CN103542407A - Flying ash recirculating device and flying ash recirculating method for circulating fluidized bed boiler - Google Patents
Flying ash recirculating device and flying ash recirculating method for circulating fluidized bed boiler Download PDFInfo
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- CN103542407A CN103542407A CN201310518978.2A CN201310518978A CN103542407A CN 103542407 A CN103542407 A CN 103542407A CN 201310518978 A CN201310518978 A CN 201310518978A CN 103542407 A CN103542407 A CN 103542407A
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- 238000000034 method Methods 0.000 title claims abstract description 18
- 230000003134 recirculating effect Effects 0.000 title abstract description 12
- 239000000428 dust Substances 0.000 claims abstract description 108
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 34
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 34
- 239000007787 solid Substances 0.000 claims abstract description 9
- 239000002956 ash Substances 0.000 claims description 156
- 239000000463 material Substances 0.000 claims description 30
- 239000003500 flue dust Substances 0.000 claims description 19
- 239000003546 flue gas Substances 0.000 claims description 18
- 230000008676 import Effects 0.000 claims description 18
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 17
- 239000003795 chemical substances by application Substances 0.000 claims description 13
- 239000003245 coal Substances 0.000 claims description 13
- 230000003009 desulfurizing effect Effects 0.000 claims description 12
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 11
- 239000000292 calcium oxide Substances 0.000 claims description 11
- 239000010881 fly ash Substances 0.000 claims description 10
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 9
- 239000007789 gas Substances 0.000 claims description 8
- 238000004064 recycling Methods 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 3
- 235000019738 Limestone Nutrition 0.000 abstract description 33
- 239000006028 limestone Substances 0.000 abstract description 33
- 238000006477 desulfuration reaction Methods 0.000 abstract description 23
- 230000023556 desulfurization Effects 0.000 abstract description 12
- 239000002245 particle Substances 0.000 abstract description 10
- 239000000779 smoke Substances 0.000 abstract description 2
- 235000013339 cereals Nutrition 0.000 description 11
- 238000012432 intermediate storage Methods 0.000 description 9
- 239000008187 granular material Substances 0.000 description 8
- 239000000446 fuel Substances 0.000 description 7
- 238000003860 storage Methods 0.000 description 7
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 5
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 235000002918 Fraxinus excelsior Nutrition 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 239000005864 Sulphur Substances 0.000 description 3
- 239000004568 cement Substances 0.000 description 3
- 239000010883 coal ash Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- 238000009434 installation Methods 0.000 description 3
- 239000004575 stone Substances 0.000 description 3
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- JGIATAMCQXIDNZ-UHFFFAOYSA-N calcium sulfide Chemical compound [Ca]=S JGIATAMCQXIDNZ-UHFFFAOYSA-N 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- 229910052698 phosphorus Inorganic materials 0.000 description 2
- 239000011574 phosphorus Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- -1 distributor 3 Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 235000013312 flour Nutrition 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000003837 high-temperature calcination Methods 0.000 description 1
- 238000005213 imbibition Methods 0.000 description 1
- 238000010348 incorporation Methods 0.000 description 1
- 230000006698 induction Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000007616 round robin method Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- HUAUNKAZQWMVFY-UHFFFAOYSA-M sodium;oxocalcium;hydroxide Chemical compound [OH-].[Na+].[Ca]=O HUAUNKAZQWMVFY-UHFFFAOYSA-M 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000002594 sorbent Substances 0.000 description 1
- 230000005532 trapping Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Abstract
The invention provides a flying ash recirculating device and a flying ash recirculating method for a circulating fluidized bed boiler. A smoke outlet of the boiler is communicated with a cyclone separator; a gas outlet of the cyclone separator is communicated with a dust remover through a heat exchanger; a solid outlet of the cyclone separator is communicated with a large-particle high-temperature ash inlet of a return feeder; a gas outlet of the dust remover is communicated with a chimney; a solid outlet of the dust remover is communicated with an ash conveying mother tube through a storehouse pump; one path of an outlet of the ash conveying mother tube is communicated with an ash storehouse, and the other path of the ash conveying mother tube is communicated with a circulating ash inlet of the return feeder; an outlet of the return feeder is communicated with a boiler furnace; large-particle high-temperature ash which is caught by the cyclone separator and has temperature of about 900 DEG C is mixed with low-temperature circulating ash which is caught by the dust remover and has temperature of lower than 150 DEG C; the temperature of mixed circulating ash entering the boiler furnace is up to 850 DEG C. The flying ash recirculating device disclosed by the invention can improve the combusting and burning performance of non-burned carbon particles in the circulating ash in the boiler furnace, effectively reduces the carbon content of flying ash and increase the utilization rate of desulfurization limestone in the boiler, runs safely and stably and can be used in the circulating fluidized bed boiler.
