CN102755822A - Flue gas circulating fluid bed system capable of simultaneously desulfurizing and denitriding - Google Patents
Flue gas circulating fluid bed system capable of simultaneously desulfurizing and denitriding Download PDFInfo
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- CN102755822A CN102755822A CN2012102661118A CN201210266111A CN102755822A CN 102755822 A CN102755822 A CN 102755822A CN 2012102661118 A CN2012102661118 A CN 2012102661118A CN 201210266111 A CN201210266111 A CN 201210266111A CN 102755822 A CN102755822 A CN 102755822A
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- flue gas
- cfbb
- sulfide
- fluidized bed
- circulating fluidized
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 53
- 239000003546 flue gas Substances 0.000 title claims abstract description 53
- 239000012530 fluid Substances 0.000 title abstract description 9
- 230000003009 desulfurizing effect Effects 0.000 title abstract description 5
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims abstract description 17
- 150000004767 nitrides Chemical class 0.000 claims abstract description 17
- 239000000428 dust Substances 0.000 claims abstract description 10
- 238000005070 sampling Methods 0.000 claims abstract description 9
- 238000001035 drying Methods 0.000 claims abstract description 7
- 238000006477 desulfuration reaction Methods 0.000 claims description 36
- 230000023556 desulfurization Effects 0.000 claims description 31
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 28
- 229910052757 nitrogen Inorganic materials 0.000 claims description 14
- 239000000463 material Substances 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 10
- 238000012360 testing method Methods 0.000 claims description 8
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 7
- 239000000920 calcium hydroxide Substances 0.000 claims description 7
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 7
- 239000010881 fly ash Substances 0.000 claims description 6
- 239000002250 absorbent Substances 0.000 claims description 4
- 230000002745 absorbent Effects 0.000 claims description 4
- 239000011575 calcium Substances 0.000 claims description 4
- 208000012839 conversion disease Diseases 0.000 claims description 3
- 238000009834 vaporization Methods 0.000 claims description 3
- 230000008016 vaporization Effects 0.000 claims description 3
- 239000000126 substance Substances 0.000 abstract description 4
- 230000007246 mechanism Effects 0.000 abstract description 3
- 238000003795 desorption Methods 0.000 abstract 2
- 239000006096 absorbing agent Substances 0.000 abstract 1
- 230000004913 activation Effects 0.000 abstract 1
- 239000010883 coal ash Substances 0.000 abstract 1
- 238000001514 detection method Methods 0.000 abstract 1
- 238000001179 sorption measurement Methods 0.000 abstract 1
- 238000005507 spraying Methods 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 12
- 238000000034 method Methods 0.000 description 8
- 239000002956 ash Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 239000002245 particle Substances 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 4
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000011449 brick Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 230000003134 recirculating effect Effects 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000006698 induction Effects 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000010079 rubber tapping Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- AKHNMLFCWUSKQB-UHFFFAOYSA-L sodium thiosulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=S AKHNMLFCWUSKQB-UHFFFAOYSA-L 0.000 description 1
- 235000019345 sodium thiosulphate Nutrition 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
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Classifications
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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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Treating Waste Gases (AREA)
Abstract
The invention provides a flue gas circulating fluid bed system capable of simultaneously desulfurizing and denitriding, comprising a circulating fluid bed boiler, a dust removing plant, a drying tower, a sulfide and nitride detector and a control device, wherein the circulating fluid bed boiler adopts a manner of ignition under a bed, and flue gas generated by the circulating fluid bed boiler is discharged from a top chimney flue; the dust removing plant is communicated with the top chimney flue of the circulating fluid bed boiler, and dust removing operation is carried out on the flue gas; the drying tower is connected with the dust removing plant and is provided with a flue gas sampling port; the sulfide and nitride detector carries out sampling at the flue gas sampling port so as to detect the content of sulfide and nitride; and the control device controls a denitriding device at the front end of the circulating fluid bed boiler according to the detection result of the sulfide and nitride detector. The system adopts the mechanism of desorption SO2 and NOX with high activated adsorption prepared by using coal ash as a fundamental substance, and solves the desorption efficiency of absorbing agents with high activation through a manner of pharmaceutical spraying.
