CN210544299U - Flue gas desulfurization system - Google Patents
Flue gas desulfurization system Download PDFInfo
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- CN210544299U CN210544299U CN201921057425.0U CN201921057425U CN210544299U CN 210544299 U CN210544299 U CN 210544299U CN 201921057425 U CN201921057425 U CN 201921057425U CN 210544299 U CN210544299 U CN 210544299U
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- flue gas
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- heat exchange
- desulfurization system
- removal
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- 239000003546 flue gas Substances 0.000 title claims abstract description 132
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 119
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 63
- 230000023556 desulfurization Effects 0.000 title claims abstract description 63
- 239000007788 liquid Substances 0.000 claims abstract description 44
- 239000011734 sodium Substances 0.000 claims abstract description 38
- 239000000428 dust Substances 0.000 claims abstract description 34
- 239000002351 wastewater Substances 0.000 claims abstract description 29
- 238000010521 absorption reaction Methods 0.000 claims abstract description 27
- 229910052708 sodium Inorganic materials 0.000 claims abstract description 20
- 239000002699 waste material Substances 0.000 claims abstract description 20
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims abstract description 19
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 15
- 229910000029 sodium carbonate Inorganic materials 0.000 claims abstract description 13
- 230000008602 contraction Effects 0.000 claims description 14
- 238000009792 diffusion process Methods 0.000 claims description 14
- 238000002156 mixing Methods 0.000 claims description 12
- 238000007789 sealing Methods 0.000 claims description 9
- 239000003054 catalyst Substances 0.000 claims description 8
- 238000000889 atomisation Methods 0.000 claims description 7
- 230000008929 regeneration Effects 0.000 claims description 6
- 238000011069 regeneration method Methods 0.000 claims description 6
- 239000004568 cement Substances 0.000 claims description 4
- 239000007921 spray Substances 0.000 claims description 4
- 238000011144 upstream manufacturing Methods 0.000 claims description 4
- 230000003197 catalytic effect Effects 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 17
- 239000002250 absorbent Substances 0.000 abstract description 15
- 230000002745 absorbent Effects 0.000 abstract description 14
- 238000005260 corrosion Methods 0.000 abstract description 9
- 230000007797 corrosion Effects 0.000 abstract description 9
- 239000002918 waste heat Substances 0.000 abstract description 6
- 230000003009 desulfurizing effect Effects 0.000 abstract description 3
- 238000000746 purification Methods 0.000 abstract description 3
- 238000010438 heat treatment Methods 0.000 abstract description 2
- 230000002087 whitening effect Effects 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 14
- 238000006243 chemical reaction Methods 0.000 description 12
- 239000007789 gas Substances 0.000 description 7
- 239000000443 aerosol Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 239000003344 environmental pollutant Substances 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- 231100000719 pollutant Toxicity 0.000 description 6
- 238000000227 grinding Methods 0.000 description 5
- 230000004048 modification Effects 0.000 description 5
- 238000012986 modification Methods 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 230000009467 reduction Effects 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 230000000712 assembly Effects 0.000 description 4
- 238000000429 assembly Methods 0.000 description 4
- 238000004523 catalytic cracking Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000000843 powder Substances 0.000 description 4
- 239000000779 smoke Substances 0.000 description 4
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 4
- 238000005507 spraying Methods 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 3
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 3
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000001238 wet grinding Methods 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 239000007832 Na2SO4 Substances 0.000 description 2
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 239000002956 ash Substances 0.000 description 2
- 238000005520 cutting process Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 2
- 238000009837 dry grinding Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 230000006911 nucleation Effects 0.000 description 2
- 238000010899 nucleation Methods 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 241001625808 Trona Species 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 239000002270 dispersing agent Substances 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000007717 exclusion Effects 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 210000003456 pulmonary alveoli Anatomy 0.000 description 1
- 238000007873 sieving Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 229910052815 sulfur oxide Inorganic materials 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
Images
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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
-
- 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
- Y02E20/32—Direct CO2 mitigation
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- Treating Waste Gases (AREA)
Abstract
The utility model discloses a flue gas desulfurization system includes along flue gas flow direction flue gas desulfurization system in proper order: SO removal3A unit; a dust remover; a waste water heat exchange concentration unit; the sodium method desulfurization unit, the desulfurization waste liquid flows back to the waste water heat exchange concentration unit to exchange heat with the flue gas, and then flows to the SO removal unit3The unit is used as absorption liquid; and the exhaust funnel is internally provided with a heater, and steam discharged by the wastewater heat exchange concentration unit flows to the sodium desulfurization unit after heat exchange between the heater and flue gas. The utility model discloses a flue gas desulfurization system can be directly with Na in the sodium method desulfurization waste water2SO3Or further removing CO2Produced Na2CO3Is absorbent, SO is removed3The dew point temperature of the flue gas is greatly reduced, and the waste heat of the flue gas is directly used for concentrating Na generated by flue gas purification2SO3/Na2CO3The waste liquid can not cause the corrosion of the heat exchanger, and the generated steam can be used for heating, desulfurizing and purifying flue gas to perform whitening.
