CN108786423A - A kind of smoke comprehensive administering method and device - Google Patents
A kind of smoke comprehensive administering method and device Download PDFInfo
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- CN108786423A CN108786423A CN201810909848.4A CN201810909848A CN108786423A CN 108786423 A CN108786423 A CN 108786423A CN 201810909848 A CN201810909848 A CN 201810909848A CN 108786423 A CN108786423 A CN 108786423A
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- flue gas
- oxidation
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- 238000000034 method Methods 0.000 title claims abstract description 29
- 239000000779 smoke Substances 0.000 title claims abstract description 19
- 239000003546 flue gas Substances 0.000 claims abstract description 102
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 100
- 238000010521 absorption reaction Methods 0.000 claims abstract description 48
- 230000003647 oxidation Effects 0.000 claims abstract description 35
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 35
- 238000010438 heat treatment Methods 0.000 claims abstract description 34
- 239000003344 environmental pollutant Substances 0.000 claims abstract description 28
- 231100000719 pollutant Toxicity 0.000 claims abstract description 28
- 230000009466 transformation Effects 0.000 claims abstract description 25
- 239000007789 gas Substances 0.000 claims abstract description 23
- 238000010791 quenching Methods 0.000 claims abstract description 22
- 238000003303 reheating Methods 0.000 claims abstract description 22
- 238000009833 condensation Methods 0.000 claims abstract description 20
- 230000005494 condensation Effects 0.000 claims abstract description 20
- 238000001816 cooling Methods 0.000 claims abstract description 15
- 230000008569 process Effects 0.000 claims abstract description 8
- 238000006477 desulfuration reaction Methods 0.000 claims description 22
- 239000002002 slurry Substances 0.000 claims description 22
- 239000007921 spray Substances 0.000 claims description 15
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 13
- 239000002250 absorbent Substances 0.000 claims description 12
- 230000023556 desulfurization Effects 0.000 claims description 12
- 239000002826 coolant Substances 0.000 claims description 7
- 230000007423 decrease Effects 0.000 claims description 7
- 238000012805 post-processing Methods 0.000 claims description 7
- 210000002966 serum Anatomy 0.000 claims description 7
- 230000007246 mechanism Effects 0.000 claims description 6
- 238000003860 storage Methods 0.000 claims description 5
- 230000035515 penetration Effects 0.000 claims description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims 1
- 239000005864 Sulphur Substances 0.000 claims 1
- 238000007789 sealing Methods 0.000 claims 1
- 230000008901 benefit Effects 0.000 abstract description 6
- 238000010276 construction Methods 0.000 abstract description 4
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 51
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 23
- 239000012071 phase Substances 0.000 description 19
- 239000002245 particle Substances 0.000 description 18
- 230000000052 comparative effect Effects 0.000 description 17
- 239000000428 dust Substances 0.000 description 14
- 229910001385 heavy metal Inorganic materials 0.000 description 12
- 230000000694 effects Effects 0.000 description 10
- 239000000443 aerosol Substances 0.000 description 9
- 235000019504 cigarettes Nutrition 0.000 description 9
- 229920002313 fluoropolymer Polymers 0.000 description 9
- 239000010419 fine particle Substances 0.000 description 8
- 239000013618 particulate matter Substances 0.000 description 8
- 239000006096 absorbing agent Substances 0.000 description 6
- 229910052785 arsenic Inorganic materials 0.000 description 6
- 229910052753 mercury Inorganic materials 0.000 description 6
- 229910052751 metal Inorganic materials 0.000 description 6
- 239000002184 metal Substances 0.000 description 6
- 230000009471 action Effects 0.000 description 5
- 230000003009 desulfurizing effect Effects 0.000 description 5
- 238000009792 diffusion process Methods 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical compound [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 5
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- 238000001089 thermophoresis Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 239000004809 Teflon Substances 0.000 description 2
- 229920006362 Teflon® Polymers 0.000 description 2
- 230000002776 aggregation Effects 0.000 description 2
- 238000004220 aggregation Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000004581 coalescence Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000010339 dilation Effects 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 230000003020 moisturizing effect Effects 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 238000013517 stratification Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Inorganic materials O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 2
- 239000012808 vapor phase Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 210000000481 breast Anatomy 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000002209 hydrophobic effect Effects 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- MXWHMTNPTTVWDM-NXOFHUPFSA-N mitoguazone Chemical compound NC(N)=N\N=C(/C)\C=N\N=C(N)N MXWHMTNPTTVWDM-NXOFHUPFSA-N 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000000844 transformation Methods 0.000 description 1
- 239000011800 void material Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 238000004457 water analysis Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
Abstract
The invention discloses a kind of smoke comprehensive administering methods and device, this method to handle flue gas, and flue gas enters absorption tower and in absorption tower in uphill process from absorption tower lower part, passes sequentially through cooling, removes SO2, dedusting demisting, phase transformation condensation and deep removal pollutant and heating reheating after discharge.It realizes the smoke comprehensive controlling device of the method, including absorption tower, is equipped with oxidation unit, Quench concentration temperature reducing unit, SO successively from bottom to up in absorption tower2Absorptive unit, dedusting demisting unit, phase transformation condensation and pollutant deep removal unit, efficient demisting unit and the hot cell again that heats up；It is equipped with gas inlet between oxidation unit and Quench concentration temperature reducing unit, exhanst gas outlet is equipped at the top of heating reheating unit.The advantages such as smoke comprehensive of the present invention administers superior performance, and level of integrated system is high, and overall construction and operating cost are low, and univers parameter matching and operating condition are good, and floor space is small, really realize " one-stop " smoke gas treatment overall up to standard.
