CN101639227B - High oxygen concentration oxygen-enriched pulverized coal fractional combustion method and device therefor - Google Patents
High oxygen concentration oxygen-enriched pulverized coal fractional combustion method and device therefor Download PDFInfo
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- CN101639227B CN101639227B CN2009100752731A CN200910075273A CN101639227B CN 101639227 B CN101639227 B CN 101639227B CN 2009100752731 A CN2009100752731 A CN 2009100752731A CN 200910075273 A CN200910075273 A CN 200910075273A CN 101639227 B CN101639227 B CN 101639227B
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
Abstract
The invention relates to a high oxygen concentration oxygen-enriched pulverized coal fractional combustion method and a device therefor. The invention has the technical scheme that a boiler type with three stages of series connection hearths is adopted; when in combustion, the pulverized coal and oxygen are respectively put into the hearths for combustion according to the proportion in the combustion process; all recycling flue gas is pumped back into the first hearth and is blended with part of the oxygen filled in the first hearth for transmitting the pulverized coal for the first hearth; part of the flue gas generated by the first hearth is blended with part of the oxygen filled in the second hearth for transmitting the pulverized coal for the second hearth; and part of the flue gas generated by the second hearth is blended with part of the oxygen filled in the third hearth for transmitting the pulverized coal for the second hearth. The total concentration of O2 in the boiler reaches 70-80%; as the next stage of hearth adopts the flue gas generated by combustion of the previous hearth as dilute gas, the actual concentration of O2 in every stage of hearth is within the range of 30-40%. The quantity of the recycling flue gas is much less than that in the current oxygen-enriched combustion boiler, and the electricity consumption in the running of a flue gas circulation fan is obviously lowered.
Description
Technical field
The present invention relates to coal fired power plant coal dust clean burning, particularly a kind of high oxygen concentration oxygen-enriched pulverized coal staged-combustion method belongs to the boiler technology field.
Background technology
Coal fired power plant is CO
2Concentrated emission source, from flue gas, separate and capture CO
2Be to implement CO
2Catch and seal up for safekeeping the key of (CCS) technology.Present most of boiler is with the air oxidant that acts as a fuel, CO in the flue gas that conventional air burning produces
2Concentration is 10%～14%, and all the other then mainly are N
2From N
2The middle separation and capture CO
2It is huge to consume energy.And oxygen-enriched combustion technology produces the N in the flue gas
2Content seldom is convenient to the compression cooling and is obtained liquid CO
2, and remove simultaneously or reclaim other pollutant, as SO
2Deng pernicious gas.In the oxygen-enriched combusting process, the general using air is made purity oxygen, then with purity oxygen and a certain amount of CO
2The burning of blending coal supply powder is used, so oxygen-enriched combusting is also referred to as O
2/ CO
2The atmosphere burning, the flue gas that this moment, coal dust firing produced is through its CO of simple process
2Concentration can reach more than 90%.And and O
2The CO of blending
2Then take from the part that coal dust firing produces flue gas, that is to say that a part is to utilize circulating fan to feed back to utilize in the flue gas, remainder then compresses and stores.Owing to contain water vapour (generally more than 15%) in the flue gas that coal combustion produces, so O
2/ CO
2In the atmosphere combustion process, combustion-supporting gas mainly contains O
2, CO
2, H
2O.O in the combustion-supporting gas in the existing oxygen-enriched combustion technology
2Generally account for about 30%, under this condition, because O in the combustion-supporting gas
2Ratio is little, and the amount of circulating gas that needs is big, and flue gas recirculation blower fan power consumption is also bigger, and the boiler operatiopn expense is higher.Because CO in the existing oxygen-enriched combustion technology flue gas
2Ratio is far above CO in the flue gas under the air burning condition
2Ratio, so theoretical temperature combustion is a little less than the air burning condition.Improve O in the combustion-supporting gas
2Ratio, can reduce amount of circulating gas, thereby effectively reduce flue gas recirculation blower fan power consumption.But under current combustion system, burn,, will cause coal dust to carry in the gas oxygen concentration too high, easily cause to cause taking place in the coal dust carrier pipe spontaneous combustion of pulverized coal even detonation if amount of circulating gas is very few because coal dust needs to be delivered to boiler by combustion-supporting gas.