Description
Technical field
The present invention relates to high-efficiency cleaning combustion field, particularly a kind of CFBB flying dust EGR and flying ash recycling method.
Background technology
Owing to having, advantage ， China development such as fuel tolerance is wide, clean burning rapidly, and occupies the market share that China's energy market is larger to CFBB.Coal-fired in CFBB internal combustion, desulfurizing agent is after desulfuration in furnace, the high-temperature flue gas producing carries a large amount of particles and (comprises: coal ash and desulfurization product, unburnt carbon granule, unreacted desulfurizing agent) leave and enter cyclone separator after boiler and carry out gas solid separation, bulky grain high temperature ash is captured down and returns to burner hearth through standpipe and material returning device, flue gas carries after fine grained (being flying dust) enters heat exchanger heat release and enters deduster, overwhelming majority flying dust (surpassing 99%) is trapped and is sent to grey storehouse by deduster, cleaning flue gases after dedusting is in the middle of chimney is drained into atmosphere.
Due to reasons such as the time of staying of coal particle in burner hearth is limited, burning in circulating fluid bed boiler temperature lower (generally lower than 950 ℃), the unburned carbon in flue dust of boiler is generally between 3% to 20%, even, up to 30%, the unburned carbon in flue dust height of CFBB is the one of the main reasons that causes boiler efficiency to reduce.Overwhelming majority CFBB carries out desulfuration in furnace with agstone as desulfurizing agent, because agstone is in the reason such as residing time in furnace is short, in order to reach desirable desulfuration efficiency, generally need too much to add desulfurizing agent, calcium to sulphur mole ratio is generally more than 2.5, the utilization rate of lime stone is generally lower than 40%, if the granularity of agstone is less than normal, the too small agstone of granularity does not also fully participate in desulphurization reaction and just by flue gas, is carried out burner hearth after calcining in burner hearth, enter in deduster and be collected, be transported in grey storehouse, the utilization rate of lime stone is lower, desulfurization is large by lime stone consumption.
In order to realize desulfurization object, toward too much adding desulfurizing agent in burner hearth, there is following shortcoming: (1) desulfurizing agent cost increases; (2) lime stone minute heat of desorption in stove, reduces boiler efficiency; (3) lime stone handling system conveying capacity increases, and fault rate improves; (4) flying dust amount increases, and the load of deduster and ash-transmission system increases, fault rate increases, and causes the dust emission concentration of flue gas to exceed standard; (5) in flying dust, contain the lime burning stone flour that has neither part nor lot in a large number desulphurization reaction, be unfavorable for that flying dust is as the raw material of cement, be difficult to comprehensive utilization.
In order to solve the problems such as CFBB unburned carbon in flue dust is high, sorbent utilization is on the low side, flying dust recirculating technique is applied: deduster is trapped to the flying dust getting off and by conveying device, send back to burner hearth, in flying dust, unburnt carbon granules again burns in burner hearth, and the lime burning stone granulate that has neither part nor lot in desulphurization reaction participates in desulphurization reaction again.By adopting flying dust recirculating technique, the phosphorus content of boiler fly ash obviously reduces, the utilization rate of lime stone significantly improves.Have result of study to show, after Installation of Circulation Fluidized Bed Boiler flying dust EGR, the unburned carbon in flue dust of boiler is reduced to 20% from 37%, and the concentration of emission of sulfur dioxide is from 300mg/m
3more than be reduced to 100mg/m
3below; Use anthracitic CFBB and adopt after flying dust recirculating technique, unburned carbon in flue dust is reduced to 19% from 24%, and energy-saving benefit is remarkable; Large circulating fluidized bed boiler adopts flying dust recirculating technique can effectively improve utilization rate and the desulfuration efficiency of lime stone.