Description
Technical field
The invention belongs to smoke comprehensive Treatment process fields, and in particular to a kind of smoke comprehensive administering method and device.
Background technology
Industrial boiler generally use fossil fuel, such as coal and oil.Since these fossil fuels in combustion can
Generate the harmful substances such as sulfur dioxide, nitrogen oxides, dust, heavy metal.Wet desulphurization widely used at present has desulfurization anti-
Answer the features such as speed is fast, efficient, sulfur-removing additives utilization rate is high, product can realize recycling, be meet circular economy,
A kind of technique that sustainable development requires.
Existing Wet Flue Gas Desulfurization Technique, former flue gas is merely through void tower Multi-layer sprinkling, demisting two procedures scrubbing CO_2, cigarette
Gas discharge is difficult to realize minimum discharge index (NOx、SO2, dust be respectively lower than 50,35,5mg/Nm3), for SO3, Hg, As etc.
Heavy metal removing effect is limited, meanwhile, wet desulfurization flue gas can carry a large amount of moisture discharges, cause water resource and vapor gas
Change latent heat waste, chimney " emitting white cigarette " phenomenon is serious, pollutes object and discharges exceeded and energy waste.
Invention content
It is for the defects in the prior art and insufficient, the present invention provides a kind of smoke comprehensive administering method and device, gram
Take existing smoke gas treatment technology easily occur flue gas emission is exceeded, pollutant control not comprehensively, " white plume " phenomenon and resource
The defect of waste.
In order to achieve the above objectives, the present invention takes the following technical solution：
A kind of smoke comprehensive administering method, this method handle flue gas, and flue gas enters absorption tower from absorption tower lower part
And in absorption tower in uphill process, passes sequentially through cooling, removes SO2, dedusting demisting, phase transformation condensation and deep removal pollutant
It is discharged with after heating reheating.
Flue gas is handled specifically, passing sequentially through following steps：
Step 1：Flue gas carries out Quench concentration cooling by Quench concentration temperature reducing unit, inhibits the generation of aerosol；
Step 2：Flue gas continues to rise through SO2The multi-stage spray layer of absorptive unit removes SO2；
Step 3：Flue gas rises through dedusting demisting unit, removes the large dust particle in flue gas；
Step 4：Flue gas rises through pollutant deep removal unit again, cools down with phase-change condenser indirect heat exchange, flue gas
Middle fine particle moves under the action of heat gushes power towards the vapor droplet of condensation, meanwhile, vapor largely condenses, and enhances
The collision frequency of droplet and particulate matter is conducive to particulate matter cohesion and grows up, in the process, SO2, dust, the heavy metals such as Hg it is solidifying
Coalescence is precipitated；
Step 5：Flue gas discharges after heating reheating unit carries out heating reheating again.
Optionally, depth denitrification step can also be added between step 1 and step 2, specifically：Flue gas rises through
Low-temperature oxidation unit, spray ozone oxidation carry out depth denitration.
The present invention also provides a kind of smoke comprehensive controlling devices for realizing the method, including absorption tower, on absorption tower
Inside it is equipped with oxidation unit, Quench concentration temperature reducing unit, SO successively from bottom to up2Absorptive unit, dedusting demisting unit, phase transformation condensation
And pollutant deep removal unit, efficient demisting unit and heating hot cell again；
It is equipped with gas inlet between oxidation unit and Quench concentration temperature reducing unit, cigarette is equipped at the top of heating reheating unit
Gas exports.
The invention also includes following technical characteristics：
Optionally, the phase transformation condensation and pollutant deep removal unit include the phase-change condenser being set in absorption tower,
Phase-change condenser is communicated with the mechanism that cools by the pipeline with coolant circulation pump；The efficient demisting unit includes being set to
Demister in absorption tower；Hot cell includes the heating reheater being set in absorption tower again for the heating.