Summary of the invention
Problem to be solved by this invention is: provide a kind of and can effectively reduce flue gas recirculation blower fan power consumption, higher high oxygen concentration oxygen-enriched pulverized coal staged-combustion method and the device of theoretical temperature combustion.
The alleged problem of the present invention is solved by following technical scheme:
A kind of high oxygen concentration oxygen-enriched pulverized coal staged-combustion method, its special feature is: as burner, described plural serial stage burner hearth is three grades, is called first burner hearth, second burner hearth and the 3rd burner hearth with the boiler of plural serial stage burner hearth for it; Combustion process is with coal dust total amount and O
215%～20%, 28%～33%, 47%～57% of total amount is put into first, second, third burner hearth respectively, and all flue gas recycleds are drawn back to first burner hearth, and wherein, flue gas recycled accounts for 15%～23% of flue gas total amount, drops into the first burner hearth O
2In according to O
27%～9.6% and flue gas recycled blending pulverized coal conveying of total amount, all the other required oxygen that burn are directly sent into first burner hearth; 46%～50% of first burner hearth burning flue gas that produces is drawn by blower fan, is cooled to 120 ℃～150 ℃, again with O
26%～7% of total amount is mixed the back and is carried the burning of second burner hearth to use coal dust, drops into all the other required oxygen that burn of second burner hearth and directly sends into second burner hearth, and all the other flue gases that the burning of first burner hearth produces then flow directly into second burner hearth; The burning of second burner hearth produces 46%～50% in the flue gas and is drawn by blower fan, is cooled to 120 ℃～150 ℃, again with O
28%～10% of total amount is mixed the back and is carried the burning of the 3rd burner hearth to use coal dust, drops into all the other required oxygen that burn of the 3rd burner hearth and directly sends into the 3rd burner hearth, and all the other flue gases that the burning of second burner hearth produces then flow directly into the 3rd burner hearth.
A kind of high oxygen concentration oxygen-enriched pulverized coal staged combustion device, it comprises boiler body, air-introduced machine, circulating fan, air separator, send oxygen blower fan and coal dust feed bin, described boiler body is by first burner hearth, second burner hearth, the 3rd burner hearth is formed, described coal dust feed bin is three, they are communicated with first by three defeated coal channels respectively, second, the 3rd burner hearth, described first, be communicated with by the first furnace exhaust road between second burner hearth, second, be communicated with by the second furnace exhaust road between the 3rd burner hearth, the outlet in the 3rd furnace exhaust road is provided with dust arrester, dust arrester is through smoke evacuation pipeline connection air-introduced machine, the described oxygen blower fan that send is communicated with air separator and oxygen deliverng pipe road respectively, article three, burning oxygen supply branch road is respectively with oxygen deliverng pipe road and first, second, the 3rd burner hearth is communicated with, article three, defeated coal oxygen supply branch road is respectively with oxygen deliverng pipe road and first, second, the defeated coal channel of the 3rd burner hearth is communicated with, described circulating fan is communicated with smoke exhaust pipe and the defeated coal channel of first burner hearth through pipeline, the defeated coal channel of described second burner hearth is through the first burner hearth smoke induced draught fan, first cooler is communicated with the first furnace exhaust road, and the defeated coal channel of described the 3rd burner hearth is through the second burner hearth smoke induced draught fan, second cooler is communicated with the second furnace exhaust road.
Above-mentioned high oxygen concentration oxygen-enriched pulverized coal staged combustion device, the described first furnace exhaust road is suitable for reading to be arranged on first upper furnace, end opening is arranged on second lower furnace portion, the described second furnace exhaust road is suitable for reading to be arranged on second upper furnace, end opening is arranged on the 3rd lower furnace portion, and the 3rd furnace exhaust road is positioned at the 3rd upper furnace.