But existing CFBB flying dust recirculating technique exists following not enough:
(1) it is on the low side that circulating ash enters the temperature of burner hearth.The flying dust temperature that deduster is collected is generally below 150 ℃, and the circulating ash temperature of returning to burner hearth through fly ash re-injection system is lower, is unfavorable for returning the desulfurization with limestone particle that burns of carbon granule in the circulating ash of burner hearth.
(2) device having is provided with circulating ash intermediate storage storehouse, and storage silo takies certain space, and cost of investment increases; Circulating ash temperature after certain memory time further reduces, and returns to the desulfurization with limestone particle that burns of carbon granule after burner hearth not only bad for circulating ash, and the circulating ash in storage silo becomes mobile performance variation after cold ash, and the electric energy of strength delivery consumes increases; Owing to containing a large amount of CaO in circulating ash, the water imbibition of cooling rear CaO, cementability are strong especially, are very easy to occur the problems such as recirculation ash in storage silo hardens, Pneumatic conveying pipeline obstruction.
(3) the intermediate storage storehouse of circulating ash is set, then the circulating ash in storage silo is transported to burner hearth, belong to two-stage conveying.Except the first order, carry and need consumption of compressed air, carry the second level needs the high pressure positive blowers such as roots blower that conveying air is provided, and consumption of power increases.
Above-mentioned analysis shows, flying dust recirculating technique can improve boiler efficiency, improve the utilization rate of the lime stone of desulfuration in furnace system.But flying dust recirculating technique also exists that system complex, operation energy consumption are high at present, system fluctuation of service, boiler flyash carbon content is high and the problems such as lime stone utilization rate is low for desulfurization.
Summary of the invention
The object of the present invention is to provide a kind of compact conformation, operation energy consumption is low, security of operation is stable, can effectively reduce unburned carbon in flue dust and improve CFBB flying dust EGR and the flying ash recycling method of lime stone utilization rate for desulfuration in furnace.
For achieving the above object, the technical solution used in the present invention is:
A kind of CFBB flying dust EGR, boiler flue gas outlet is communicated with cyclone separator, cyclone separator gas vent is communicated with deduster through heat exchanger, cyclone separator solid outlet is communicated with the bulky grain high temperature ash import of material returning device, deduster gas vent is communicated with chimney, deduster solid outlet is communicated with the female pipe of defeated ash through storehouse pump, the female pipe outlet of defeated ash is divided into two-way, one Yu Hui storehouse, road is communicated with, another road is communicated with the circulating ash import of material returning device, and material returning device outlet is communicated with boiler furnace.
The female pipe outlet of described defeated ash is provided with the distributor of three-way pipe structure, distributor import is communicated with the female pipe outlet of defeated ash, after ash discharge switch valve is installed in distributor one outlet, be communicated with grey storehouse, after circulating ash switch valve is installed in another outlet of distributor, be communicated with the circulating ash import of material returning device.
On the female pipe of described defeated ash, be connected with to the female pipe of defeated ash and provide and carry the compressed-air actuated air accumulator of flying dust.
The outlet of described material returning device is by returning charge inclined tube and boiler furnace, air compartment, coal feeding hole, desulfurizing agent spout connection.
The inlet and outlet of described storehouse pump is respectively arranged with storehouse pump inlet valve and storehouse pump outlet valve.
A flying ash recycling method for flying dust EGR, comprises the following steps:
The female pipe outlet of described defeated ash is provided with the distributor of three-way pipe structure, distributor import is communicated with the female pipe outlet of defeated ash, after ash discharge switch valve is installed in distributor one outlet, be communicated with grey storehouse, after circulating ash switch valve is installed in another outlet of distributor, be communicated with the circulating ash import of material returning device; In step 3, by controlling the unlatching of ash discharge switch valve and circulating ash switch valve or closing, realize fly ash emission to grey storehouse and the ratio of returning to the amount of burner hearth.
In described step 3, when in unburned carbon in flue dust and flying dust, calcium oxide content is reduced to certain value, increase the opening times of ash discharge switch valve, the opening times of minimizing circulating ash switch valve, to reduce the flying dust amount of returning to burner hearth and the ratio that is discharged into the flying dust amount in grey storehouse, reduce flying dust recirculation multiplying power; When in unburned carbon in flue dust and flying dust, calcium oxide content rises to certain value, reduce the opening times of ash discharge switch valve, the opening times of increase circulating ash switch valve, increase the flying dust amount of returning to burner hearth and the ratio that is discharged into the flying dust amount in grey storehouse, increase flying dust recirculation multiplying power.