Optionally, in the absorption tower different zones be equipped with tower tray, for realizing concentration of slurry in tower from bottom to top by
Grade successively decrease and tower in temperature reduce step by step from bottom to top.
Optionally, in SO2Absorptive unit lower part is equipped with the tower tray；In SO2It is set between absorptive unit and dedusting demisting unit
There is the tower tray.
Optionally, temperature reducing unit and SO are concentrated in the Quench2It is additionally provided with low-temperature oxidation unit between absorptive unit, is used for
Spray penetration denitration；
The low-temperature oxidation unit includes the ozone nozzle being set in absorption tower, and the ozone nozzle is communicated with ozone
System.
Optionally, the oxidation unit is used in absorb the bottom of the tower oxidation sweetening product, and oxidation unit includes absorption tower bottom
Portion inner cavity, absorb the bottom of the tower inner cavity seal air inlet pipe and post-processing communicating pipe of the connection with wind turbine respectively；After described
It is used to processing communicating pipe slurries being delivered to after-treatment system；
The Quench concentration temperature reducing unit includes carrying the serum recycle pipeline of slurry circulating pump and in absorption tower
Slurries nozzle, the slurries nozzle are connected to the serum recycle pipeline.
Optionally, the SO2Absorptive unit includes the multistage SO being set in absorption tower2Absorbent nozzle, SO2Absorbent sprays
Head has been respectively communicated with circulating slot and SO by the pipeline with desulfuration recycle pump2Absorbent storage box；The dedusting demisting unit
It include the dedusting demister in absorption tower.
Optionally, it is with pressure to circulating slot bottom to realize to be connected to the air inlet pipe for the circulating slot sealed bottom
Oxidation；At the top of circulating slot SO is connected to by being connected to the seal of tube2Absorption tower inner cavity below absorptive unit is for conveying desulfurization product
To circulating slot；Circulating slot also seals the connection pipeline for carrying desulfuration recycle pump.
Optionally, the phase-change condenser that the pollutant deep removal unit uses is fluoroplastics nonmetallic heat exchanger；Institute
The heating reheater that uses of heating reheating unit is stated as fluoroplastics nonmetallic heat exchanger.
Compared with prior art, the present invention beneficial has the technical effect that：
(I) present invention is that have the de- white, dedusting of water removal, except the heavy metals such as sour gas and Hg and energy-savings such as SO2, SO3
The flue gas integrated synthesis administering method and device of water effect.
The present invention greatly improves desulfurization dust-removing efficiency, together using the design concept of " decreasing energy, concentration step absorb "
When by " flue gas phase transformation agglomerate, heat up reheating " technology, flue gas vapor may be implemented on tower upper layer and condense water-saving, deep removal
The effects that heavy metals such as particulate matter, Hg, As in flue gas, flue gas heat recovery, can meet simultaneously minimum discharge technology and
Flue gas " de- white " requires, desulfurizing tower exiting flue gas NOx, SO2, dustiness be respectively lower than 50,35,5mg/Nm3, humidity of flue gas drop
Low 30% or more, pollutant removings rate >=30% such as SO3, Hg, As.Smoke comprehensive administers superior performance, and level of integrated system is high, always
The advantages such as body construction and operating cost are low, and univers parameter matching and operating condition are good, and floor space is small, really realize " a station
Formula " smoke gas treatment overall up to standard.
(II) flue gas first passes through slurries spray Quench cooling in the present invention, and flue-gas temperature rapid drawdown effectively inhibits sulphite
Decomposition, and then reduce the generation of aerosol, then by low-temperature oxidation section depth denitration, flue gas continues on through single-stage or multi-stage spray
Remove SO2Equal sour gas, dedusting demister intercept part large dust particle and droplet, and the flue gas for continuing to rise passes through phase transformation
Condenser cools down, and since steam partial pressure is more than saturation pressure at this temperature, vapor supersaturation phase transformation is condensed and generated big
Harl is measured, vapor largely condenses and (can be used for desulfurizing tower moisturizing) in flue gas, and fine particle is under the action of heat gushes power in flue gas
Vapor droplet towards condensation moves, meanwhile, vapor largely condenses, and enhances the collision frequency of droplet and particulate matter, has
It grows up conducive to particulate matter cohesion, in the process, SO2, dust, the heavy metals such as Hg agglomerate and are precipitated；For range grain within 1 μm
The particle of diameter, thermophoretic forces are very notable to its diffusion, and thermophoresis diffusion velocity is higher, under the action of thermophoretic forces, within 1 μm
Particle aggregation becomes larger, and is partly attached to the particle of heat exchange pipe surface and can be cleaned, and other agglomerate increased fine particle and pass through
Demister removing discharge, it can be achieved that in flue gas moisture recycling, pollutant deep removal；Micron order fine particle is steamed with water in flue gas
Airsetting fogging is dripped collision frequency and is risen, and during Water vapor condensation, hydrone reunion is grown up, SO3, the heavy metals such as Hg, As
The hydrone package that molecule is attached to hydrone or is agglomerated, finally sweeps along in droplet, is cooperateed with as vapor phase transformation condenses
It administers, this is the key that the present invention realizes deep desulfuration, removing heavy metal.