Above-mentioned high oxygen concentration oxygen-enriched pulverized coal staged combustion device is equipped with flow control valve on described three burning oxygen supply branch roads and three defeated coal oxygen supply branch roads.
The present invention is directed to oxygen-enriched combustion technology and reduce amount of circulating gas, and O in the control combustion-supporting gas
2Ratio and the problem that causes has proposed a kind of three grades of high oxygen concentration oxygen-enriched combustion technologies of burner hearth, compared with prior art, main feature of the present invention is as follows: 1. boiler O
2Total concentration can reach 75～80%, and the flue gas recycled amount obviously reduces, and effectively reduces flue gas recirculation blower fan power consumption; 2. the coal dust fractional combustion makes three grades of actual O of burner hearth combustion process
2Concentration is controlled at 33%～45%; Three grades of burner hearth theoretical temperature combustions all than conventional oxygen-rich coal dust stove and air burning stove height, help the abundant after-flame of fuel 2200～2600 ℃ of scopes; 3. owing to the theoretical temperature combustion height, three grades of burner hearths all can adopt the slag tap mode to carry out deslagging, and it is long-pending to help reducing furnace heating surface, and because whole flue gases all are recovered, the NOx that combustion process Yin Gaowen produces also no longer becomes problem; 4. the flue gas of prime burner hearth burning generation plays the effect of controlling ignition temperature on the one hand as the diluent gas of back level burner hearth burning; And the effect that front burner hearth burning generation flue gas is heated up is again played in the burning of back level burner hearth after cooling on the other hand, makes along whole flow of flue gas direction flue-gas temperature and remains on higher level, helps each heating surface heat exchange.
Description of drawings
Fig. 1 is apparatus of the present invention schematic diagrames.
Label is expressed as follows in the accompanying drawing: 1. first burner hearth; 2. second burner hearth; 3. the 3rd burner hearth; 4. the first furnace exhaust road; 5. the second furnace exhaust road; 6. the 3rd furnace exhaust road; 7. dust arrester; 8. smoke exhaust pipe; 9. circulating fan; 10. the 3rd burner hearth burning oxygen supply branch road; 11. the 3rd burner hearth is failed coal channel; 12. the 3rd burner hearth feed bin; 13. the 3rd burner hearth is failed coal oxygen supply branch road; 14. the second burner hearth smoke induced draught fan; 15. second cooler; 16. second burner hearth burning oxygen supply branch road; 17. second burner hearth is failed coal channel; 18. second burner hearth is failed coal oxygen supply branch road; 19. the second burner hearth feed bin; 20. the first burner hearth smoke induced draught fan; 21. first cooler; 22. first burner hearth is failed coal oxygen supply branch road; 23. send the oxygen blower fan; 24. air separator; 25. the first burner hearth feed bin; 26. first burner hearth is failed coal channel; 27. first burner hearth burning oxygen supply branch road; 28. air-introduced machine; 29. flow control valve, 30. oxygen deliverng pipe roads.
