CN107519751A - The processing unit and method and purposes of a kind of electrolytic aluminium carbon anode roasting flue gas - Google Patents
The processing unit and method and purposes of a kind of electrolytic aluminium carbon anode roasting flue gas Download PDFInfo
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- CN107519751A CN107519751A CN201710940495.XA CN201710940495A CN107519751A CN 107519751 A CN107519751 A CN 107519751A CN 201710940495 A CN201710940495 A CN 201710940495A CN 107519751 A CN107519751 A CN 107519751A
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- 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
- B01D53/75—Multi-step processes
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- 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
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- 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
- B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
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- 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
- B01D53/68—Halogens or halogen compounds
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- 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
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/10—Oxidants
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/10—Oxidants
- B01D2251/104—Ozone
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/10—Oxidants
- B01D2251/106—Peroxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/10—Oxidants
- B01D2251/108—Halogens or halogen compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/50—Combinations of absorbents
- B01D2252/504—Mixtures of two or more absorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Abstract
The present invention relates to the processing unit of electrolytic aluminium carbon anode roasting flue gas and method and purposes, including flue-gas-cooling system, electrical tar precipitator, pre-oxidation system and the semidry method cleaning system being sequentially connected；Wherein, the outlet of flue-gas-cooling system is connected with the entrance of electrical tar precipitator, and the outlet of electrical tar precipitator is connected with the entrance of semidry method cleaning system by intermediate flue, and intermediate flue is provided with pre-oxidation system.Flue gas removes most of glance coal by electrical tar precipitator, and NO is oxidized to high-valence state NO by pre-oxidation systemx, it is CO by glance coal oxidation Decomposition2And H2O, then remove SO in semidry method cleaning system2, high-valence state NOx, fluoride and glance coal.The present invention realizes the Collaborative Control of multiple pollutant, and purification efficiency is higher, disclosure satisfy that the discharge standard of increasingly strict electrolytic aluminium carbon anode roasting flue gas.
Description
Technical field
The present invention relates to Pollutant Control Technology field, more particularly to a kind of processing of electrolytic aluminium carbon anode roasting flue gas
Device and method and purposes.
Background technology
Electrolytic aluminium carbon anode roasting refers to process of the green anode through 1150 DEG C of high-temperature roastings after shaping.Green anode is matched somebody with somebody
In material containing calcining petroleum coke into calcined coke, the pitch as adhesive and a part of anode scrap.Carbon anode roasting cigarette
Gas composition is complex, and its major pollutants includes particulate matter (350mg/m3)、SO2(300mg/m3)、NOx(50-120mg/m3)、
Fluoride (50-80mg/m3) and glance coal (185mg/m3), multiple pollutant discharge is exceeded.Calcining process is electrolytic aluminium carbon sun
One important procedure of pole production, pollutant discharge amount are higher in whole aluminium industry pollutant discharge amount accounting.Therefore, carbon is developed
Plain anode-baking flue gas multi-pollutant untied simulated techniques, realize SO in flue gas2, fluoride and glance coal joint removing, tool
It is significant.
The method that electrically trapped tar oil purification techniques traps tar using high-pressure electrostatic.At present dry electrostatic oil-trap more into
Work(.40000~60000V is maintained with Electrostatic method supply voltage.Glance coal is larger in high temperature applicationss ratio resistance, it is difficult to removes；
Temperature is too low to be easily adhered and not easy-clear (under glance coal condensation temperature).General control electrostatic catcher entrance flue gas temperature
Not less than 70~80 DEG C, average efficiency is 90% or so.But electrically trapped tar oil purification techniques is to SO in flue gas2It is unnet with fluoride
Change effect, on the premise of generally performing special emission limit in the multiple areas in the whole nation, need to additionally add desulfurization defluorinate facility.
