-1 and separator 1-2 to enhance stove
Interior desulfuration efficiency realizes high-efficiency desulfurization in stove.Other compositions and connection relation are identical with specific embodiment seven.
Specific embodiment nine：Illustrate present embodiment with reference to Fig. 1, present embodiment rises when circulating fluidized bed boiler 1
Stop, sudden load change and coal are fluctuated when special circumstances, it is necessary to which SNCR denitration device denitration, denitration liquid ammonium hydroxide or urea are molten
Liquid, by denitrification apparatus 3 into the inlet of separator 1-2, denitration liquid leads to denitration liquid after being mixed with flue gas in separator 1-2
Cross chemical reaction abjection NOx；Other compositions and connection relation are identical with specific embodiment eight.
Specific embodiment ten：Illustrate present embodiment with reference to Fig. 1, limestone granularity described in present embodiment is 0-
0.5mm。
Other compositions and connection relation are identical with specific embodiment nine.
Claims (10)
1. a kind of circulating fluidized bed boiler minimum discharge cooperative control method, it is characterised in that：
First, a part of lime stone of the certain particle size come out from limestone desulfurization system (2) enters burner hearth (1-1), in burner hearth (1-
1) once desulfurization is carried out in, once desulfurization enters separator (1-2) and carries out secondary desulfuration, and flue gas is isolated by separator (1-2)
It goes, lime stone and ash enter burner hearth (1-1), such iterative cycles through material returning device (1-3)；
2nd, by controlling coal feeder (1-5) into the returning charge on the fuel granularity of burner hearth (1-1) and control material returning device (1-3)
Valve changes solid circulating rate；Using the single layer structure of overfire air device (1-4), by the wind for adjusting overfire air device (1-4)
The size of door carrys out the reducing atmosphere of enhanced fuel burning；To realize low nitrogen burning, denitration in the stove is completed；
3rd, another part lime stone come out from limestone desulfurization system (2) enters back-end ductwork (1-6), and with ash and flue gas
After carrying out humidification desulfurization by cao activation reactor (4-1), desulfurization again is carried out into dry method desulfuration system (4)；
4th, after dry method desulfuration system (4) desulfurization, lime stone, into bag-type dust removal system (5), flue gas is separated, stone with ash
With ash into ash-storing bin (5-1), lime stone and ash are sent to dry method desulfuration system (4) and carried out again lime stone by ash-storing bin (5-1)
Desulfurization so moves in circles, and purified flue gas is discharged by chimney (6)；
5th, purified flue gas before chimney (6) discharge through, by flue gas concentration detection device (7), detecting NOx, SO2, PM and ammonia etc.
The discharge content of pollutant, the feedback signal of generation are transferred to limestone desulfurization system (2), denitrification apparatus (3), dry method and take off respectively
Sulphur system (4) and the valve of each automatic adjustment on bag-type dust removal system (5) change the amount of feeding so that emission compliance.
2. a kind of circulating fluidized bed boiler minimum discharge cooperative control method according to claim 1, it is characterised in that：Institute
Stating dry method desulfuration system (4) can be substituted with semi-dry desulphurization system.
3. a kind of circulating fluidized bed boiler minimum discharge cooperative control method according to claim 2, it is characterised in that：
Ignition temperature when circulating fluidized bed boiler (1) desulfurization and denitration is controlled between 850 DEG C -880 DEG C.
4. a kind of circulating fluidized bed boiler minimum discharge cooperative control method according to claim 3, it is characterised in that：
When circulating fluidized bed boiler (1) start-stop, sudden load change and coal fluctuate when special circumstances when, it is necessary to SNCR denitration device
Denitration, denitration liquid ammonium hydroxide or urea liquid, denitration liquid enter the inlet of separator (1-2), denitration by denitrification apparatus (3)
Liquid and flue gas mix in separator (1-2) after by chemical reaction abjection NOx；
5. a kind of circulating fluidized bed boiler minimum discharge cooperative control method according to claim 4, it is characterised in that：Institute
Limestone granularity is stated as 0-0.5mm.