The female pipe of described defeated ash connects promising its provides conveying flying dust compressed-air actuated air accumulator.
It is that the bulky grain high temperature ash of 900 ℃ of left and right enters material returning device that cyclone separator of the present invention traps the temperature of getting off, 150 ℃ of following low-temperature circulating ashes that come from storehouse pump enter material returning device through circulating ash import, and mix with bulky grain high temperature ash before returning to burner hearth, because bulky grain high temperature ash flow is generally 30 to 50 times of ash flow of circulating, the two mixed mean temperature is up to more than 850 ℃, increased substantially the burning of unburnt carbon granule in burner hearth in circulating ash, after-flame performance, and the desulfurization performance of circulating ash sodalime stone, advantage of the present invention is apparently higher than traditional direct flying dust EGR of low-temperature circulating ash being delivered to burner hearth, effectively reduce unburned carbon in flue dust and improve desulfuration in furnace lime stone utilization rate, by material returning device blended coal ash, compact conformation, the CFBB flying dust EGR that security of operation is stable.
Further, distributor and supporting ash discharge switch valve and circulating ash switch valve are set on the female pipe of defeated ash of the present invention by the flying dust EGR of CFBB, can effectively control by deduster and trap the ash amount and the ratio that is discharged into the ash amount in grey storehouse that the flying dust getting off returns to burner hearth, the control of lime stone utilization rate is used in realization to unburned carbon in flue dust and desulfuration in furnace.
The present invention also tool has the following advantages: the present invention adopts one-level to carry, recirculation ash is directly transported to material returning device, burner hearth from storehouse pump, save the intermediate storage storehouse of the circulating ash that in prior art, flying dust EGR generally adopts, saved occupation of land space and the initial cost cost of storage silo, simple in structure.What flow in ash conveying pipe of the present invention is heat ash (temperature is higher than 100 ℃), and heat ash is carried and do not had sucting wet problem, has also solved the blockage problem that cold ash is carried harden in storage silo after the flying dust moisture absorption existing problem and conveyance conduit.
The present invention is that sealing is carried, and has also solved because storage silo top arranges the dust polluting environment problem causing with atmosphere UNICOM opening.
The present invention adopts one-level to carry, and adopts integrated setting with pneumatic ash removal system, saves the conveying fan that in prior art, flying dust EGR generally adopts, and has further saved the electric energy that conveying fan operation must consume, and reduces energy consumption.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention.
In figure: 1-ash releasing tube, 2-ash discharge switch valve, 3-distributor, the female pipe of the defeated ash of 4-, 5-air accumulator, 6-circulating ash switch valve, 7-material returning device, 8-returning charge inclined tube, 9-burner hearth, 10-air compartment, 11-coal feeding hole, 12-desulfurizing agent spout, the import of 13-circulating ash, 14-flue, 15-cyclone separator, 16-standpipe, 17-heat exchanger, 18-heating surface, 19-deduster, 20-chimney, 21-storehouse pump inlet valve, Beng，23-storehouse, 22-storehouse pump outlet valve, 24-circulation ash pipe, 25-ash storehouse
The specific embodiment
Below in conjunction with the drawings and specific embodiments, the present invention is described in further detail.
Referring to Fig. 1, the present invention includes burner hearth 9, cyclone separator 15, material returning device 7, deduster 19, storehouse pump 22, the female pipe 4 of defeated ash, distributor 3, ash releasing tube 1, circulation ash pipe 24, returning charge inclined tube 8, flue 14 etc.
The flying dust EGR of CFBB, the top exhanst gas outlet of described burner hearth 9 is connected with cyclone separator 15 by flue 14, cyclone separator 15 solid outlets are connected with material returning device 7 bulky grain high temperature ash imports, and material returning device 7 outlets are connected with returning charge inclined tube 8 and burner hearth 9; Cyclone separator 15 gas vents are also connected with heat exchanger 17 by flue 14, the inlet end of deduster 19 is connected with heat exchanger 17, outlet side is connected with chimney 20 by flue 14, and the bottom solid outlet of deduster 19 is connected with storehouse pump 22, is further connected with the female pipe 4 of defeated ash of storehouse pump 22 bottoms.The female pipe 4 of defeated ash is connected with air accumulator 5, distributor 3, and distributor 3 arranges two outlets: an outlet is connected with grey storehouse 25 by ash releasing tube 1, and another outlet is connected with the circulating ash import 13 of material returning device 7 by circulation ash pipe 24.The import and export of described storehouse pump 22 arrange respectively storehouse pump inlet valve 21 and storehouse pump outlet valve 23.On described ash releasing tube 1, ash discharge switch valve 2 is set, circulating ash switch valve 6 is set on circulation ash pipe 24.On described heat exchanger 17, heating surface 18 is set.The bottom of described burner hearth 9 is connected with returning charge inclined tube 8, air compartment 10, coal feeding hole 11, desulfurizing agent spout 12.