The specific embodiment
The high oxygen concentration oxygen-enriched pulverized coal staged-combustion method that the present invention proposes is implemented on the boiler with three grades of series connection burner hearths, and it can be with O in the combustion-supporting gas
2Ratio is increased to 75%～80%, and oxygen concentration is controlled at 18%～22% in the coal dust conveying gas, and the combustion process theoretical temperature combustion is controlled at 2200～2600 ℃.The inventive method is put into fractional combustion in three burner hearths with coal dust, is furnished with heating surface in each burner hearth and between burner hearth.Combustion process is with coal dust total amount and O
215%～20%, 28%～33%, 47%～57% of total amount is put into first, second, third burner hearth respectively, and all flue gas recycleds are also drawn back to first burner hearth by recirculation blower.Wherein, flue gas recycled accounts for 15%～23% of flue gas total amount, therefore, is dropped in the actual O of first burner hearth
2In flue gas, O
2Only account for 36%～44.4%, theoretical temperature combustion is 2200 ℃～2600 ℃.Flue gas recycled all is used to carry the required coal dust of first burner hearth, for guaranteeing that coal dust in time catches fire O in first burner hearth
27%～9.6% and flue gas recycled blending of total amount are the first burner hearth pulverized coal conveying, like this O in the powder feeding gas
2Ratio can be controlled in 18%～22%, with O in the air
2Concentration is suitable, can avoid the spontaneous combustion and the detonation of coal dust.All the other drop into the oxygen of first burner hearth and directly send into first burner hearth by pipeline.
The burning of first burner hearth is produced 46%～50% in the flue gas draw, be cooled to 120～150 ℃ through gas cooler, again with total O by blower fan
26%～7% mix the back and carry the second burner hearth required coal dust that burns to enter second burner hearth, O in the powder feeding gas like this
2Ratio also can be controlled in 17%～22% scope.All the other flue gases that the burning of first burner hearth produces then flow directly into second burner hearth, and all the other oxygen that the burning of second burner hearth needs are directly sent into second burner hearth, not with the coal dust blending.Because first burner hearth produces the diluting effect of flue gas, O in the total gas of second burner hearth
2Can be controlled in 36%～39% scope.If directly entering second chamber flue gas temperature is 300～500 ℃, then the second burner hearth theoretical temperature combustion is 2300～2520 ℃.
Coal dust firing in second burner hearth is produced 46%～50% in the flue gas draw, be chilled to but 120～150 ℃ through heat exchanger, with total O by blower fan
28%～10% mix after, be used to carry the burning of the third level burner hearth coal dust, powder feeding gas O
2Concentration also can be controlled in 18%～21%.Required all the other O of third level burner hearth burning
2Directly send into third level burner hearth.Because second burner hearth produces the diluting effect of flue gas, the actual O of third level burner hearth
2Concentration can be controlled in 33%～43% scope, is 300～500 ℃ if hypothesis flows into flue-gas temperature by second burner hearth, and the 3rd burner hearth theoretical temperature combustion is 2200～2600 ℃.
Owing to be O
2/ CO
2The atmosphere burning, and because flue gas reclaims, three burner hearths all can adopt slag tap mode deslagging, needn't consider the problem that the NOx growing amount is high, and as can be seen, the diluent gas that the flue gas that burner hearth burning in front is produced burns as back grade burner hearth plays the effect of control ignition temperature on the one hand; And the effect that front burner hearth burning generation flue gas is heated up is again played in the burning of back level burner hearth after cooling on the other hand, makes along whole flow of flue gas direction, and flue-gas temperature remains on higher level, helps each heating surface heat exchange.