Description
Technical Field
The utility model relates to a waste flue gas handles field, in particular to flue gas desulfurization system.
Background
A great deal of SO is generated in the production process of various industries such as electric power, metallurgy, petrochemical industry and the like2And SO3The flue gas of (1). Currently, the commonly adopted desulphurization device is used for SO2Shows good removal effect but on SO3There was little removal. The existing data show that 0.5-1.5% of sulfur in a common coal-fired boiler is oxidized into SO in the power industry3(ii) a Under the condition of oxygen-enriched regeneration, the SO in the catalytic cracking regeneration flue gas3About 5% to 10% of the total amount of sulfur oxides; SO in sintering flue gas in iron and steel industry3The discharge amount of the sulfur oxide is 1% -2% of the total discharge amount of the sulfur oxide. In the general adoption of V2O5In the SCR denitration device using active component, part of SO is also added2Oxidation to SO3The conversion rate is about 0.5-1.5%, and especially SO is generated when the SCR reactor operates at low load2Conversion to SO3The conversion of (a) can be drastically increased.
SO3The corrosion inhibitor has strong corrosion, can be combined with water vapor in flue gas to form sulfuric acid, is condensed on the surface of a metal part at a dew point temperature, causes corrosion perforation of subsequent equipment such as a waste heat boiler, a CO boiler, an air preheater and the like, and influences the long-period operation of the device; SO (SO)3The ammonia gas can react with escaping ammonia of an SCR denitration system to generate viscous ammonium bisulfate, a large amount of generated ammonium bisulfate is deposited in catalyst channels at low temperature, fly ash is adhered, the catalyst channels are easily blocked to reduce the activity of the catalyst, and the ammonium bisulfate can enter downstream equipment such as a subsequent waste heat boiler, a CO boiler, an air preheater and the like along with flue gas and is adhered to the surface of a heat exchange element to cause ash accumulation, scaling, blockage and corrosion; in addition, in order to avoid SO in flue gas3Dew point corrosion is generated, the exhaust gas temperature of the boiler is generally higher and is generally over 180 ℃, and great waste of the heat of the exhaust gas is caused. SO discharged from chimney3Can also form H with water vapor in the atmosphere2SO4Aerosol, and H2SO4The aerosol is a precursor of PM2.5, causes one of the rudimentary haze, can be inhaled by a human body to enter pulmonary alveoli, is deposited in the human body and is difficult to discharge, so that the aerosol has great harm to the health of the human body.
When containing gaseous SO3When the flue gas passes through the wet flue gas desulfurization system, the flue gas is rapidly cooled to be below an acid dew point, SO3By homogeneous nucleation and heterogeneous nucleation with particulate matter as condensation nucleus, submicron-sized H which is difficult to capture is rapidly formed2SO4An aerosol. Generally, the fog drops with larger particles in the flue gas can be removed by the absorption tower, but the H with submicron order2SO4Aerosol, H formed by absorption tower without function2SO4The submicron aerosol can only be discharged into the atmosphere through a chimney, and a blue smoke phenomenon is formed at the mouth of the chimney.