Aluminum oxide dry method purification techniques is the dry purification process using aluminum oxide as adsorbent.Can be with the drip in purifying smoke
Blue or green cigarette, fluoride, particulate matter.This technique be raw material-aluminum oxide using Aluminum Electrolysis Production as adsorbent, adsorb substantial amounts of pitch
The aluminum oxide of tar returns to Aluminum Electrolysis Production and used.Into after electrolytic cell, a part of tarvia is burned off, and another part enters
Electrolytic aluminum smoke, cause certain secondary pollution.And the aluminum oxide mobility containing tarvia is poor, after returning to electrolytic cell
Electrolyte phosphorus content can be caused to increase, normally produced so as to influence electrolytic cell.
Wet purification technology uses dilute NaOH solution spray washing, HF and SO in flue gas2Absorbed by NaOH solution, one
Dust and glance coal is divided also to be washed, the flue gas come out from scrubbing tower purifies through wet electrical dust precipitator again.But wet cleaning is present
Some defects：System is huge, and capital expenditure and maintenance are costly, need to solve the problems, such as discharge of wastewater and equipment corrosion.
CN 1974866A disclose a kind of anode-baking furnace flue gas purifying technique applied to electrolytic aluminium anode factory.
Baking furnace fume first passes around flue-gas-cooling system by cooling high-temperature fume, and the flue gas after cooling removes smoke abatement into electrical tar precipitator
Substantial amounts of tarvia in gas, a large amount of tar in flue gas are removed into dry purifying system afterwards, afterwards into dry cleaning
System removes the solid-state fluoride and HF gases, flue dust, tar in flue gas, and the flue gas after purification enters cigarette by main smoke discharging blower fan
Chimney.But the anode-baking furnace flue gas purifying technique of the electrolytic aluminium anode factory is to the SO in flue gas2And NOxSubstantially without net
Change effect.
The content of the invention
In view of electrolytic aluminium carbon anode roasting flue gas is difficult to not only economy but also efficiently by SO mostly in the prior art2、NOx、
The integration joint removing of the multi-pollutant such as fluoride and glance coal, an object of the present invention be to provide it is a kind of by desulfurization,
Denitration, defluorinate, the apparatus and method of the effective integration of depitching cigarette system and circulating fluid bed reactor, realize electrolytic aluminium carbon
Multi-pollutant integration joint removing in anode-baking flue gas.
For the above-mentioned purpose, the present invention adopts the following technical scheme that：
In a first aspect, the invention provides a kind of processing unit of electrolytic aluminium carbon anode roasting flue gas, including connect successively
Flue-gas-cooling system, electrical tar precipitator, pre-oxidation system and the semidry method cleaning system connect.
Wherein, the outlet of the flue-gas-cooling system is connected with the entrance of the electrical tar precipitator, the electrical tar precipitator
Outlet be connected with the entrance of the semidry method cleaning system by intermediate flue, the intermediate flue is provided with pre-oxidation system.
For electrolytic aluminium carbon anode roasting flue gas, only installation electrical tar precipitator is difficult to meet SO mostly2、NOx, fluoride and
The multi-pollutants such as glance coal administer present situation, the present invention combine circulating fluid bed semi-drying method have technological process it is short, take up an area it is small, effect
The advantages that rate is high, by the effective integration of desulphurization and denitration, defluorinate, depitching cigarette system and circulating fluid bed reactor, realize more
Integration joint removing of the pollutant in circulating fluid bed reactor.Pre-oxidation system wherein of the present invention and semidry method purification system
Synergy between system be present, the NO in flue gas is not only oxidized to high-valence state NO by pre-oxidation systemx, while by pitch in flue gas
Cigarette organic principle oxidation Decomposition is CO2And H2O so that flue gas enter semidry method cleaning system in after easily in the effect of atomized water
Lower to be absorbed by absorbent, absorption efficiency improves, and the removal of glance coal is more thorough.
Preferably, the flue-gas-cooling system includes pervaporation cooling tower, water pump, conveyance conduit, spray gun and PLC controls system
System.
Preferably, the electrical tar precipitator is horizontal dual field electric cleaner.