Referring to Fig. 1, apparatus of the present invention comprise boiler body, air-introduced machine 28, circulating fan 9, air separator 24, send oxygen blower fan 23 and coal dust feed bin.Boiler body is made up of first burner hearth 1, second burner hearth 2, the 3rd burner hearth 3 of three connections, corresponding three burner hearths, and the coal dust feed bin also is provided with three, and they are communicated with first, second, third burner hearth by three defeated coal channels 26,17,11 respectively.Be arranged on the first furnace exhaust road 4 that first upper furnace, end opening be arranged on second lower furnace portion and be communicated with by suitable for reading between first, second burner hearth, be arranged on the second furnace exhaust road 5 that second upper furnace, end opening be arranged on the 3rd lower furnace portion and be communicated with by suitable for reading between second, third burner hearth.The 3rd furnace exhaust road 6 is arranged on the 3rd upper furnace, and the outlet in the 3rd furnace exhaust road is provided with dust arrester 7, and dust arrester is communicated with air-introduced machine 28 through smoke evacuation pipeline 8, and the said structure setting helps flue gas and fully is distributed in each burner hearth.The described oxygen blower fan 23 that send is communicated with 30, three burnings of air separator 24 and oxygen deliverng pipe road oxygen supply branch road 27,16,10 respectively respectively with oxygen deliverng pipe road 30 and the connection of first, second, third burner hearth, in order to directly to carry the oxygen for burning usefulness to each burner hearth.Article three, defeated coal oxygen supply branch road 22,18,13 is communicated with the defeated coal channel 26 of oxygen deliverng pipe road 30 and first burner hearth, the defeated coal channel 17 of second burner hearth, the defeated coal channel 11 of the 3rd burner hearth respectively, in order to the flue gas blending after pulverized coal conveying.Described circulating fan 9 is communicated with smoke exhaust pipe 8 and the defeated coal channel 26 of first burner hearth through pipeline, all carries the required coal dust of first burner hearth behind a certain amount of oxygen of flue gas recycled blending.The defeated coal channel 17 of described second burner hearth is communicated with the first furnace exhaust road 4 through the first burner hearth smoke induced draught fan 20, first cooler 21, after the partial fume of first burner hearth is extracted out by the first burner hearth smoke induced draught fan 20, with the required coal dust of conveying second burner hearth after a certain amount of oxygen blending.The defeated coal channel 11 of described the 3rd burner hearth is communicated with the second furnace exhaust road 5 through the second burner hearth smoke induced draught fan 14, second cooler 15, after the partial fume of second burner hearth is extracted out by the second burner hearth smoke induced draught fan 14, with the required coal dust of conveying the 3rd burner hearth after a certain amount of oxygen blending.As seen from the figure, for regulating oxygen flow, be equipped with flow control valve 29 on 27,16,10 and three defeated coal oxygen supply branch roads 22,18,13 of described three burning oxygen supply branch roads.
Point out in passing, staged-combustion method provided by the present invention and device are according to three grades of chamber design, according to mentality of designing of the present invention, the high oxygen concentration oxygen-enriched pulverized coal staged-combustion method can promote the use of in the oxygen-rich coal dust multistage combustions such as secondary, level Four, Pyatyi according to mentality of designing of the present invention fully.
Several specific embodiments below are provided:
Embodiment 1: coal-fired by the calculating of Fuxin coal, the constituent analysis of coal is: C
Ar=48.3%, H
Ar=3.3%, O
Ar=8.6%, N
Ar=0.8%S
Ar=1.0%, A
Ar=23%, M
Ar=15%, Q
Net, ar=18645 (kJ/kg), V
Daf=41%.With the boiler fired coal amount is that 100t/h is an example, is chronomere with the second, the coal-fired 27.78kg/s of per second.For guaranteeing that coal dust fully burns, make excessive O
2Coefficient is 1.05, then needs O
2Be 30.09m
3/ s.Make O in the combustion-supporting gas
2Concentration is 80%, needs circulating flue gas 7.52m
3/ s, then combustion process produces total exhaust gas volumn 48.27m
3/ s, flue gas recycled account for 15.58% of total flue gas.Be the standard state volume with upper volume.Concrete scheme is:
Total coal dust amount and total O
215%, 28% and 57% be dropped in first, second and the 3rd burner hearth respectively.Just the first burner hearth Coal-fired capacity is 4.17kg/s, and the oxygen amount is 4.51m
3/ s; The second burner hearth Coal-fired capacity is 7.78kg/s, and the oxygen amount is 8.43m
3/ s; The 3rd burner hearth Coal-fired capacity is 15.83kg/s, and the oxygen amount is 17.15m
3/ s.