6. a kind of circulating fluidized bed boiler minimum discharge system integration device, it is characterised in that：It includes circulating fluidized bed boiler
(1), limestone desulfurization system (2), denitrification apparatus (3), dry method desulfuration system (4) and bag-type dust removal system (5)；
The top of the burner hearth (1-1) of circulating fluidized bed boiler (1) is connected with separator (1-2), material returning device (1-3) and recycle stream
The bottom of the burner hearth (1-1) of fluidized bed boiler (1) is connected, material returning device (1-3) and the burner hearth (1-1) of circulating fluidized bed boiler (1)
Between be provided with denitrification apparatus (3), burner hearth (1-1) and back-end ductwork (1-6) are connected respectively with limestone desulfurization system (2),
The bottom of burner hearth (1-1) is respectively equipped with coal feeder (1-5) and individual layer overfire air device (1-4)；
Back-end ductwork (1-6) and bag-type dust removal system (5) are connected respectively with dry method desulfuration system (4), bag-type dust removal system (5)
It is connected with ash-storing bin (5-1), ash-storing bin (5-1) is connected with dry method desulfuration system (4).
7. a kind of circulating fluidized bed boiler minimum discharge system integration device according to claim 6, it is characterised in that：Institute
Denitrification apparatus (3) is stated as SNCR denitration device.
8. a kind of circulating fluidized bed boiler minimum discharge system integration device according to claim 6 or 7, feature exist
In：Cao activation reactor (4-1) is provided between back-end ductwork (1-6) and dry method desulfuration system (4).
9. a kind of circulating fluidized bed boiler minimum discharge system integration device according to claim 8, it is characterised in that：Institute
It states bag-type dust removal system (5) with chimney (6) to be connected, flue gas concentration detection device (7) is provided in chimney (6).
10. a kind of circulating fluidized bed boiler minimum discharge system integration device according to claim 9, it is characterised in that：
Separator (1-2) includes the long flue of import (1-2-1), cylinder (1-2-2), cone cylinder (1-2-3), standpipe (1-2-4) and central tube
(1-4-5), the entrance of the long flue of import (1-2-1) are connected with burner hearth (1), outlet and the cylinder (1- of the long flue of import (1-2-1)
Top side wall connection 2-2), the height (h) of the long flue of import (1-2-1) along its length is equal, the long flue (1-2- of import
1) width along its length is gradually reduced, and the throat width (w1) of the long flue of import (1-2-1) is more than exit width (w2),
Cylinder (1-2-2), cone cylinder (1-2-3) and standpipe (1-2-4) are from top to bottom sequentially communicated and one are made, central tube (1-4-5)
For the rounded cylindrical structure of upper and lower opening, the upper end of central tube (1-4-5) at the top of cylinder (1-2-2) with being fixedly communicated, center
Cylinder (1-4-5) is set for double offset, and the plane that x-axis and perpendicular y-axis are formed is overlapped with the upper surface of cylinder (1-2-2)
And the upper surface center of circle (o) that the intersection point of x-axis and y-axis is cylinder (1-2-2), x-axis and the entrance of the long flue of import (1-2-1) hang down
Directly, the upper surface center of circle (o1) of central tube (1-4-5) compared with cylinder (1-2-2) the upper surface center of circle (o) first to x-axis losing side
A distance is biased to biasing a distance, then to the positive direction of y-axis.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810032019.2A CN108105761B (en) | 2018-01-12 | 2018-01-12 | Ultra-low emission cooperative control method and system integration device for circulating fluidized bed boiler |
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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 |
| CN114135865A (en) * | 2021-12-20 | 2022-03-04 | 重庆大学 | High-temperature ash storage device and circulating fluidized bed boiler provided with same |
| CN116892722A (en) * | 2023-07-10 | 2023-10-17 | 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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