Preferably, the pre-oxidation system includes oxidant supply arrangement, dilution air, surge tank and distributor.
Preferably, the semidry method cleaning system includes absorbent storehouse, spray nozzle, recirculating fluidized bed reaction tower.
The bottom of the recirculating fluidized bed reaction tower is inlet end, and the inlet end is provided with Venturi, the text
The air inlet of device connects the gas outlet of the pre-oxidation system in mound, and the gas outlet of the Venturi is located at the circulation
The inside of fluid bed reacting tower.
The expansion segment of the Venturi is provided with absorbent entrance and spray nozzle, and the absorbent entrance is with absorbing
Agent storehouse is connected.
Preferably, the absorbent storehouse is filled with absorbent.
Preferably, the absorbent include lime, magnesia, red mud, carbide slag and flyash any one or at least
Two kinds of combination, wherein typical but non-limiting be combined as：The combination of the combination of lime and magnesia, red mud and carbide slag,
The combination of lime and flyash, the combination of red mud, carbide slag and flyash.Coal-fired thermal power is typically had in view of aluminium electrolysis enterprise
Factory, while thermoelectricity is provided, discharge substantial amounts of flyash solid waste.And main component is Al in flyash2O3And SiO2, separately contain
There are 10%~20% or so alkaline metal oxide (CaO, MgO, Na2O、K2O etc.) and 5% or so uncompleted burned carbon.Wherein,
Al2O3And SiO2The absorbents such as CaO, MgO are much better than to the absorbability of fluoride, alkaline metal oxide can be used for absorbing
SO in flue gas2With high-valence state NOx, and uncompleted burned carbon then can be used for adsorbing the glance coal in flue gas.Therefore, present absorbent
It is preferred that flyash.The collaboration that flyash not only realizes sulfide, fluoride and glance coal removes, and derives from electrolytic aluminium work
Solid waste on industry chain, reach collaboration and control useless doulbe-sides' victory effect.Ensure the desulfurization suitable with lime, magnesia, red mud, carbide slag
Denitration efficiency, while further improve the purification efficiency of fluoride and glance coal.
Preferably, the semidry method cleaning system also includes cyclone separator, sack cleaner and ash silo.
Preferably, the gas outlet of the recirculating fluidized bed reaction tower is connected with the air inlet of the cyclone separator, described
The gas outlet of cyclone separator is connected with the air inlet of the sack cleaner, the gas outlet of the sack cleaner and the ash
The air inlet in storehouse is connected.
Preferably, the bottom of the cyclone separator is provided with the first separation hopper, and the outlet of the first separation hopper is set
Have tie point and the second branch road, in order to by reacted absorbent return realization recycle, the tie point with it is described
The expansion segment of Venturi is connected, and second branch road is connected with the ash silo.
Preferably, the bottom of the sack cleaner be provided with second separation hopper, it is described second separation hopper outlet with
Ash silo is connected.
Preferably, the outlet of the second separation hopper and the described first the second branch road remittance for separating hopper and rear and ash silo
It is connected.
Second aspect, the invention provides a kind of processing method of electrolytic aluminium carbon anode roasting flue gas, methods described bag
Include following steps：
1) the electrolytic aluminium carbon anode roasting flue gas is cooled, liquid bitumen tar is generated after cohesion；
2) flue gas through step 1) cooling carries out electrically trapped tar oil, removes liquid bitumen tar；
3) flue gas after step 2) electrically trapped tar oil is pre-oxidized；
4) flue gas after step 3) is pre-oxidized carries out semidry method purification, removes particulate matter, SO in flue gas2, high-valence state
NOx, fluoride and glance coal, be purified flue gas.
Preferably, methods described is carried out using device as described in relation to the first aspect.
Preferably, the step 1) cooling is carried out in flue-gas-cooling system.
Preferably, the method for the step 1) cooling cools including water spraying atomization.