It has been reported that there are 22 states in the United states for SO in flue gas from coal-fired power plants3Emission limits are proposed with 14 states requiring less than 6mg/m3Germany general2And SO3The mixed concentration discharge standard is set to 50 mg/m3Japan general SO3/H2SO4And controlling the total amount of the smoke. China has not yet dealt with SO in flue gas3The emission concentration of the sulfur-containing organic compound is definitely specified, but the scheme for supporting simultaneous development of combined collaborative removal of atmospheric pollutants and control of SO is proposed in action plans for energy conservation, emission reduction, upgrade and modification of coal and electricity (2014-2020)3And mercury, arsenic and other pollutants. The standard for the Integrated emission of atmospheric pollutants in Shanghai City (DB 31933-2015) stipulates that the maximum allowable emission concentration of the sulfuric acid mist is 5mg/m3The maximum allowable discharge rate is 1.1 kg/h; the emission Standard of atmospheric pollutants for boilers (manuscript of comments) in Hangzhou City, newly-built boiler flue gas SO3Emission limit of 5mg/m3Existing boiler flue gas SO3Emission limit of 10mg/m3. To SO according to local standard3The emission limit value puts forward a specific requirement, and SO in the flue gas3Has been a great trend in removal of (2).
At present, SO in flue gas3The removal method of (2) is mainly divided into two methods, one is a dry absorbent jet removal method, and the other is a wet absorbent jet removal method.
The dry absorbent is sodium-based absorbent, magnesium-based absorbent or calcium-based absorbent, and SO is removed by spraying the dry absorbent3When the particle size is smaller, SO3The higher the removal efficiency. The particle size of the commercially available alkaline powder is large, and the requirement on the particle size of the absorbent is difficult to meet, so that the absorbent needs to be ground. The grinding of the ultrafine powder is divided into dry grinding and wet grinding. The dry grinding can grind the powder to about 8 mu m with the lowest energy, but the temperature of the powder can be sharply increased in the grinding process, and the risk of dust explosion exists; the wet grinding needs to use a dispersing agent, an auxiliary agent and the like, the temperature is controlled, the continuous grinding time needs several hours or even more than ten hours, the grinding is carried out for dozens of times or even hundreds of times, the occupied area of grinding equipment is large, noise pollution is generated, sieving, dehydrating and drying treatment are carried out after the wet grinding, and the process is complicated. In addition, the dry absorbent is difficult to be mixed with the smoke gas when being sprayed in the flue, and the smoke gasAn additional static mixer is required in the channel.
The patent document CN103055684A uses trona as an absorbent, and has large dosage, application difficulty and cost. The coverage rate of the absorption liquid atomized and sprayed in the flue of the patent document CN103233656A is 150% -200%, which causes waste. Patent document CN105879641A sprays alkaline absorption liquid into the inlet of the SCR reactor, and unreacted alkali is liable to generate toxic and side effects on the SCR denitration catalyst.
The information disclosed in this background section is only for enhancement of understanding of the general background of the invention and should not be taken as an acknowledgement or any form of suggestion that this information constitutes prior art already known to a person skilled in the art.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a flue gas desulfurization system can effectively get rid of the SO in the flue gas3And the use of extra absorbent is reduced, and the new addition of pollutants or the corrosion of equipment is avoided.
Another object of the present invention is to improve the desulfurization efficiency and the lower utilization rate of the desulfurizing agent.
In order to achieve the above object, the utility model provides a flue gas desulfurization system includes along flue gas flow direction flue gas desulfurization system in proper order: SO removal3A unit; a dust remover; a waste water heat exchange concentration unit; the sodium method desulfurization unit, the desulfurization waste liquid flows back to the waste water heat exchange concentration unit to exchange heat with the flue gas, and then flows to the SO removal unit3The unit is used as absorption liquid; and the exhaust funnel is internally provided with a heater, and steam discharged by the wastewater heat exchange concentration unit flows to the sodium desulfurization unit after heat exchange between the heater and flue gas.
Further, in the above technical scheme, the desulfurization waste liquid is Na2SO3And (3) solution.
Furthermore, in the technical scheme, SO is removed3The unit is arranged in the flue and used for removing SO3The unit includes: at least one set of mixing elements, each set of mixing elements comprising: the shape of the sealing plate is matched with the inner diameter of the flue; a plurality of annular through-holes uniformly provided on the sealing plateThe cross section of the tube is Venturi tube-shaped; and a plurality of hollow conical nozzles arranged at the upstream of the plurality of annular through holes, each hollow conical nozzle corresponding to the center of one annular through hole, the hollow conical nozzles spraying absorption liquid to the annular through holes.