Description
Technical field
The present invention relates to a kind of flue gas circulating fluidized bed while desulfurization removing nitric system.
Background technology
Flue gas circulating fluidized bed technology is a kind of newer dry desulfurizing process; Because characteristics such as it has that system is simple, removal efficiency is higher, water saving, secondary pollution discharging are less, equipment investment and operating cost are lower; Be considered to a kind of very promising flue gas desulfurization technique at present, and obtained industrial applications: the flue gas desulfurization technique of German LURGI company exploitation, the GSA flue gas desulfurization technique of German WU LFF company improved RCFB desulfur technology, the exploitation of Denmark F.L.SMITH company on the LURGI technical foundation, the NID sulfur removal technology of ABB AB's exploitation.But above-mentioned technology does not possess denitrification functions.
For nitrogen oxide control, general maturation process is to install a cover nitrogen rejection facility at the back additional at desulfurizer, like SCR or SNCR, thereby realizes the combined desulfurization denitrogenation, and this is the classification administration way.This mode not only floor space is big, and investment and operating cost height, is difficult to extensive use.In order to reduce the gas cleaning expense, exploitation is the desulfurization removing nitric new technology simultaneously, and new equipment has become the research direction that has frontier nature in the Air Pollution Control field.Existing more correlative study both at home and abroad, but the shortcoming of existence technology mostly and economic aspect is difficult to develop into comparatively practical technology.Therefore how the cost-effective desulfurization removing nitric technology of improving is the technical barrier that the market demand is created.
Summary of the invention
To the demand of industry, the present invention proposes a kind of flue gas circulating fluidized bed while desulfurization removing nitric system, comprising:
CFBB, said CFBB adopts the ignition under bed mode, and the flue discharge from the top of the flue gas of said CFBB generation;
Cleaner is communicated with the top flue of said CFBB, and said flue gas is carried out dust removal operation;
Drying tower is connected with said cleaner and has the flue gas sampling mouth;
Sulfide and nitride detector are sampled to detect sulfide and amount of nitrides from said flue gas sampling mouth; And
Control device is controlled the nitrogen rejection facility of said CFBB front end according to the testing result of said sulfide and nitride detector.
According to a preferred embodiment, in above-mentioned flue gas circulating fluidized bed while desulfurization removing nitric system, further comprise: material library, said CFBB receives material from said material library; Wherein, said nitrogen rejection facility is arranged between said material library and the said CFBB.
According to a preferred embodiment, in above-mentioned flue gas circulating fluidized bed while desulfurization removing nitric system, be provided with the highly active absorbent that is the basis with flyash and Ca (OH) in the said nitrogen rejection facility.
According to a preferred embodiment; In above-mentioned flue gas circulating fluidized bed while desulfurization removing nitric system; Further comprise: desulfurizer is arranged at the outlet expander section of the Venturi tube in the said CFBB, wherein; Said desulfurizer is connected with said control device signal, and said control device is controlled said desulfurizer according to the testing result of said sulfide and nitride detector.
According to a preferred embodiment; In above-mentioned flue gas circulating fluidized bed while desulfurization removing nitric system; Said desulfurizer is a pipeline water injector; The water of wherein said pipeline water injector ejection contacts back vaporization fast with said flue gas, to create the chemical reaction temperature condition of 20～30 ° of C more than the dew point, so that the reaction conversion of sulfur dioxide and calcium hydroxide is moment to accomplish the reaction of ionic type.
According to a preferred embodiment, in above-mentioned flue gas circulating fluidized bed while desulfurization removing nitric system, under the control of said control device, said desulfurizer and nitrogen rejection facility are worked simultaneously.
According to a preferred embodiment, in above-mentioned flue gas circulating fluidized bed while desulfurization removing nitric system, said control system is a Programmable Logic Controller.