Preferably, after the step 1) cooling flue gas temperature be 90~100 DEG C, such as 90 DEG C, 91 DEG C, 92 DEG C, 93 DEG C,
94 DEG C, 95 DEG C, 96 DEG C, 97 DEG C, 98 DEG C, 99 DEG C or 100 DEG C etc..
Preferably, the step 2) electrically trapped tar oil is carried out in electrical tar precipitator.
Preferably, the pre-oxidation described in step 3) is carried out in pre-oxidation system.
Preferably, oxidant is hydrogen peroxide, ozone, potassium permanganate, sodium hypochlorite and sodium chlorite used by step 3)
Any one or at least two combination, wherein, it is typical but non-limiting to be combined as：The combination of hydrogen peroxide and ozone, it is high
The combination of the combination of potassium manganate and sodium hypochlorite, hydrogen peroxide and sodium chlorite.
Preferably, the semidry method purification described in step 4) is carried out in semidry method cleaning system.
Preferably, used by step 4) absorbent be flyash, lime, magnesia, red mud, carbide slag any or
At least two combination, preferably flyash.
As currently preferred technical scheme, the processing method of electrolytic aluminium carbon anode roasting flue gas includes following step
Suddenly：
1) high-temperature flue gas is after flue-gas-cooling system is cooled to 90~100 DEG C, most of gaseous glance coal in flue gas
It is condensed into liquid bitumen tar；
2) enter electrical tar precipitator after flue gas cool-down, remove liquid bitumen tar；
3) flue gas enters pre-oxidation system, using appointing for hydrogen peroxide, ozone, potassium permanganate, sodium hypochlorite and sodium chlorite
A kind of or at least two combinations of anticipating are pre-oxidized flue gas as oxidant；
4) flue gas enters semidry method cleaning system, with flyash, lime, magnesia, red mud, carbide slag any or extremely
Few two kinds combination absorbs particulate matter, the SO removed in flue gas as absorbent2, high-valence state NOx, fluoride and glance coal, wherein
Absorbent in absorbent storehouse sprays into the expansion segment of Venturi with powder-form, while spray nozzle sprays into atomized water, with
Flue gas enters recirculating fluidized bed reaction tower, and absorbent is reacted or inhaled to the multi-pollutant in flue gas in the presence of atomized water
Removing is received, realizes that semidry method purifies, flue gas separation is preferably carried out by cyclone separator and sack cleaner, gained dirt powder is collected
In Yu Huicang, Hui Cangzhong dirt powder is preferably returned to Venturi and recycled as absorbent, and separating obtained purifying smoke can
It is expelled directly out.
The third aspect, the invention provides a kind of purposes of device as described in relation to the first aspect, described device takes off for desulfurization
Nitre defluorinate depitching cigarette integrated purifying technique.
Compared with prior art, the present invention at least has the advantages that：
1. electrolytic aluminium carbon anode roasting flue gas processing device provided by the invention, realize the collaboration control of multiple pollutant
System, and purification efficiency is higher, desulfuration efficiency is up to more than 95%, and for denitration efficiency up to more than 80%, defluorinate compound efficiency is reachable
More than 90%, depitching cigarette efficiency disclosure satisfy that increasingly strict electrolytic aluminium carbon anode roasting flue gas up to more than 95%
Discharge standard；
2. the present invention cooperates with mutually pre-oxidation system with semidry method cleaning system, desulfuration efficiency, denitration effect are not only improved
Rate and depitching cigarette efficiency, it is further without that special denitrification apparatus and depitching cigarette device is separately configured so that the economy of device
Loomed large with validity；
3. the present invention by selecting suitable absorbent, coordinates with the dry systems of recirculating fluidized bed half, realizes that multi-pollutant exists
Integration joint removing in circulating fluid bed reactor.