All flue gas recycleds are 7.52m just
3/ s flue gas is drawn back to first burner hearth by recirculation blower, therefore, is dropped in the actual O of first burner hearth
2In flue gas, O
2Only account for 37.5%, theoretical temperature combustion is 2483 ℃.Flue gas recycled is 7.52m just
3/ s flue gas can all be used for pulverized coal conveying, for guarantee that coal dust in time catches fire in first burner hearth, with total O
26.64% with flue gas blending pulverized coal conveying, O in the powder feeding gas like this
2Ratio be 21%, with O in the air
2Concentration is suitable, can avoid the spontaneous combustion and the detonation of coal dust.Required all the other oxygen of first burner hearth burning (account for total oxygen 8.36%) not with the coal dust blending, directly send into first burner hearth.The exhaust gas volumn that the burning of first burner hearth produces is 13.63m
3/ s.
The burning of first burner hearth produces 48.8% in the flue gas and is drawn by blower fan, is cooled to 120～150 ℃ through gas cooler, again with total O
25.88% mix the back and carry the 7.78kg/s coal dust to enter second burner hearth, O in the powder feeding gas like this
2Ratio also is 21%.All the other flue gases that first burner hearth burning produces then flow directly into second burner hearth, required all the other oxygen of second burner hearth burning (account for total oxygen 22.12%) not with the coal dust blending, directly send into second burner hearth.Because first burner hearth burning produces the diluting effect of flue gas, be dropped in O in total gas of second burner hearth
2Account for 37.22%.If directly entering second chamber flue gas temperature is 300～500 ℃, the second burner hearth theoretical temperature combustion is 2476～2514 ℃.The exhaust gas volumn that the burning of second burner hearth produces is 25.04m
3/ s.
Coal dust and required O in third level burner hearth input 57%
2(15.83kg/s coal dust, 17.15m
3/ sO
2), coal dust firing in second burner hearth is produced 54.1% in the flue gas, be chilled to but 120～150 ℃ through heat exchanger, and with total O
212% mix, be used to carry the burning of the third level burner hearth coal dust, powder feeding gas O
2Concentration is 21%.Required all the other O of third level burner hearth burning
2Directly send into third level burner hearth.Because second level burner hearth produces the diluting effect of flue gas, the actual O of third level burner hearth
2Concentration is 40.64%, is 300～500 ℃ if hypothesis flows into flue-gas temperature by second burner hearth, and the 3rd burner hearth theoretical temperature combustion is 2371 ℃～2421 ℃.
Embodiment 2: coal-fired by the calculating of Yangquan anthracite, the constituent analysis of coal is: C
Ar=68.9%, H
Ar=2.9%, O
Ar=2.4%, N
Ar=1%S
Ar=0.8%, A
Ar=19%, M
Ar=5%, Q
Net, ar=26400 (kJ/kg), V
Daf=9%.With the boiler fired coal amount is that 100t/h is an example, is chronomere with the second, the coal-fired 27.78kg/s of per second.For guaranteeing that coal dust fully burns, make excessive O
2Coefficient is 1.05, then needs O
2Be 41.87m
3/ s.Make O in the combustion-supporting gas
2Concentration is 75%, needs circulating flue gas 13.95m
3/ s, then combustion process produces total exhaust gas volumn 55.83m
3/ s, flue gas recycled account for 22.9% of total flue gas.Be the standard state volume with upper volume.Concrete scheme is:
Total coal dust amount and total O
220%, 33% and 47% be dropped in first, second and the 3rd burner hearth respectively.Just the first burner hearth Coal-fired capacity is 5.56kg/s, and the oxygen amount is 8.37m
3/ s; The second burner hearth Coal-fired capacity is 9.17kg/s, and the oxygen amount is 13.82m
3/ s; The 3rd burner hearth Coal-fired capacity is 13.06kg/s, and the oxygen amount is 19.68m
3/ s.