It is the high activity absorbing and removing SO of basic substance preparation with flyash that the present invention has utilized
2With the mechanism of NOX,, solve high activity and receive the agent removal efficiency through the mode that preparation sprays.Experiment shows; Technology of the present invention is under dry method duct injection flue gas desulfuration and denitrification situation; Have desulfuration efficiency and about 40% nitric efficiency about 84%, under best operating condition of test condition, possess desulfurization removing nitric efficient and be respectively: 92.3%, 60.8% simultaneously.
Should be appreciated that the above generality of the present invention is described and following detailed description all is exemplary and illustrative, and be intended to further explanation is provided for as claimed in claim the present invention.
Description of drawings
Accompanying drawing mainly is to be used to provide the present invention is further understood.Accompanying drawing shows embodiments of the invention, and plays the effect of explaining the principle of the invention with this specification.In the accompanying drawing:
Fig. 1 schematically shows the structure chart of flue gas circulating fluidized bed while of the present invention desulfurization removing nitric system.
The specific embodiment
Describe technical scheme of the present invention in detail below in conjunction with accompanying drawing.
Fig. 1 schematically shows the structure chart of flue gas circulating fluidized bed while of the present invention desulfurization removing nitric system.As shown in the figure, flue gas circulating fluidized bed while of the present invention, the desulfurization removing nitric system 100 mainly comprised: CFBB 101, cleaner 102, drying tower 103, sulfide and nitride detector 104, control device 105 and nitrogen rejection facility 106.
Flue gas flue discharge that CFBB 101 adopts ignition under bed mode and this CFBB 101 to produce from the top.For example, this CFBB 101 can adopt ignition under bed (oil or coal gas), fractional combustion; One time the wind ratio accounts for 50-60%; The flying dust circulation is low range, and middle temperature is separated the lime-ash discharging and adopted dry type, is discharged by water-cooling spiral tapping machine, ash cooler and dust collector ash hopper respectively.Burner hearth is the key that guarantees full combustion of fuel; Adopt turbulent bed; Make fluidizing velocity at 3.5-4.5m/s, and design suitable section of burner hearth, on burner hearth membrane wall pipe, lay thin liner (high alumina matter brick); When even different fuel is used in boiler combustion, efficiency of combustion also can remain on more than 98-99%.
The high-temperature separator inlet flue gas temperature is about 800 ℃, and whirlwind tube internal diameter is less, and designs simplification only needs the very thin abrasionproof liner of one deck (nitrogenize silica brick) in the tube.Its service life is longer.Circulating ratio is about 10-20.The circulating ash induction system is mainly by feed back pipe, loop back device, and several parts such as overflow pipe and ash cooler are formed.The adjustment process of bed temperature control system is automatic.In whole load variations scope, remain a certain steady state value between 850-950 ℃ of concentrated phase bed bed temperature, this value is best desulfurization temperature.When automatic control did not drop into, armrest is moving also can keep constant bed temperature.
Then, cleaner 102 receives flue gas from the top flue of said CFBB 101, and said flue gas is carried out dust removal operation.Flue gas through dust removal operation will be transported to drying tower 103.Drying tower 103 has flue gas sampling mouth 107, and sulfide and nitride detector 104 can be sampled to detect sulfide and amount of nitrides from said flue gas sampling mouth 107.At last, control device 105, a Programmable Logic Controller for example will be controlled the nitrogen rejection facility 106 of said CFBB front end according to the testing result of said sulfide and nitride detector 104.
In addition, preferably as shown in Figure 1, above-mentioned flue gas circulating fluidized bed while, the desulfurization removing nitric system 100 may further include material library 108.Wherein, said CFBB 101 receives material from said material library 108, and said nitrogen rejection facility 106 is arranged between said material library 108 and the said CFBB 101.
According to a preferred embodiment of the present invention, be provided with the highly active absorbent that is the basis with flyash and Ca (OH) in the nitrogen rejection facility 106 of the present invention, to replace the denitrifier of traditional sodium thiosulfate.