Brief description of the drawings
Fig. 1 is the schematic diagram of device in the embodiment of the present invention 1；
Mark is illustrated as in figure：1- flue-gas-cooling systems；2- electrical tar precipitators；3- pre-oxidizes system；4- semidry methods purify
System；5- absorbents storehouse；6- spray nozzles；7- recirculating fluidized bed reaction towers；8- cyclone separators；9- sack cleaners；10- ashes
Storehouse；11- chimneys
Embodiment
Further illustrate technical scheme below in conjunction with the accompanying drawings and by embodiment.But following reality
Example is only the simple example of the present invention, does not represent or limit the scope of the present invention, protection scope of the present invention
It is defined by claims.
Embodiment 1
A kind of electrolytic aluminium carbon anode roasting fume desulfurizing, defluorinating depitching cigarette device, including the flue gas cooling being sequentially connected
System 1, electrical tar precipitator 2, pre-oxidation system 3 and semidry method cleaning system 4, flue-gas-cooling system 1 exports and electrical tar precipitator
2 entrances are connected, and the outlet of electrical tar precipitator 2 is connected with the entrance of semidry method cleaning system 4, the semidry method cleaning system 4 of electrical tar precipitator 2
Intermediate flue is provided with pre-oxidation system 3.
Flue-gas-cooling system 1 is made up of pervaporation cooling tower, water pump, conveyance conduit, spray gun, PLC control system, electric tar
Oily device 2 is horizontal dual field electric cleaner, and pre-oxidation system 3 is by oxidant supply arrangement, dilution air, surge tank, distributor
Composition, semidry method cleaning system 4 is by absorbent storehouse 5, spray nozzle 6, recirculating fluidized bed reaction tower 7, cyclone separator 8, pocket type
Deduster 9 and ash silo 10 form.
Electrical tar precipitator 2, which exports to come in and go out with the flue gas of the bottom of recirculating fluidized bed reaction tower 7, to be connected.Absorbent storehouse 5 and circulation
The venturi expansion segment of fluid bed reacting tower 7 is connected.Spray nozzle 6 is located at the venturi expansion segment of recirculating fluidized bed reaction tower 7.
The separation hopper of the bottom of cyclone separator 8 is divided into two branch roads, and the venturi of a branch road and recirculating fluidized bed reaction tower 7 is expanded
Duan Xianglian, another branch road are connected with after the separation hopper convergence of the bottom of sack cleaner 8 with ash silo 10.
A kind of more pollutions carried out by above-mentioned electrolytic aluminium carbon anode roasting flue gas desulfurization and denitrification defluorinate depitching cigarette device
The method that thing jointly controls, methods described comprise the following steps：
1) after high-temperature flue gas cools by flue-gas-cooling system 1, most of gaseous glance coal is condensed into liquid in flue gas
State tarvia；
2) enter electrical tar precipitator 2 after flue gas cool-down, remove liquid bitumen tar；
3) flue gas enters pre-oxidation system 3, and NO in flue gas is oxidized into high-valence state NOx, by glance coal oxidation point in flue gas
Solve as CO2And H2O；
4) flue gas enters semidry method cleaning system 4, removes particulate matter, SO in flue gas2, high-valence state NOx, fluoride and drip
Blue or green cigarette, the wherein absorbent in absorbent storehouse 5 spray into the expansion segment of Venturi with powder-form, while spray nozzle 6 sprays
Enter atomized water, enter recirculating fluidized bed reaction tower 7 with flue gas, absorbent is in the presence of atomized water to the multi-pollutant in flue gas
Reacted or absorbing and removing, realize that semidry method purifies, preferably passed through cyclone separator 8 and sack cleaner 9 carries out flue gas point
From, gained dirt powder is collected in ash silo 10, and the dirt powder in ash silo 10 is preferably returned to Venturi and recycled as absorbent,
Separating obtained purifying smoke is expelled directly out by chimney 11.