First 150 ℃ of following low-temperature circulating ashes enter material returning device before returning to burner hearth mixes and carries out preheating with high temperature bulky grain high temperature ash, after temperature increase to 850 ℃ is above, through returning charge inclined tube, enter burner hearth again, improve the reactivity of the interior carbon granule of circulating ash and desulfurizing agent, burn-off rate, desulfurizing agent that the carbon granule of raising circulating ash returns after burner hearth return to the desulfuration efficiency after burner hearth, final realization reduced unburned carbon in flue dust, raising boiler efficiency, improve the object of the utilization rate of lime stone and raising desulfuration efficiency for desulfurization, improve the economy of boiler operatiopn.
The flying dust round-robin method of a kind of flying dust EGR of the present invention, its job step is as follows:
When in unburned carbon in flue dust and flying dust, calcium oxide content is reduced to certain value, increase the opening times of ash discharge switch valve 2, the opening times of reduction circulating ash switch valve 6, reduce and return to the ash amount of burner hearth and be discharged into the ratio that flies storehouse ash amount, reduce flying dust recirculation multiplying power;
When in unburned carbon in flue dust and flying dust, calcium oxide content rises to certain value, reduce the opening times of ash discharge switch valve 2, the opening times of increase circulating ash switch valve 6, increase and return to the ash amount of burner hearth and be discharged into the ratio that flies storehouse ash amount, increase flying dust recirculation multiplying power.
Technique effect of the present invention has:
1, before turning back to burner hearth, circulating ash first enters into material returning device, circulating ash temperature is brought up to more than 800 ℃ below from 150 ℃, improved the desulfurization performance that carbon granule in circulating ash returns to lime stone in after-flame performance after burner hearth and circulating ash, effectively reduce unburned carbon in flue dust, improve boiler efficiency, effectively improve utilization rate and the desulfuration efficiency of lime stone, improve the economy of boiler operatiopn.
2, unburned carbon in flue dust reduces, and after the utilization rate of lime stone improves, the calcium oxide content of flying dust reduces, has significantly improved the performance of flying dust as cement additire, improves and usings boiler fly ash as the performance of the cement of raw material, and flying dust can be realized comprehensive utilization.
3, pneumatic ash handling and flying dust recirculation integrated setting, no longer arrange intermediate storage storehouse, system compact, the occupation of land of saving intermediate storage storehouse.Because flying dust EGR adopts sealed conveying, also solved because top, intermediate storage storehouse arranges the dust polluting environment problem causing with atmosphere UNICOM opening.
4, pneumatic ash handling and flying dust recirculation integrated setting, intermediate storage storehouse is no longer set, fly ash re-injection system is that heat ash is carried (temperature is generally higher than 100 ℃), efficiently solves flying dust that traditional fly ash re-injection system with intermediate storage storehouse adopts the moisture absorption of cold grey induction system flying dust to cause harden problem and conveyance conduit blockage problem.
5, pneumatic ash handling and flying dust recirculation integrated setting, no longer arrange conveying fan, except saving initial cost, can also save the electric energy that conveying fan consumes.
6, pneumatic ash handling and flying dust recirculation integrated setting, by regulating the opening and closing state of ash discharge switch valve and circulating ash switch valve, the circulating ratio that just can facilitate, adjust reliably flying dust recirculation, effectively guarantees that phosphorus content and the calcium oxide content in flying dust remains on lower level.