Further, in the above technical scheme, the annular through hole comprises a contraction section, a throat section and a diffusion section in sequence along the flow direction of the flue gas.
Further, in the technical scheme, the contraction angle of the contraction section is 23-30 degrees, the diffusion angle of the diffusion section is not more than 90 degrees, and preferably 5-20 degrees.
Further, in the above technical solution, the width of the inlet end of the contraction section is the same as the width of the outlet end of the diffusion section, and the width of the throat section is 0.5 times the width of the inlet end of the contraction section.
Further, in the above technical scheme, the hollow conical nozzle is a mechanical atomizing nozzle or a pneumatic atomizing nozzle.
Further, in the above technical scheme, the flue gas is catalytic cracking unit catalyst regeneration flue gas, coal-fired boiler flue gas or cement kiln flue gas.
Further, in the above technical scheme, the dust collector is a bag type dust collector, an electric dust collector or a cyclone dust collector.
The utility model also provides a flue gas desulfurization system includes along flue gas flow direction flue gas desulfurization system in proper order: SO removal3A unit; a dust remover; a waste water heat exchange concentration unit; a sodium desulfurization unit; CO removal2Unit for CO removal2The waste liquid flows back to the waste water heat exchange concentration unit to exchange heat with the flue gas and then flows to the SO removal unit3The unit is used as absorption liquid; and the exhaust funnel is internally provided with a heater, and steam discharged by the wastewater heat exchange concentration unit flows to the sodium desulfurization unit after heat exchange between the heater and flue gas.
Furthermore, in the technical scheme, CO is removed2The waste liquid is Na2CO3And (3) solution.
Furthermore, in the technical scheme, SO is removed3The unit is arranged in the flue and used for removing SO3The unit includes: at least one set of mixing elements, each set of mixing elements comprising: seal for a motor vehicleA plate having a shape matching the inner diameter of the flue; a plurality of annular through holes uniformly provided on the sealing plate, the annular through holes having a venturi-shaped cross section; and a plurality of hollow conical nozzles arranged at the upstream of the plurality of annular through holes, each hollow conical nozzle corresponding to the center of one annular through hole, the hollow conical nozzles spraying absorption liquid to the annular through holes.
Further, in the above technical scheme, the annular through hole comprises a contraction section, a throat section and a diffusion section in sequence along the flow direction of the flue gas.
Further, in the technical scheme, the contraction angle of the contraction section is 23-30 degrees, the diffusion angle of the diffusion section is not more than 90 degrees, and preferably 5-20 degrees.
Further, in the above technical solution, the width of the inlet end of the contraction section is the same as the width of the outlet end of the diffusion section, and the width of the throat section is 0.5 times the width of the inlet end of the contraction section.
Further, in the above technical scheme, the hollow conical nozzle is a mechanical atomizing nozzle or a pneumatic atomizing nozzle.
Further, in the above technical scheme, the flue gas is catalytic cracking unit catalyst regeneration flue gas, coal-fired boiler flue gas or cement kiln flue gas.
Further, in the above technical scheme, the dust collector is a bag type dust collector, an electric dust collector or a cyclone dust collector.
Compared with the prior art, the utility model discloses following beneficial effect has:
1. the utility model discloses a flue gas desulfurization system can be directly with Na in the sodium method desulfurization waste water2SO3Or further removing CO2Produced Na2CO3Is absorbent, SO is removed3The dew point temperature of the flue gas is greatly reduced, and the waste heat of the flue gas is directly used for concentrating Na generated by flue gas purification2SO3/Na2CO3The waste liquid can not cause the corrosion of the heat exchanger, and the generated steam can be used for heating, desulfurizing and purifying flue gas to perform whitening.
2. The utility model uses the Na produced by the flue gas purification2SO3Or Na2CO3For absorbent removalSO in flue gas3The method realizes the treatment of waste by waste without adding any pollutant.