All flue gas recycleds are 13.95m just
3/ s flue gas is drawn back to first burner hearth by recirculation blower, therefore, is dropped in the actual O of first burner hearth
2In flue gas, O
2Only account for 37.5%, theoretical temperature combustion is 2222 ℃.Flue gas recycled is 13.95m just
3/ s flue gas can all be used for pulverized coal conveying, for guarantee that coal dust in time catches fire in first burner hearth, with total O
29.55% with flue gas blending pulverized coal conveying, O in the powder feeding gas like this
2Ratio be 21%, with O in the air
2Concentration is suitable, can avoid the spontaneous combustion and the detonation of coal dust.Required all the other oxygen of first burner hearth burning (account for total oxygen 10.45%) not with the coal dust blending, directly send into first burner hearth.The exhaust gas volumn that the burning of first burner hearth produces is 23.31m
3/ s.
The burning of first burner hearth produces 46.83% in the flue gas and is drawn by blower fan, is cooled to 120～150 ℃ through gas cooler, again with total O
27.17% mix the back and carry the 9.17kg/s coal dust to enter second burner hearth, O in the powder feeding gas like this
2Ratio also is 21%.All the other flue gases that first burner hearth burning produces then flow directly into second burner hearth, required all the other oxygen of second burner hearth burning (account for total oxygen 25.83%) not with the coal dust blending, directly send into second burner hearth.Because first burner hearth burning produces the diluting effect of flue gas, be dropped in O in total gas of second burner hearth
2Account for 38.2%.If directly entering second chamber flue gas temperature is 300～500 ℃, the second burner hearth theoretical temperature combustion is 2476～2514 ℃.The exhaust gas volumn that the burning of second burner hearth produces is 25.04m
3/ s.
Coal dust and required O in third level burner hearth input 57%
2(15.83kg/s coal dust, 17.15m
3/ s O
2), coal dust firing in second burner hearth is produced 54.1% in the flue gas, be chilled to but 120～150 ℃ through heat exchanger, and with total O
212% mix, be used to carry the burning of the third level burner hearth coal dust, powder feeding gas O
2Concentration is 21%.Required all the other O of third level burner hearth burning
2Directly send into third level burner hearth.Because second level burner hearth produces the diluting effect of flue gas, the actual O of third level burner hearth
2Concentration is 40.64%, is 300～500 ℃ if hypothesis flows into flue-gas temperature by second burner hearth, and the 3rd burner hearth theoretical temperature combustion is 2558 ℃～2590 ℃.
Claims (4)
1. high oxygen concentration oxygen-enriched pulverized coal staged-combustion method is characterized in that: as burner, described plural serial stage burner hearth is three grades, is called first burner hearth, second burner hearth and the 3rd burner hearth with the boiler of plural serial stage burner hearth for it; In combustion process with coal dust total amount and O
215%～20%, 28%～33%, 47%～57% of total amount is put into first, second, third burner hearth respectively, and all flue gas recycleds are drawn back to first burner hearth, and wherein, flue gas recycled accounts for 15%～23% of flue gas total amount; Drop into the first burner hearth O
2In according to O
27%～9.6% and flue gas recycled blending pulverized coal conveying of total amount, the required oxygen of all the other burnings are directly sent into first burner hearth; 46%～50% of first burner hearth burning flue gas that produces is drawn by blower fan, is cooled to 120 ℃～150 ℃, again with O
26%～7% of total amount is mixed the back and is carried the second burner hearth used coal dust that burns, and drops into all the other required oxygen that burn of second burner hearth and directly sends into second burner hearth, and all the other flue gases that the burning of first burner hearth produces then flow directly into second burner hearth; The burning of second burner hearth produces 46%～50% in the flue gas and is drawn by blower fan, is cooled to 120 ℃～150 ℃, again with O
28%～10% of total amount is mixed the back and is carried the burning of the 3rd burner hearth to use coal dust, drops into all the other required oxygen that burn of the 3rd burner hearth and directly sends into the 3rd burner hearth, and all the other flue gases that the burning of second burner hearth produces then flow directly into the 3rd burner hearth.