The coal-burning boiler of 1, one 600MW of embodiment, installs flying dust EGR and compares with flying dust EGR is not installed, and the expense of the annual fuel cost of saving and lime stone is in Table 1, and the conveying fan power consumption that existing two-stage conveying system is installed is calculated in Table 2.By table 1 and table 2, can be found out, with flying dust EGR be not installed compared, installation flying dust EGR is per hour can save 7.16 tons, lime stone, carbon amount with fly ash emission reduces 1.604 tons, minimizing lime stone per hour take and fuel cost amounts to 3035 yuan, reduce every year 1973 ten thousand yuan, owing to adopting one-level to carry, one of the conveying fan that minimizing power is 129.8KW, reduces 42.2 ten thousand yuan of the electricity charge every year.
In addition, because the present invention no longer arranges intermediate storage storehouse, installation cost, capital cost significantly reduce, and because the complexity of device systems significantly reduces, fault rate reduces, operation, the maintenance cost of equipment significantly reduce.
Table 1 fuel saving and lime stone calculate
| Sequence number | | Unit amount | |
| 1 | Unit load | MW600.00 | |
| 2 | The thermal efficiency | %45.00 | |
| 3 | Input heat | MW1333.33 | |
| 4 | The low heat valve of coal | MJ/kg22.00 | |
| 5 | The consumption of coal | t/h218.18 | |
| 6 | Ash content | %15.00 | |
| 7 | Sulphur content | %1.50 | |
| 8 | Flying dust EGR calcium sulfur ratio is not installed | -2.50 | |
| 9 | Flying dust EGR calcium sulfur ratio is installed | -1.80 | |
| 10 | Flying dust EGR lime stone consumption is not installed | t/h25.57 |
| 11 | Flying dust EGR lime stone amount is installed | t/h | 18.41 |
| 12 | Save lime stone amount | t/h | 7.16 |
| 13 | Flying dust share | % | 70 |
| 14 | Flying dust EGR unburned carbon in flue dust is not installed | % | 12 |
| 15 | Flying dust EGR unburned carbon in flue dust is installed | % | 5 |
| 16 | Flying dust EGR carry-over loss carbon amount is not installed | t/h | 2.749 |
| 17 | Femto-ampere dress flying dust EGR carry-over loss carbon amount | t/h | 1.145 |
| 18 | The carbon amount reducing | t/h | 1.604 |
| 19 | Lime stone price | Yuan/ton | 200 |
| 20 | The price of carbon | Yuan/ton | 1000 |
| 21 | Minimizing lime stone expense per hour | Unit/h | 1432 |
| 22 | The fuel cost of minimizing per hour | Unit/h | 1604 |
| 23 | The lime stone of saving per hour and fuel cost | Unit/h | 3035 |
| 24 | Annual running time | H/ | 6500 |
| 25 | Annual lime stone and the fuel cost saved | Ten thousand yuan/year | 1973 |
The power consumption of the existing two-stage conveying system of table 2 conveying fan is calculated
| Sequence number | Title | Unit | |
| 1 | Flying dust recirculation multiplying power | - | 4.0 |
| 2 | Recirculation ash amount per hour | t/h | 91.6 |
| 3 | Ash gas ratio | - | 35.0 |
| 4 | Air consumption per hour | t/h | 2.6 |
| 5 | Conveying fan pressure | kPa | 150.0 |
| 6 | Conveying fan efficiency | % | 65.0 |
| 7 | Conveying fan power consumption | kW | 129.8 |
| 8 | Rate for incorporation into the power network | Unit/kWh | 0.5 |
| 9 | Annual running time | H/ | 6500.0 |
| 10 | The annual saving electricity charge | Ten thousand yuan/year | 42.2 |
Claims (9)
1. a CFBB flying dust EGR, it is characterized in that: boiler flue gas outlet is communicated with cyclone separator (15), cyclone separator (15) gas vent is communicated with deduster (19) through heat exchanger (17), cyclone separator (15) solid outlet is communicated with the bulky grain high temperature ash import of material returning device (7), deduster (19) gas vent is communicated with chimney (20), deduster (19) solid outlet is communicated with the defeated female pipe of ash (4) through storehouse pump (22), the defeated female pipe of ash (4) outlet is divided into two-way, one Yu Hui storehouse, road (25) is communicated with, another road is communicated with the circulating ash import (13) of material returning device (7), material returning device (7) outlet is communicated with boiler furnace (9).