(III) tower tray is arranged in different zones in comprehensive treatment tower, realizes that concentration of slurry successively decreases step by step from bottom to top in tower,
Tower area temperature reduces step by step from bottom to top.Bottom enriching section flue gas cool-down, absorber portion are used for highly effective reaction desulfurization, and top is efficiently removed
Dirt.Each reaction zone is relatively independent, is independent of each other, and ensures each regional work performance.
The reheating section that heats up uses heat source indirect heat exchange, improves exhaust gas temperature, and flue gas extension and lifting force significantly improve, cigarette
Air water saturated with vapor degree is greatly reduced, and heat source used is unrestricted, original flue gas can be used to carry out indirect heat exchange, has energy saving effect
Fruit.
(IV) the characteristics of being directed in fire coal boiler fume containing particulate matter, sour gas, phase transformation knockouts and heating reheating
Fluoroplastics (or other similar materials) heat exchanger can be used in device.It mainly has the advantage that：Material corrosion resistance, wear-resisting property
Excellent, surface hydrophobicity is strong, is not easy dust stratification, and equipment running resistance is small, and O&M expense is low；Fluoroplastics exchange heat original paper with great
Specific surface area, heat exchange property are excellent；Fluoroplastics density is the 1/4 of common metal, the teflon heat exchanger of same heat exchange amount, weight
Far below metallic recuperator, it is conducive to the advantages such as installation and civil construction in tower.
(V) in the present invention, in SO2Larger atomizing particle size nozzle can be used in absorber portion lower layer, reduces aerosol and droplet is taken
Band, in SO2Smaller atomizing particle size nozzle can be selected in absorber portion upper layer, and spray coverage rate is high, and atomizing particle size is small, large specific surface area,
Heat and mass transfer performance is excellent, and desulfuration efficiency is high.Small atomizing particle size nozzle can be used in dedusting demisting water spray section, be conducive to efficiently
Capture dedusting.
Description of the drawings
Fig. 1 is the overall structure diagram of the smoke comprehensive controlling device of the present invention；
Fig. 2 is relational graph of the collision efficiency with particle and different-grain diameter droplet.
Fig. 3 is that heat gushes influence diagram of the power to different-grain diameter.
Each label is expressed as in figure:1- oxidation units, 2- Quench concentrate temperature reducing unit, 3- low-temperature oxidation units, 4-SO2It inhales
Receive unit, 5- dedusting demisting units, 6- pollutant deep removal units, the efficient demisting units of 7-, 8- heatings hot cell again；
100- gas inlets, 101- exhanst gas outlets；
11- wind turbines, 12- air inlet pipes, 13- slurry circulating pumps, 14- serum recycle pipelines, 15- post-processing connections
Pipe；
21- slurries nozzles；
31- ozone nozzles, 32- ozone generators；
41-SO2Absorbent nozzle, 42- desulfuration recycle pumps, 43- circulating slots, 44-SO2Absorbent storage box；
51- dedusting demisters；
61- phase-change condensers, 62- coolant circulation pumps, 63- cool mechanism；
71- demisters；
81- heating reheaters.
The present invention is illustrated below in conjunction with specification drawings and specific embodiments.
Specific implementation mode
Present embodiment provides a kind of smoke comprehensive administering method, and this method handles flue gas, and flue gas is from absorption tower
Lower part enters absorption tower and in absorption tower in uphill process, passes sequentially through cooling, removes SO2, dedusting demisting, phase transformation condensation simultaneously
It is discharged after deep removal pollutant and heating reheating.
Following steps are passed sequentially through to handle flue gas：
Step 1：Flue gas carries out Quench concentration cooling by Quench concentration temperature reducing unit, inhibits the generation of aerosol；
Step 2：Flue gas continues to rise through SO2The multi-stage spray layer of absorptive unit removes SO2；
Step 3：Flue gas rises through dedusting demisting unit, removes the large dust particle in flue gas；
Step 4：Flue gas rises through pollutant deep removal unit again, cools down with phase-change condenser indirect heat exchange, flue gas
Middle fine particle moves under the action of heat gushes power towards the vapor droplet of condensation, meanwhile, vapor largely condenses, and enhances
The collision frequency of droplet and particulate matter is conducive to particulate matter cohesion and grows up, in the process, SO2, dust, the heavy metals such as Hg it is solidifying
Coalescence is precipitated；
Step 5：Flue gas discharges after heating reheating unit carries out heating reheating again.