Embodiment 2
Using the device described in embodiment 1, the baking flue gas of 100,000 tons/year of carbon annode factories is purified：
Exhaust gas volumn is 100000m3/ h, initial flue gas temperature are 150 DEG C, SO2Concentration is 300mg/m3, NOxConcentration is
80mg/m3, fluoride concentration 50mg/m3, asphalt smoke concentration 200mg/m3.By flue-gas-cooling system by flue gas cool-down extremely
100 DEG C, ozone is used to use flyash for oxidant as absorbent.SO after processing2Concentration is 10mg/m3, NOxConcentration is
10mg/m3, fluoride concentration 2.5mg/m3, asphalt smoke concentration 3.5mg/m3。
Embodiment 3
Using the device described in embodiment 1, the baking flue gas of 60,000 tons/year of carbon annode factories is purified：
Exhaust gas volumn is 50000m3/ h, initial flue gas temperature are 180 DEG C, SO2Concentration is 500mg/m3, NOxConcentration is
120mg/m3, fluoride concentration 80mg/m3, asphalt smoke concentration 300mg/m3.By flue-gas-cooling system by flue gas cool-down extremely
90 DEG C, hydrogen peroxide is used as oxidant, using flyash and lime quality ratio 1:1 composite absorber.SO after processing2Concentration is
8mg/m3, NOxConcentration is 15mg/m3, fluoride concentration 2mg/m3, asphalt smoke concentration 5mg/m3。
Embodiment 4
With differing only in for embodiment 2：Oxidant replaces with potassium permanganate, and absorbent replaces with magnesia and red mud matter
Measure ratio 1:1 composite absorber.
SO after processing2Concentration is 8mg/m3, NOxConcentration is 10mg/m3, fluoride concentration 5mg/m3, asphalt smoke concentration is
10mg/m3。
Embodiment 5
With differing only in for embodiment 3：Oxidant replaces with sodium hypochlorite, and absorbent replaces carbide slag.
SO after processing2Concentration is 15mg/m3, NOxConcentration is 15mg/m3, fluoride concentration 5mg/m3, asphalt smoke concentration is
12mg/m3。
Embodiment 6
With differing only in for embodiment 3：Oxidant replaces with sodium chlorite, and absorbent replaces with：Magnesia and fine coal
Grey mass ratio 1:2 composite absorber.
SO after processing2Concentration is 5mg/m3, NOxConcentration is 10mg/m3, fluoride concentration 2.5mg/m3, asphalt smoke concentration
For 3.5mg/m3。
Comparative example 1
With differing only in for embodiment 3：Pre-oxidation system is saved in device.
SO after processing2Concentration is 8mg/m3, NOxConcentration is 110mg/m3, fluoride concentration 2mg/m3, asphalt smoke concentration is
50mg/m3。
Comparative example 2
With differing only in for embodiment 3：Device replaces with the purification shown in Fig. 3 in CN1974866A embodiments
System.
SO after processing2Concentration is 450mg/m3, NOxConcentration is 115mg/m3, fluoride concentration 3.5mg/m3, glance coal is dense
Spend for 15mg/m3。
If comparative example 2 will improve desulfurization and denitration efficiency, it is necessary to increase extra desulfurization and denitrification apparatus, not only increase
Equipment complexity reduces its economy, and the removing to fluoride and glance coal does not also almost help, it is impossible to realizes this hair
Bright integration removing, purification efficiency is also not as the present invention.Comparative examples 3 understand that the present invention is pre- with comparative example 1, comparative example 2
Oxidative system not only improves denitration efficiency, and improves the efficiency of depitching cigarette, achieves unexpected technique effect.
Applicant states that the present invention illustrates the detailed process equipment of the present invention and technological process by above-described embodiment,
But the invention is not limited in above-mentioned detailed process equipment and technological process, that is, it is above-mentioned detailed not mean that the present invention has to rely on
Process equipment and technological process could be implemented.Person of ordinary skill in the field it will be clearly understood that any improvement in the present invention,
The addition of equivalence replacement and auxiliary element to each raw material of product of the present invention, selection of concrete mode etc., all fall within the present invention's
Within the scope of protection domain and disclosure.