On the other hand; Above-mentioned flue gas circulating fluidized bed while, the desulfurization removing nitric system 100 can also comprise: desulfurizer (not shown); This desulfurizer is arranged at the outlet expander section of the Venturi tube in the said CFBB 101; Wherein said desulfurizer is connected with said control device 105 signals, and said control device 105 is controlled said desulfurizer according to the testing result of said sulfide and nitride detector 104.
Preferably, said desulfurizer is a pipeline water injector, and the temperature of wherein coming out from boiler air preheater is the flue gas about 120～180 ℃, gets in the recirculating fluidized bed absorption tower through Venturi tube from the bottom.Establish a cover water injector in Venturi tube outlet expander section, created good desulfurization reaction temperature.The main chemical reactions principle of circulating fluid bed flue-gas desulfurizing technology is following:
Because the course of reaction of particle in recirculating fluidized bed of SO2 and calcium hydroxide; It is the chemical reaction process of an external diffusion control; Through landing speed big between gas-solid; Mass transfer, rate of heat transfer and the gas-solid strengthened between gas-solid mix, thereby have satisfied the conditional request of sulfur dioxide and calcium hydroxide highly effective reaction.Particle huge surface area, fierce turbulence in the fluid bed on absorption tower; For the quick vaporization of water filling and the cooling of fast controllable provide basic assurance; Thereby created good chemical reaction temperature condition (above 20～30 ° of C of dew point), the reaction conversion that makes sulfur dioxide and calcium hydroxide is moment to accomplish the reaction of ionic type.Fierce turbulence through particle causes constantly collision between the particle, and the surface of desulfurizing agent calcium hydroxide particle is constantly upgraded, and the continuous recirculation use of desulphurization ash, thereby has improved the utilization rate of calcium hydroxide greatly.
Particularly, characteristics of the present invention are that said desulfurizer and nitrogen rejection facility are worked simultaneously under the control of said control device.
It is the high activity absorbing and removing SO of basic substance preparation with flyash that the present invention has utilized
2With the mechanism of NOX,, solve high activity and receive the agent removal efficiency through the mode that preparation sprays.Experiment shows; Technology of the present invention is under dry method duct injection flue gas desulfuration and denitrification situation; Have desulfuration efficiency and about 40% nitric efficiency about 84%, under best operating condition of test condition, possess desulfurization removing nitric efficient and be respectively: 92.3%, 60.8% simultaneously.
To sum up, characteristics of the present invention are at least: having prepared with flyash, Ca (OH) is the novel high-activity absorbent of basic substance; Adopt fixed bed mode and pipeline water spray mode, realize flue gas desulfuration and denitrification.
The foregoing description provides to those of ordinary skills and realizes or use of the present invention; Those of ordinary skills can be under the situation that does not break away from invention thought of the present invention; The foregoing description is made various modifications or variation; Thereby protection scope of the present invention do not limit by the foregoing description, and should be the maximum magnitude that meets the inventive features that claims mention.
Claims (7)
- One kind flue gas circulating fluidized bed while the desulfurization removing nitric system, comprising:CFBB, said CFBB adopts the ignition under bed mode, and the flue discharge from the top of the flue gas of said CFBB generation;Cleaner is communicated with the top flue of said CFBB, and said flue gas is carried out dust removal operation;Drying tower is connected with said cleaner and has the flue gas sampling mouth;Sulfide and nitride detector are sampled to detect sulfide and amount of nitrides from said flue gas sampling mouth; AndControl device is controlled the nitrogen rejection facility of said CFBB front end according to the testing result of said sulfide and nitride detector.
- 2. flue gas circulating fluidized bed while as claimed in claim 1 the desulfurization removing nitric system, it is characterized in that, further comprise:Material library, said CFBB receives material from said material library;Wherein, said nitrogen rejection facility is arranged between said material library and the said CFBB.