In the present embodiment, depth denitrification step is added in step 1 and step 2, specifically：Flue gas rises logical
Low temperature oxidation unit is crossed, spray ozone oxidation carries out depth denitration.
The present invention also provides a kind of smoke comprehensive controlling devices for realizing the method, including absorption tower, on absorption tower
Inside it is equipped with oxidation unit 1, Quench concentration temperature reducing unit 2, SO successively from bottom to up2Absorptive unit 4, dedusting demisting unit 5, phase transformation
Condensation and pollutant deep removal unit 6, efficient demisting unit 7 and heating reheating unit 8；It is concentrated in oxidation unit 1 and Quench
It is equipped with gas inlet 100 between temperature reducing unit 2, exhanst gas outlet 101 is equipped at 8 top of heating reheating unit.
In the present embodiment, the phase transformation condensation and pollutant deep removal unit 6 include the phase being set in absorption tower
Become condenser 61, phase-change condenser 61 is communicated with the mechanism 63 that cools by the pipeline with coolant circulation pump 62；The height
Effect demisting unit 7 includes the demister 71 being set in absorption tower；The heating reheating unit 8 includes the heating being set in absorption tower
Reheater 81.In other embodiments, MGGH may be used and replace heating reheater 81, former fume afterheat is utilized to realize
Carry out heating reheating.
In the absorption tower different zones be equipped with tower tray, successively decrease step by step from bottom to top for realizing concentration of slurry in tower with
And temperature reduces step by step from bottom to top in tower.
Specifically, in SO24 lower part of absorptive unit is equipped with the tower tray；In SO2Absorptive unit 4 and dedusting demisting unit 5 it
Between be equipped with the tower tray.
Temperature reducing unit 2 and SO are concentrated in the Quench2Low-temperature oxidation unit 3 is additionally provided between absorptive unit 4, for spraying
Depth denitration；The low-temperature oxidation unit 3 includes the ozone nozzle 31 being set in absorption tower, and the ozone nozzle 31 is communicated with smelly
Oxygen evolution system system 32.
Specifically, the oxidation unit 1 is used in absorb the bottom of the tower oxidation sweetening product, oxidation unit 1 includes absorption tower
Bottom inner cavity, absorb the bottom of the tower inner cavity seal air inlet pipe 12 and post-processing communicating pipe of the connection with wind turbine 11 respectively
15；It is used to the post-processing communicating pipe 15 slurries being delivered to after-treatment system；The Quench concentration temperature reducing unit 2 includes carrying
The serum recycle pipeline 14 of slurry circulating pump 13 and the slurries nozzle 21 in absorption tower, the slurries nozzle 21 are connected to described
Serum recycle pipeline 14.
SO2Absorptive unit 4 includes the multistage SO being set in absorption tower2Absorbent nozzle 41, SO2Absorbent nozzle 41 passes through
Pipeline with desulfuration recycle pump 42 has been respectively communicated with circulating slot 43 and SO2Absorbent storage box 44；The dedusting demisting unit 5
It include the dedusting demister 51 in absorption tower.
More specifically, 43 sealed bottom of the circulating slot is connected to the air inlet pipe 12 to realize to circulating slot 43
Bottom oxidation with pressure；43 top of circulating slot is connected to SO by being connected to the seal of tube2The absorption tower inner cavity of 4 lower section of absorptive unit is for defeated
It send in desulfurization product to circulating slot 43；Circulating slot 43 also seals the connection pipeline for carrying desulfuration recycle pump 42.
Optionally, the phase-change condenser 61 that the phase transformation condensation and pollutant deep removal unit 6 use is non-for fluoroplastics
Metallic recuperator (or other similar materials)；The heating reheater 81 that the heating reheating unit 8 uses is nonmetallic for fluoroplastics
Heat exchanger (or other similar materials).It mainly has the advantage that：Material corrosion resistance, wear-resisting property are excellent, surface hydrophobic
Property is strong, is not easy dust stratification, equipment running resistance is small, and O&M expense is low；Fluoroplastics exchange heat original paper with great specific surface area, heat exchange
It has excellent performance；Fluoroplastics density is the 1/4 of common metal, and the teflon heat exchanger of same heat exchange amount, weight is changed far below metal
Hot device is conducive to the advantages such as installation and civil construction in tower.
In the present embodiment, slurry circulating pump, wind turbine, slurries nozzle, ozone nozzle, ozone generation system, SO2It absorbs
Agent nozzle, desulfuration recycle pump, circulating slot, SO2It is absorbent storage box, dedusting demister, phase-change condenser, coolant circulation pump, cold
But the systems auxiliary device such as cooling mechanism, demister, heating reheater and system equipment for after-treatment are conventional equipment.