3. The utility model discloses a take off SO3The unit reduces the flue gas flow area and increases the flue gas flow velocity by arranging the inner member in the flue, and the absorption liquid achieves the multistage atomization effect by utilizing the wind power cutting effect of nozzle atomization and high-flow-velocity flue gas on the absorption liquid, thereby greatly reducing the particle size of fog drops, increasing the gas-liquid two-phase contact area, and simultaneously fully playing the role of SO3The strong hygroscopicity and the rapidity of acid-base neutralization reaction enable gas-liquid two phases to realize strong mixing, gas-liquid mass transfer and reaction in a Venturi structure, and greatly increase the utilization rate of the desulfurizer and the desulfurization efficiency.
The foregoing description is only an overview of the technical solutions of the present invention, and in order to make the technical means of the present invention more clearly understood and to make the technical means more comprehensible, and to make the above and other objects, technical features, and advantages of the present invention easier to understand, one or more preferred embodiments are listed below, and the following detailed description is given with reference to the accompanying drawings.
Drawings
Fig. 1 is a schematic flow diagram of a flue gas desulfurization system according to one or more embodiments of the present invention.
Fig. 2 is a schematic flow diagram of a flue gas desulfurization system according to one or more embodiments of the present invention.
FIG. 3 is SO removal according to one or more embodiments of the present disclosure3The structure of the unit is shown schematically.
Fig. 4 is a schematic structural view of a sealing plate according to one or more embodiments of the present invention.
FIG. 5 is SO removal according to one or more embodiments of the invention3The distribution of the annular through holes of the unit on the cross section of the flue and the control schematic diagram of the hollow conical nozzle are shown, wherein the hollow conical nozzle is a mechanical atomization nozzle.
FIG. 6 is SO removal according to one or more embodiments of the invention3Distribution of annular through holes of units on flue cross section and hollow conical nozzleThe control schematic diagram is that the hollow conical nozzle is a pneumatic atomizing nozzle.
Description of the main reference numerals:
10-boiler, 20-flue gas, 30-SO removal3The unit comprises a 31-sealing plate, a 32-annular through hole, a 321-contraction section, a 322-throat section, a 323-diffusion section, a 331-spraying pipeline, a 332-hollow conical nozzle, a 333-valve, a 334-absorption liquid pipeline, a 335-compressed air pipeline, a 40-dust remover, a 50-wastewater heat exchange and concentration unit, a 60-sodium method desulfurization unit, a 70-CO removal unit2Unit, 80-exhaust funnel, 81-heater.
Detailed Description
The following detailed description of the present invention is provided in conjunction with the accompanying drawings, but it should be understood that the scope of the present invention is not limited by the following detailed description.
Throughout the specification and claims, unless explicitly stated otherwise, the word "comprise", or variations such as "comprises" or "comprising", will be understood to imply the inclusion of a stated element or component but not the exclusion of any other element or component.
Spatially relative terms, such as "below," "lower," "upper," "above," "upper," and the like, may be used herein for ease of description to describe one element or feature's relationship to another element or feature in the figures. It will be understood that the spatially relative terms are intended to encompass different orientations of the object in use or operation in addition to the orientation depicted in the figures. For example, if the items in the figures are turned over, elements described as "below" or "beneath" other elements or features would then be oriented "above" the elements or features. Thus, the exemplary term "below" can encompass both an orientation of below and above. The article may be otherwise oriented (rotated 90 degrees or at other orientations) and the spatially relative terms used herein should be interpreted accordingly.
In this document, the terms "first", "second", etc. are used to distinguish two different elements or portions, and are not used to define a particular position or relative relationship. In other words, the terms "first," "second," and the like may also be interchanged with one another in some embodiments.