2. CFBB flying dust EGR according to claim 1, it is characterized in that: the described defeated female pipe of ash (4) outlet is provided with the distributor (3) of three-way pipe structure, distributor (3) import is communicated with the defeated female pipe of ash (4) outlet, after ash discharge switch valve (2) is installed in distributor (3) one outlets, be communicated with grey storehouse (25), after circulating ash switch valve (6) is installed in another outlet of distributor (3), be communicated with the circulating ash import (13) of material returning device (7).
3. CFBB flying dust EGR according to claim 1 and 2, is characterized in that: on the described defeated female pipe of ash (4), be connected with to the female pipe of defeated ash and provide and carry compressed-air actuated air accumulator (5) for flying dust.
4. CFBB flying dust EGR according to claim 1 and 2, is characterized in that: described material returning device (7) outlet is communicated with boiler furnace (9), air compartment (10), coal feeding hole (11), desulfurizing agent spout (12) by returning charge inclined tube (8).
5. CFBB flying dust EGR according to claim 1 and 2, is characterized in that: the inlet and outlet of described storehouse pump (22) is respectively arranged with storehouse pump inlet valve (21) and storehouse pump outlet valve (23).
6. the flying ash recycling method based on claim 1 flying dust EGR, is characterized in that comprising the following steps:
Step 1, the flue gas that in boiler, coal burning generates carries unburnt residue and leaves burner hearth (9), through flue (14), enters into cyclone separator (15), and high temperature bulky grain high temperature ash is sent in material returning device (7) after being trapped by cyclone separator (15);
Step 2, flue gas carry flying dust leave cyclone separator (15) through heat exchanger (17) heat exchange, cooling after enter in deduster (19), flying dust is trapped by deduster (19), clean flue gas is discharged in atmosphere through chimney (20), and the flying dust that deduster (19) traps is sent in the defeated female pipe of ash (4) through storehouse pump (22);
Step 3, a flying dust part that enters the female pipe of defeated ash (4) is discharged into grey storehouse (25), and another part is sent in material returning device (7) with after cyclone separator traps the high temperature bulky grain high temperature ash getting off and mixes, and through returning charge inclined tube (8), returns to burner hearth (9).
7. flying ash recycling method according to claim 6, it is characterized in that: the described defeated female pipe of ash (4) outlet is provided with the distributor (3) of three-way pipe structure, distributor (3) import is communicated with the defeated female pipe of ash (4) outlet, after ash discharge switch valve (2) is installed in distributor (3) one outlets, be communicated with grey storehouse (25), after circulating ash switch valve (6) is installed in another outlet of distributor (3), be communicated with the circulating ash import (13) of material returning device (7); In step 3, by controlling the unlatching of ash discharge switch valve (2) and circulating ash switch valve (6) or closing, realize fly ash emission to grey storehouse (25) and return to the ratio that burner hearth (9) is measured.
8. flying ash recycling method according to claim 7, it is characterized in that: when in described step 3, in unburned carbon in flue dust and flying dust, calcium oxide content is reduced to certain value, increase the opening times of ash discharge switch valve (2), the opening times of minimizing circulating ash switch valve (6), to reduce the flying dust amount of returning to burner hearth and the ratio that is discharged into the flying dust amount in grey storehouse, reduce flying dust recirculation multiplying power; When in unburned carbon in flue dust and flying dust, calcium oxide content rises to certain value, reduce the opening times of ash discharge switch valve (2), the opening times of increase circulating ash switch valve (6), increase the flying dust amount of returning to burner hearth and the ratio that is discharged into the flying dust amount in grey storehouse, increase flying dust recirculation multiplying power.
9. according to the flying ash recycling method described in claim 6-8 any one, it is characterized in that: the female pipe of described defeated ash (4) connects promising its to be provided and carry compressed-air actuated air accumulator (5) for flying dust.