As shown in Fig. 2, for the fine particle within 1 μm, Blang's diffusion is smaller with inertia, and droplet interception function is unknown
Aobvious, therefore, for the fine particle within 1 μm, collision mechanism is more micro- to the collision efficiency effect of droplet and aerosol particle
It is weak.And cooled by flue gas, harl and heat exchanger tube surface temperature are less than aerosol particle temperature, are conducive to aerosol particle
(submicron order) reunites under thermophoresis force effect, and is moved to harl and heat exchanger tube surface.As shown in figure 3, for 1
The particle of range grain size within μm, thermophoretic forces are very notable to its diffusion, and thermophoresis diffusion velocity is higher.In the work of thermophoretic forces
Under, particle aggregation becomes larger within 1 μm, is partly attached to the particle of heat exchange pipe surface and can be cleaned, and other cohesions are increased
Fine particle is removed by demister and is discharged, this is the guarantee of efficiently demisting of the invention.
In compliance with the above technical solution, specific embodiments of the present invention are given below, it should be noted that the present invention not office
It is limited to following specific examples, all equivalent transformations made on the basis of the technical solutions of the present application each falls within the protection model of the present invention
It encloses.The present invention is described in further details with reference to embodiment.
Embodiment 1：
In the experimental system of the present embodiment, exhaust gas volumn 50000Nm3/ h, inlet flue gas dustiness≤50mg/Nm3, SO2 is dense
Degree≤2000mg/Nm3, NOx concentration≤150mg/Nm3；
Step 1：Flue gas carries out Quench concentration cooling by Quench concentration temperature reducing unit, inhibits the generation of aerosol；
Step 2：Flue gas rises through low-temperature oxidation unit, and spray ozone oxidation carries out flue gas NOx concentration after depth denitration
It is reduced to≤50mg/Nm3；
Step 3：Flue gas continues to rise through SO2The multi-stage spray layer of absorptive unit removes SO2；
Step 4：Flue gas rises through dedusting demisting unit, removes the large dust particle in flue gas；Flue gas through step 3 and
After step 4, SO2 concentration is reduced to≤30mg/Nm3, dust concentration≤8mg/Nm3；
Step 5：Flue gas rises through pollutant deep removal unit again, cools down with phase-change condenser indirect heat exchange, this reality
It applies in example, cooling temperature of circulating water control in phase transformation condensation region is in import≤32 DEG C, and outlet circulating water temperature is at 37 DEG C or so, flue gas
Temperature is condensed by phase transformation to 48 DEG C (phase-change condenser unlatchings) from 52 DEG C of (phase-change condenser closing) flue gases, and dust contains in flue gas
Amount is reduced to 1~4mg/Nm3.System 1~1.2t of recovered flue gas condensed water per hour, wherein condensed water PH are 3 or so, condensed water
In dissolved with heavy metals such as a large amount of acid solutions and Hg, As.The step is the key that realize water-saving " de- white ", the deep purifying of flue gas, the portion
Divide condensed water to can be used as desulphurization system moisturizing use, saves water consume.For part plant area, low-temperature receiver can continue profit after heating
With realization steam gasification recovery of latent heat utilizes.
Step 6：Flue gas discharges after heating reheating unit carries out heating reheating again, and the flue gas of deep purifying passes through liter again
The lifting force and dilation angle of warm reheater enhancing flue gas, further decrease flue gas saturation degree, realize vision " no white cigarette ", environment
Temperature >=15 DEG C, in the case of relative air humidity≤50%, smog discharge temperature is higher than 60 DEG C, and vision " white cigarette " phenomenon is atomic
Weak, almost without trailing phenomenon, finally discharge reaches minimum discharge standard to flue gas.
In other embodiments, as needed further removing flue gas pollutant and flue gas moisture, more harsh
Under the conditions of realize vision " no white cigarette ", can by further decrease flue gas condensing temperature and improve flue gas exhaust gas temperature
Reach effect.
Comparative example 1:
This comparative example provides a kind of conventional wet desulfurization system, and difference lies in this comparisons with embodiment 1 for this comparative example
The system of example is condensed without containing phase transformation, and pollutant deep removal section, i.e., the flue gas of gas inlet is directly through SO2It is absorber portion, common
Direct demister removal after water multi-stage spray, after testing：Since conventional Sprayer Circulation coolant-temperature gage is higher, can not flue gas be dropped
Temperature, vapor condense phase transformation, that is, substantially without flue gas " de- white " water-saving result, and are condensed using phase transformation, pollutant depth
After removing section, flue gas can be made to eliminate white cigarette, vapor phase 30~40% or more vapor condensation and removal in flue gas
Cycle can be participated in desulfurizing tower by becoming the water generated after cohesion, reduce desulfurizing tower rate of water make-up.