As shown in FIG. 1, in the flue gas desulfurization system according to one or more embodiments of the present invention, SO is contained in the exhaust gas of a boiler 10XThe temperature of the flue gas 20 is 150-220 ℃, and the flue gas 20 is subjected to SO removal in sequence3Unit 30, dust remover 40, waste water heat exchange concentration unit 50, sodium desulfurization unit 60 and aiutage 80. In an exemplary embodiment of the present invention, the flow of the flue gas in the desulfurization system is: the flue gas 20 is in SO removal3SO is removed by reaction with the absorption liquid in unit 303Dust is removed in the dust remover 40, heat exchange and temperature reduction are carried out in the wastewater heat exchange concentration unit 50, and then SO is removed in the sodium desulphurization unit 602And then discharged to the atmosphere through the exhaust funnel 80. Wherein, the desulfurization waste liquid of the sodium method desulfurization unit 60 flows to the waste water heat exchange concentration unit 50 to exchange heat with the flue gas 20, and the desulfurization waste liquid after heat exchange concentration with the flue gas 20 flows to SO removal3The unit 30 is used as absorption liquid, and the waste heat of the flue gas is recovered. Illustratively, the desulfurized waste liquid is Na2SO3And (3) solution. When the flue gas 20 enters the dust remover 40, in the process of removing dust in the flue gas 20, SO in the flue gas 203With Na trapped by the dust collector 402SO3Reaction, further removing SO3. Removal of SO3The dew point temperature of the flue gas is greatly reduced, and after the heat exchange and temperature reduction of the desulfurization waste liquid from the wastewater heat exchange concentration unit 50 and the sodium-method desulfurization unit 60, the temperature of the flue gas can be reduced to 110-130 ℃, so that the flue gas is not corroded. Illustratively, the effluent from the wastewater heat exchange concentration unit 50 is used as SO-depleted3Na of absorption liquid of cell 302SO3The mass concentration of the solution is 2-20%, and the preferred mass concentration is 8-15%. The amount of the absorption liquid added is SO3Removal amount is measured as Na2SO3With SO3The molar ratio is 1: 1-3: 1.
as shown in FIG. 2, according to one or more embodiments of the present invention, a CO removal unit 60 is added after the sodium desulfurization unit of the flue gas desulfurization system shown in FIG. 12 Unit 70 for further removal of CO from flue gas2And then discharged to the atmosphere through the exhaust funnel 80. Flue gas is shown in figure 2The process in the desulfurization system is as follows: the flue gas 20 is in SO removal3SO is removed by reaction with the absorption liquid in unit 303Dust is removed in the dust remover 40, heat exchange and temperature reduction are carried out in the wastewater heat exchange concentration unit 50, and then SO is removed in the sodium desulphurization unit 602Entering into CO removal2Unit 70 CO removal2And then discharged to the atmosphere through the exhaust funnel 80. Unlike the desulfurization system shown in FIG. 1, the desulfurization system shown in FIG. 2 removes CO2Cell 70 discharging Na2CO3The solution flows to the waste water heat exchange concentration unit 50 to exchange heat with the flue gas 20, and Na after heat exchange concentration with the flue gas 202CO3The solution flows to SO removal3The unit 30 is used as absorption liquid, and the waste heat of the flue gas is recovered. Accordingly, when the flue gas 20 enters the dust remover 40, the SO in the flue gas 20 is removed in the process of removing the dust in the flue gas 203With Na trapped by the dust collector 402CO3Reaction, further removing SO3. Removal of SO3The dew point temperature of the flue gas is greatly reduced, and CO is removed in the waste water heat exchange concentration unit 502 Cell 70 discharging Na2CO3After the solution is subjected to heat exchange and temperature reduction, the temperature of the flue gas can be reduced to 110-130 ℃, and the worry about corrosion is avoided. Illustratively, the effluent from the wastewater heat exchange concentration unit 50 is used as SO-depleted3Na of absorption liquid of cell 302CO3The mass concentration of the solution is 2-20%, and the preferred mass concentration is 8-15%. The amount of the absorption liquid added is SO3Removal amount is measured as Na2CO3With SO3The molar ratio is 1: 1-3: 1.
with reference to fig. 1 and 2, for example, in one or more embodiments of the present invention, a heater 81 may be disposed in the exhaust funnel 80, and the steam generated by the wastewater heat exchange concentration unit 50 may heat the purified flue gas in the heater 81, where the steam temperature is 110-130 ℃, and the temperature of the heated purified flue gas is 70-80 ℃, so as to achieve "white elimination" of the flue gas. The condensed water generated by the heater 81 flows to the sodium desulfurization unit 60. Excess Na2SO3/Na2CO3The wastewater further produces solid products or is discharged after being treated.