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| CN105485706A (en) * | 2015-11-20 | 2016-04-13 | 张建存 | Boiler smoke cyclone separation recycling device and smoke recycling method thereof |
| CN105823059A (en) * | 2016-06-18 | 2016-08-03 | 集美大学 | Fluidized bed waste incineration treatment system |
| CN105823039A (en) * | 2016-04-21 | 2016-08-03 | 山东科院天力节能工程有限公司 | Dry distillation system combined with combustion of circulating fluidized bed and pyrolysis of rotary kiln |
| CN105972586A (en) * | 2016-07-26 | 2016-09-28 | 四川普什醋酸纤维素有限责任公司 | Circulating fluidized bed boiler fly ash forced circulation system and process |
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| CN113462434A (en) * | 2021-07-06 | 2021-10-01 | 中国科学院工程热物理研究所 | Gasification method and system with fly ash regasification function |
| CN113757640A (en) * | 2021-10-09 | 2021-12-07 | 焦作市华康糖醇科技有限公司 | Biomass chain boiler soot recycling system |
| CN114110648A (en) * | 2021-12-29 | 2022-03-01 | 成都海泰科欣远节能科技有限公司 | Boiler control device and method |
| CN114234178A (en) * | 2021-11-02 | 2022-03-25 | 平湖弘欣热电有限公司 | Fly ash recirculation system of fluidized bed boiler |
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| CN105485706A (en) * | 2015-11-20 | 2016-04-13 | 张建存 | Boiler smoke cyclone separation recycling device and smoke recycling method thereof |
| CN105823039A (en) * | 2016-04-21 | 2016-08-03 | 山东科院天力节能工程有限公司 | Dry distillation system combined with combustion of circulating fluidized bed and pyrolysis of rotary kiln |
| CN105823039B (en) * | 2016-04-21 | 2018-11-09 | 山东科院天力节能工程有限公司 | A kind of distillation system that circulating fluidized bed combustion is combined with rotary kiln pyrogenation |
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| CN109328119A (en) * | 2016-07-22 | 2019-02-12 | 株式会社Ryux | Heating and firing device and firing method for fly ash |
| CN109328119B (en) * | 2016-07-22 | 2021-08-24 | 株式会社Ryux | Heating and firing device and firing method for fly ash |
| CN105972586A (en) * | 2016-07-26 | 2016-09-28 | 四川普什醋酸纤维素有限责任公司 | Circulating fluidized bed boiler fly ash forced circulation system and process |
| CN108361687A (en) * | 2018-04-11 | 2018-08-03 | 山西沁新能源集团股份有限公司 | A kind of boiler dusting ash extracorporal circulatory system guarantee flue gas ultra-clean exhaust system |
| CN109336149A (en) * | 2018-12-17 | 2019-02-15 | 河南科达东大国际工程有限公司 | A kind of Aluminium hydroxide roasting furnace system |
| CN109701323A (en) * | 2019-01-16 | 2019-05-03 | 南京航空航天大学 | Axial flow combined dust removal system and method for high temperature and high dust-containing flue gas |
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| CN111486448A (en) * | 2020-04-01 | 2020-08-04 | 南京航空航天大学 | A fluidized bed boiler fly ash recycling device with axial flow cyclone separation |
| CN111878801A (en) * | 2020-08-31 | 2020-11-03 | 北京永博洁净科技有限公司 | Fly ash circulating device and circulating fluidized bed boiler comprising same |
| CN112325282A (en) * | 2020-10-29 | 2021-02-05 | 中国石油化工集团有限公司 | Circulating fluidized bed flue gas and fly ash combined circulating system and control method |
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| CN113462434A (en) * | 2021-07-06 | 2021-10-01 | 中国科学院工程热物理研究所 | Gasification method and system with fly ash regasification function |
| CN113462434B (en) * | 2021-07-06 | 2022-08-02 | 中国科学院工程热物理研究所 | A gasification method and system with fly ash regasification |
| CN113757640A (en) * | 2021-10-09 | 2021-12-07 | 焦作市华康糖醇科技有限公司 | Biomass chain boiler soot recycling system |
| CN114234178A (en) * | 2021-11-02 | 2022-03-25 | 平湖弘欣热电有限公司 | Fly ash recirculation system of fluidized bed boiler |
| CN114234178B (en) * | 2021-11-02 | 2022-07-12 | 平湖弘欣热电有限公司 | Fly ash recirculation system of fluidized bed boiler |
| CN114110648A (en) * | 2021-12-29 | 2022-03-01 | 成都海泰科欣远节能科技有限公司 | Boiler control device and method |
| CN114738737A (en) * | 2022-05-07 | 2022-07-12 | 润电能源科学技术有限公司 | A combustion system with flue gas fly ash circulation function |
| CN115681958A (en) * | 2022-10-21 | 2023-02-03 | 中国石油化工集团有限公司 | Fly ash screening device and method for a circulating fluidized bed boiler |
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