Comparative example 2:
This comparative example provides a kind of conventional wet desulfurization system, and difference lies in this comparisons with embodiment 1 for this comparative example
The system of example is condensed without containing phase transformation, and pollutant deep removal section, i.e., the flue gas of gas inlet is directly through SO2It is absorber portion, common
Direct demister removal after water multi-stage spray, after testing：It condenses due to the use of phase transformation, after pollutant deep removal section, can incite somebody to action
Vapor condensation and removal in flue gas, and the SO in flue gas2, dust particale object, the substances such as heavy metal be dissolved in or mixed with vapor,
It is difficult to detach, and by flue gas " dehydration ", the contaminant collecting that this part can be mixed with vapor, to further decrease
Pollutant emission in flue gas.Off-gas recovery water (without flue gas condensing) water analysis is compared, Cl in flue gas condensing water-、
SO4 2-, the content of beary metal such as Hg, As be vapor, powder in flue gas pollutant deep removal flue gas 2~5 times in off-gas recovery water
Dirt, heavy metal, sour gas equal size can reduce by 30% or more so that flue gas deep purifying discharges.
Comparative example 3:
This comparative example provides a kind of conventional wet desulfurization system, and difference lies in this comparisons with embodiment 1 for this comparative example
The system of example is without containing the hot arc again that heats up, i.e., flue gas is through SO2Direct emission after demister again after absorber portion, washing, after testing：By
In flue gas without the reheating that heats up, flue gas remains as saturation wet flue gas, and plume rise power and dilation angle are relatively low, in chimney breast,
Since environment temperature is relatively low, flue gas intersects in temperature-fall period with saturated steam line, Water vapor condensation, vision " white cigarette " phenomenon
Obviously.
Comparative example 4:
This comparative example provides a kind of wet desulfurization system directly cooling using flue gas, the area of this comparative example and embodiment 1
It is not, the system of this comparative example is using directly cooling (directly spraying cooling medium, be in direct contact with the flue gas) mode of flue gas
For flue gas cool-down (cooling, cold water cooling of slurries etc.).The carrying of flue gas droplet and aerosol can be caused to generate using the technique, together
When flue gas pollutant can be caused to influence system stable operation to the pollution of cooling medium.
Comparative example 5:
This comparative example provides the desulphurization system that the indirect type of cooling is used after a kind of wet desulphurization, this comparative example and embodiment
1 difference lies in the system of this comparative example is cooled down using common metal heat exchanger, and equipment is arranged in outside desulfurizing tower.
Using this kind of mode, mainly have the disadvantages that：1. heat exchanger specific surface area is much smaller than embodiment 1, it is unfavorable for subtle of flue gas
The cohesion of grain, meanwhile, embodiment 1 also has defogging effect (being similar to tubular demister), is conducive to exhaust gas dust removing；2. by
Contain multiple pollutant in flue gas, flue gas condensing water acidity is stronger, for common metal seriously corroded.
Claims (9)
1. a kind of smoke comprehensive administering method, this method handle flue gas, which is characterized in that flue gas from absorption tower lower part into
Enter absorption tower and in absorption tower in uphill process, passes sequentially through cooling, removes SO2, dedusting demisting, phase transformation condensation and depth it is de-
It is discharged after depollution object and heating reheating.
2. a kind of smoke comprehensive controlling device for realizing claim 1 the method, which is characterized in that including absorption tower, inhaling
It receives and is equipped with oxidation unit (1), Quench concentration temperature reducing unit (2), SO in tower successively from bottom to up2Absorptive unit (4), dedusting demisting
Unit (5), phase transformation condensation and pollutant deep removal unit (6), efficient demisting unit (7) and hot cell (8) again of heating up；
Gas inlet (100) is equipped between oxidation unit (1) and Quench concentration temperature reducing unit (2), in hot cell (8) again of heating up
Top is equipped with exhanst gas outlet (101).
3. device as claimed in claim 2, which is characterized in that the phase transformation condensation and pollutant deep removal unit (6) packet
The phase-change condenser (61) in absorption tower is included, phase-change condenser (61) is connected to by carrying the pipeline of coolant circulation pump (62)
The mechanism that cools (63)；The efficient demisting unit (7) includes the demister (71) being set in absorption tower；The heating is again
Hot cell (8) includes the heating reheater (81) being set in absorption tower.
4. device as claimed in claim 2, which is characterized in that different zones are equipped with tower tray in the absorption tower, for real
In existing tower concentration of slurry successively decrease step by step from bottom to top and tower in temperature reduce step by step from bottom to top.