Referring to fig. 3 and 4, in one or more embodiments of the present inventionIn one embodiment SO removal3The unit 30 is arranged in the flue and used for removing SO3The unit 30 comprises at least one set of mixing elements. Preferably, SO is removed3The unit 30 comprises 2-5 groups of mixing assemblies, and all the groups of mixing assemblies are sequentially arranged along the flow direction of the flue gas 20 in the flue. It should be understood that only one set of mixing assemblies is shown in fig. 3, and the present invention is not limited thereto. Each group of mixing assemblies comprises a sealing plate 31 matched with the inner diameter of the flue, a plurality of annular through holes 32 are uniformly arranged on the sealing plate 31, and the cross section of each annular through hole 32 is in a Venturi tube shape. Illustratively, the annular through-hole 32 includes a converging section 321, a throat section 322, and a diverging section 323 in order along the flow direction of the flue gas 20. The upstream of the center of each annular through hole 32 corresponds to a hollow conical nozzle 332, and the absorption liquid is sprayed from the hollow conical nozzle 332 to the annular through hole 32 through a spray pipe 331. The utility model discloses a take off SO3The unit 30 reduces the flow area of flue gas and increases the flow velocity of flue gas by arranging an inner member in the flue, and utilizes the atomization of the nozzle and the wind cutting action of high-flow-velocity flue gas on absorption liquid, so that the absorption liquid achieves a multi-stage atomization effect, the particle size of fog drops is greatly reduced, the contact area of gas and liquid phases is increased, the gas and liquid phases are intensively mixed and undergo gas and liquid mass transfer and reaction in the throat section of the annular through hole 32, and the utilization rate of a desulfurizer and the desulfurization efficiency are greatly increased.
Preferably, but not limitatively, in one or more exemplary embodiments of the present invention, the contraction angle of the contraction section 321 is 23 ° -30 °, and the diffusion angle of the diffusion section 323 is 90 ° or less, preferably 5 ° -20 °. Preferably, but not limitatively, the inlet end of the convergent section 321 has the same width as the outlet end of the divergent section 323, and the throat section 322 has a width 0.5 times the width of the inlet end of the convergent section 321. Preferably, but not limitatively, the air flow velocity of the throat section 322 is 20 to 80 m/s.
In one or more exemplary embodiments of the present invention, the hollow cone nozzle 332 is a mechanical atomizing nozzle or a pneumatic atomizing nozzle. As shown in FIG. 5, the hollow conical nozzle 332 can be a mechanical atomizing nozzle, the spray pipe 331 has a plurality of branch pipes, each branch pipe is provided with a valve 333, and the injection of the plurality of hollow conical nozzles 332 can be controlled in a partition manner by adjusting the valves 333. As shown in FIG. 6, the hollow conical nozzles 332 may be pneumatically atomized nozzles, and the absorption liquid pipe 334 and the compressed air pipe 335 may have a plurality of branch pipes, each of which is provided with a valve, so that the injection of the plurality of hollow conical nozzles 332 can be controlled in a divisional manner by adjusting the valves, or even the injection of each hollow conical nozzle 332 can be controlled individually.
In one or more exemplary embodiments of the present invention, the SO-containing3The flue gas is catalytic cracking unit catalyst regeneration flue gas, coal-fired boiler flue gas or cement kiln flue gas. While the embodiment shown in fig. 1 and 2 is shown with flue gas 20 exiting the boiler 10, it should be understood that the present invention is not limited thereto.
In one or more exemplary embodiments of the present invention, the dust collector 40 may be a bag type dust collector, an electric dust collector, or a cyclone dust collector. Preferably a bag house. The filtering speed is 0.5-5.0 m/s, and when the pressure drop of the bag type dust collector reaches 0.5-1.3 kPa, the ash is removed.
In one or more exemplary embodiments of the present invention, SO is removed3In the unit 30, when excessive Na is sprayed into the flue gas2SO3After solution, Na2SO3With SO in flue gas3The following reactions occur:
SO3+ Na2SO3→ Na2SO4+ SO2①
in one or more exemplary embodiments of the present invention, SO is removed3In the unit 30, when excessive Na is sprayed into the flue gas2CO3After solution, Na2CO3With SO in flue gasXThe following reactions occur:
Na2CO3+SO2→Na2SO3+CO2
after drying of the sprayed solution, solid Na is formed2SO3（SO3Adsorbent), with SO3Reaction:
Na2SO3+SO3→Na2SO4+SO2
the foregoing descriptions of specific exemplary embodiments of the present invention have been presented for purposes of illustration and description. It is not intended to limit the invention to the precise form disclosed, and obviously many modifications and variations are possible in light of the above teaching. The exemplary embodiments were chosen and described in order to explain certain principles of the invention and its practical application to enable one skilled in the art to make and use various exemplary embodiments of the invention and various alternatives and modifications as are suited to the particular use contemplated. Any simple modifications, equivalent changes and modifications made to the above exemplary embodiments shall fall within the scope of the present invention.