2. high oxygen concentration oxygen-enriched pulverized coal staged combustion device of using of method according to claim 1, it is characterized in that: it comprises boiler body, air-introduced machine (28), circulating fan (9), air separator (24), send the feed bin of oxygen blower fan (23) and pulverized coal conveying, and described boiler body is composed in series by first burner hearth (1), second burner hearth (2), the 3rd burner hearth (3); Described feed bin is three, is respectively the first burner hearth feed bin, the second burner hearth feed bin and the 3rd burner hearth feed bin, and three feed bins are communicated with first, second, third burner hearth by defeated coal channel respectively; Be communicated with by the first furnace exhaust road (4) between described first, second burner hearth, be communicated with by the second furnace exhaust road (5) between second, third burner hearth; The outlet in the 3rd furnace exhaust road (6) is provided with dust arrester (7), and dust arrester is communicated with air-introduced machine (28) through smoke evacuation pipeline (8); The described oxygen blower fan (23) that send is communicated with air separator (24) and oxygen deliverng pipe road (30) respectively, article three, burning oxygen supply branch road is communicated with oxygen deliverng pipe road and first, second, third burner hearth respectively, and three defeated coal oxygen supply branch roads are communicated with oxygen deliverng pipe road and the defeated coal channel of first, second, third burner hearth respectively; Described circulating fan (9) is communicated with smoke exhaust pipe (8) and the defeated coal channel (26) of first burner hearth through pipeline, the defeated coal channel (17) of described second burner hearth is communicated with the first furnace exhaust road (4) through the first burner hearth smoke induced draught fan (20), first cooler (21), and the defeated coal channel (11) of described the 3rd burner hearth is communicated with the second furnace exhaust road (5) through the second burner hearth smoke induced draught fan (14), second cooler (15).
3. high oxygen concentration oxygen-enriched pulverized coal staged combustion device according to claim 2, it is characterized in that: the described first furnace exhaust road (4) is suitable for reading to be arranged on first upper furnace, end opening is arranged on second lower furnace portion, the described second furnace exhaust road (5) is suitable for reading to be arranged on second upper furnace, end opening is arranged on the 3rd lower furnace portion, and the 3rd furnace exhaust road (6) is positioned at the 3rd upper furnace.
4. high oxygen concentration oxygen-enriched pulverized coal staged combustion device according to claim 3 is characterized in that: described three burnings are supported on branch road and three defeated coal oxygen supply branch roads and are equipped with flow control valve (29).
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| CN101839476A (en) * | 2010-06-22 | 2010-09-22 | 华中科技大学 | Method for micro positive pressure oxygen-enriched combustion of pulverized coal |
| CN101839474B (en) * | 2010-06-22 | 2011-05-18 | 华中科技大学 | Method for re-circulating combustion of flue gas of pulverized coal fired boiler |
| US9657937B2 (en) * | 2010-08-23 | 2017-05-23 | Saudi Arabian Oil Company | Steam generation system having multiple combustion chambers and dry flue gas cleaning |
| CN102494334B (en) * | 2011-12-22 | 2013-12-25 | 上海锅炉厂有限公司 | Coal powder combustion system used in high-moisture type coal oxygen-enriched combustion |
| CN103062789B (en) * | 2012-12-25 | 2015-07-01 | 西安交通大学 | System and method for utilizing flue gas circulation to prevent deflagration of hearth bottom |
| CN104990066B (en) * | 2015-07-24 | 2018-05-25 | 重庆森盟新能源开发有限公司 | One kind automatically controls multi-stage biological matter combustion system |
| CN104949105B (en) * | 2015-07-24 | 2017-12-01 | 重庆巴洛克新能源有限公司 | One kind automatically controls biomass combustion system |
| CN105444157A (en) * | 2015-11-24 | 2016-03-30 | 洛阳开拓新能源开发有限公司 | Biomass combustion furnace |
| CN110645567A (en) * | 2019-10-29 | 2020-01-03 | 辽宁绿源能源环保科技集团有限责任公司 | Pulverized coal boiler structure and pulverized coal combustion method |
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