5. device as claimed in claim 4, which is characterized in that in SO2Absorptive unit (4) lower part is equipped with the tower tray；In SO2
The tower tray is equipped between absorptive unit (4) and dedusting demisting unit (5).
6. device as claimed in claim 2, which is characterized in that in Quench concentration temperature reducing unit (2) and SO2Absorptive unit
(4) it is additionally provided with low-temperature oxidation unit (3) between, is used for spray penetration denitration；
The low-temperature oxidation unit (3) includes the ozone nozzle (31) being set in absorption tower, and the ozone nozzle (31) is communicated with
Ozone generation system (32).
7. device as claimed in claim 2, which is characterized in that the oxidation unit (1) is used for de- in absorb the bottom of the tower oxidation
Sulphur product, oxidation unit (1) include absorb the bottom of the tower inner cavity, and absorb the bottom of the tower inner cavity seals connection and carries wind turbine (11) respectively
Air inlet pipe (12) and post-processing communicating pipe (15)；The post-processing communicating pipe (15) is used to slurries being delivered to post-processing
System；
The Quench concentration temperature reducing unit (2) includes carrying the serum recycle pipeline (14) of slurry circulating pump (13) and set on absorption
Slurries nozzle (21) in tower, the slurries nozzle (21) are connected to the serum recycle pipeline (14).
8. device as claimed in claim 7, which is characterized in that the SO2Absorptive unit (4) includes more in absorption tower
Grade SO2Absorbent nozzle (41), SO2Absorbent nozzle (41) has been respectively communicated with by carrying the pipeline of desulfuration recycle pump (42) and has been followed
Annular groove (43) and SO2Absorbent storage box (44)；The dedusting demisting unit (5) includes the dedusting demister being set in absorption tower
(51)。
9. device as claimed in claim 8, which is characterized in that circulating slot (43) sealed bottom is connected to the air input
Pipeline (12) is to realize to the oxidation with pressure of circulating slot (43) bottom；At the top of circulating slot (43) SO is connected to by being connected to the seal of tube2
Absorption tower inner cavity below absorptive unit (4) is for conveying in desulfurization product to circulating slot (43)；Circulating slot (43) the also company of sealing
The logical pipeline for carrying desulfuration recycle pump (42).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810909848.4A CN108786423A (en) | 2018-08-10 | 2018-08-10 | A kind of smoke comprehensive administering method and device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810909848.4A CN108786423A (en) | 2018-08-10 | 2018-08-10 | A kind of smoke comprehensive administering method and device |
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| CN108786423A true CN108786423A (en) | 2018-11-13 |
Family
ID=64079731
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| Application Number | Title | Priority Date | Filing Date |
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| CN201810909848.4A Pending CN108786423A (en) | 2018-08-10 | 2018-08-10 | A kind of smoke comprehensive administering method and device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110052128A (en) * | 2019-03-18 | 2019-07-26 | 山东博然电力科技有限公司 | A kind of desulfurizer that control white cigarette generates |
| CN113332838A (en) * | 2021-05-31 | 2021-09-03 | 国能神东煤炭集团有限责任公司 | Smoke white elimination control method, storage medium and electronic equipment |
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| CN207056315U (en) * | 2017-07-14 | 2018-03-02 | 孙晓 | A kind of ultra-clean discharge of flue gas and white cigarette eliminate integrated apparatus |
| CN108057325A (en) * | 2017-12-27 | 2018-05-22 | 西安航天源动力工程有限公司 | A kind of temperature classification formula ammonia type flue gas desulfurizing demisting technique and system |
| US20180140991A1 (en) * | 2015-07-21 | 2018-05-24 | Huaneng Power International, Inc. | High-efficiency gradient hierarchy complex desulfurizing tower |
| CN208244444U (en) * | 2018-08-10 | 2018-12-18 | 西安航天源动力工程有限公司 | A kind of smoke comprehensive controlling device |
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| US4082835A (en) * | 1975-06-27 | 1978-04-04 | Allied Chemical Corporation | Removal of SO2 from gases |
| US20180140991A1 (en) * | 2015-07-21 | 2018-05-24 | Huaneng Power International, Inc. | High-efficiency gradient hierarchy complex desulfurizing tower |
| CN207056315U (en) * | 2017-07-14 | 2018-03-02 | 孙晓 | A kind of ultra-clean discharge of flue gas and white cigarette eliminate integrated apparatus |
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| CN110052128A (en) * | 2019-03-18 | 2019-07-26 | 山东博然电力科技有限公司 | A kind of desulfurizer that control white cigarette generates |
| CN113332838A (en) * | 2021-05-31 | 2021-09-03 | 国能神东煤炭集团有限责任公司 | Smoke white elimination control method, storage medium and electronic equipment |
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