Claims (11)
1. The utility model provides a flue gas desulfurization system which characterized in that, along flue gas flow direction flue gas desulfurization system includes in proper order:
SO removal3A unit;
a dust remover;
a waste water heat exchange concentration unit;
and a sodium desulfurization unit, wherein the desulfurization waste liquid flows back to the wastewater heat exchange concentration unit to exchange heat with the flue gas and then flows to the SO removal unit3The unit is used as absorption liquid; and
and a heater is arranged in the exhaust funnel, and steam discharged by the wastewater heat exchange concentration unit flows to the sodium desulfurization unit after the heat exchange between the heater and the flue gas.
2. The flue gas desulfurization system of claim 1, wherein the desulfurization waste liquid is Na2SO3And (3) solution.
3. The flue gas desulfurization system according to claim 1 or 2, wherein the SO removal is performed3The unit is arranged in the flue and used for removing SO3The unit includes:
at least one set of mixing elements, each set of mixing elements comprising:
the shape of the sealing plate is matched with the inner diameter of the flue;
a plurality of annular through holes uniformly provided on the sealing plate, the annular through holes having a venturi-shaped cross section; and
and the hollow conical nozzles are arranged at the upstream of the annular through holes, each hollow conical nozzle corresponds to the center of one annular through hole, and the hollow conical nozzles spray the absorption liquid to the annular through holes.
4. The flue gas desulfurization system according to claim 3, wherein the annular through-hole comprises a constriction section, a throat section and a diffuser section in this order in the flue gas flow direction.
5. The flue gas desulfurization system according to claim 4, wherein the contraction angle of the contraction section is 23 ° -30 °, and the diffusion angle of the diffusion section is not greater than 90 °.
6. The flue gas desulfurization system according to claim 4, wherein the inlet end of the constriction section has the same width as the outlet end of the diffusion section, and the width of the throat section is 0.5 times the width of the inlet end of the constriction section.
7. The flue gas desulfurization system of claim 3, wherein the hollow conical nozzle is a mechanical atomization nozzle or a pneumatic atomization nozzle.
8. The flue gas desulfurization system according to claim 1 or 2, wherein the flue gas is catalytic cracker catalyst regeneration flue gas, coal-fired boiler flue gas, or cement kiln flue gas.
9. The flue gas desulfurization system according to claim 1 or 2, wherein the dust collector is a bag filter, an electric dust collector, or a cyclone dust collector.
10. The utility model provides a flue gas desulfurization system which characterized in that, along flue gas flow direction flue gas desulfurization system includes in proper order:
SO removal3A unit;
a dust remover;
a waste water heat exchange concentration unit;
a sodium desulfurization unit;
CO removal2Unit for CO removal2The waste liquid flows back to the waste water heat exchange concentration unit to exchange heat with the flue gas and then flows to the SO removal unit3The unit is used as absorption liquid; and
and a heater is arranged in the exhaust funnel, and steam discharged by the wastewater heat exchange concentration unit flows to the sodium desulfurization unit after the heat exchange between the heater and the flue gas.
11. The flue gas desulfurization system of claim 10, wherein the CO removal is performed2The waste liquid is Na2CO3And (3) solution.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114432851A (en) * | 2020-10-31 | 2022-05-06 | 中国石油化工股份有限公司 | SO removal of flue gas3System and method |
| CN114618274A (en) * | 2022-02-21 | 2022-06-14 | 柳州钢铁股份有限公司 | Method for preventing corrosion of metal heat exchanger |
-
2019
- 2019-07-09 CN CN201921057425.0U patent/CN210544299U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114432851A (en) * | 2020-10-31 | 2022-05-06 | 中国石油化工股份有限公司 | SO removal of flue gas3System and method |
| CN114618274A (en) * | 2022-02-21 | 2022-06-14 | 柳州钢铁股份有限公司 | Method for preventing corrosion of metal heat exchanger |
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