- 3. flue gas circulating fluidized bed while as claimed in claim 2 the desulfurization removing nitric system, it is characterized in that, be provided with the highly active absorbent that is the basis with flyash and Ca (OH) in the said nitrogen rejection facility.
- 4. flue gas circulating fluidized bed while as claimed in claim 1 the desulfurization removing nitric system, it is characterized in that, further comprise:Desulfurizer is arranged at the outlet expander section of the Venturi tube in the said CFBB,Wherein, said desulfurizer is connected with said control device signal, and said control device is controlled said desulfurizer according to the testing result of said sulfide and nitride detector.
- 5. flue gas circulating fluidized bed while as claimed in claim 4 the desulfurization removing nitric system; It is characterized in that; Said desulfurizer is a pipeline water injector; The water of wherein said pipeline water injector ejection contacts back vaporization fast with said flue gas, to create the chemical reaction temperature condition of 20～30 ° of C more than the dew point, so that the reaction conversion of sulfur dioxide and calcium hydroxide is moment to accomplish the reaction of ionic type.
- 6. flue gas circulating fluidized bed while as claimed in claim 5 the desulfurization removing nitric system, it is characterized in that under the control of said control device, said desulfurizer and nitrogen rejection facility are worked simultaneously.
- 7. flue gas circulating fluidized bed while as claimed in claim 1 the desulfurization removing nitric system, it is characterized in that said control system is a Programmable Logic Controller.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012102661118A CN102755822A (en) | 2012-07-30 | 2012-07-30 | Flue gas circulating fluid bed system capable of simultaneously desulfurizing and denitriding |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012102661118A CN102755822A (en) | 2012-07-30 | 2012-07-30 | Flue gas circulating fluid bed system capable of simultaneously desulfurizing and denitriding |
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| CN102755822A true CN102755822A (en) | 2012-10-31 |
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| CN2012102661118A Pending CN102755822A (en) | 2012-07-30 | 2012-07-30 | Flue gas circulating fluid bed system capable of simultaneously desulfurizing and denitriding |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1996038218A1 (en) * | 1995-05-30 | 1996-12-05 | Thermal Energy International Inc. | Flue gas scrubbing and waste heat recovery system |
| CN1539546A (en) * | 2003-11-02 | 2004-10-27 | 华北电力大学 | A flue gas desulfurization and denitrification purification method and device |
| CN101332400A (en) * | 2008-07-18 | 2008-12-31 | 朱学智 | Applying PLC Control System to Carry Out Calcium Spraying Desulfurization Method in Circulating Fluidized Bed Boiler |
| CN101648099A (en) * | 2009-08-26 | 2010-02-17 | 福建龙净脱硫脱硝工程有限公司 | Purifying treatment device and purifying treatment method for flue gas multicomponent pollutant generated by incinerating refuse |
| CN101732941A (en) * | 2009-12-29 | 2010-06-16 | 李见成 | Waste gas continuous purification device |
-
2012
- 2012-07-30 CN CN2012102661118A patent/CN102755822A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1996038218A1 (en) * | 1995-05-30 | 1996-12-05 | Thermal Energy International Inc. | Flue gas scrubbing and waste heat recovery system |
| CN1539546A (en) * | 2003-11-02 | 2004-10-27 | 华北电力大学 | A flue gas desulfurization and denitrification purification method and device |
| CN101332400A (en) * | 2008-07-18 | 2008-12-31 | 朱学智 | Applying PLC Control System to Carry Out Calcium Spraying Desulfurization Method in Circulating Fluidized Bed Boiler |
| CN101648099A (en) * | 2009-08-26 | 2010-02-17 | 福建龙净脱硫脱硝工程有限公司 | Purifying treatment device and purifying treatment method for flue gas multicomponent pollutant generated by incinerating refuse |
| CN101732941A (en) * | 2009-12-29 | 2010-06-16 | 李见成 | Waste gas continuous purification device |
Non-Patent Citations (1)
| Title |
|---|
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