Claims (10)
1. a kind of processing unit of electrolytic aluminium carbon anode roasting flue gas, it is characterised in that including the flue gas cooling being sequentially connected
System (1), electrical tar precipitator (2), pre-oxidation system (3) and semidry method cleaning system (4)；
Wherein, the outlet of the flue-gas-cooling system (1) is connected with the entrance of the electrical tar precipitator (2), the electrically trapped tar oil
The outlet of device (2) is connected with the entrance of the semidry method cleaning system (4) by intermediate flue, and the intermediate flue is provided with pre- oxygen
Change system (3).
2. device as claimed in claim 1, it is characterised in that the flue-gas-cooling system (1) includes pervaporation cooling tower, water
Pump, conveyance conduit, spray gun and PLC control system.
3. device as claimed in claim 1 or 2, it is characterised in that the electrical tar precipitator (2) is horizontal dual field electric precipitation
Device.
4. the device as described in any one of claims 1 to 3, it is characterised in that the pre-oxidation system (3) supplies including oxidant
To equipment, dilution air, surge tank and distributor.
5. the device as described in any one of Claims 1 to 4, it is characterised in that the semidry method cleaning system (4) includes absorbing
Agent storehouse (5), spray nozzle (6), recirculating fluidized bed reaction tower (7)；
The bottom of the recirculating fluidized bed reaction tower (7) is inlet end, and the inlet end is provided with Venturi, the literary mound
In the air inlet of device connect the gas outlet of the pre-oxidation system (3), the gas outlet of the Venturi is followed positioned at described
The inside of ring fluid bed reacting tower (7)；
The expansion segment of the Venturi is provided with absorbent entrance and spray nozzle (6), and the absorbent entrance is with absorbing
Agent storehouse (5) is connected；
Preferably, the absorbent storehouse is filled with absorbent；
Preferably, the absorbent include flyash, lime, magnesia, red mud and carbide slag any one or at least two
Combination, preferred flyash.
6. device as claimed in claim 5, it is characterised in that the semidry method cleaning system (4) also includes cyclone separator
(8), sack cleaner (9) and ash silo (10)；
Preferably, the gas outlet of the recirculating fluidized bed reaction tower (7) is connected with the air inlet of the cyclone separator (8), institute
The gas outlet for stating cyclone separator (8) is connected with the air inlet of the sack cleaner (9), and sack cleaner (9) go out
Gas port is connected with the air inlet of the ash silo (10)；
Preferably, the bottom of the cyclone separator (8) is provided with the first separation hopper, and the outlet of the first separation hopper is provided with
Tie point and the second branch road, the tie point are connected with the expansion segment of the Venturi, second branch road and institute
Ash silo (10) is stated to be connected；
Preferably, the bottom of the sack cleaner (9) is provided with the second separation hopper, the outlet of the second separation hopper and ash
Storehouse (10) is connected；
Preferably, the outlet of the second separation hopper and the described first the second branch road remittance for separating hopper and rear and ash silo (10)
It is connected.
7. a kind of processing method of electrolytic aluminium carbon anode roasting flue gas, it is characterised in that methods described comprises the following steps：
1) the electrolytic aluminium carbon anode roasting flue gas is cooled, liquid bitumen tar is generated after cohesion；
2) flue gas through step 1) cooling carries out electrically trapped tar oil, removes liquid bitumen tar；
3) flue gas after step 2) electrically trapped tar oil is pre-oxidized；
4) flue gas after step 3) is pre-oxidized carries out semidry method purification, removes particulate matter, SO in flue gas2, high-valence state NOx, fluorine
Compound and glance coal, are purified flue gas.
8. method as claimed in claim 7, it is characterised in that methods described is utilized as described in any one of claim 1~6
Device is carried out.
9. method as claimed in claim 7 or 8, it is characterised in that the step 1) cooling is carried out in flue-gas-cooling system；
Preferably, the method for the step 1) cooling cools including water spraying atomization；
Preferably, the temperature of flue gas is 90~100 DEG C after the step 1) cooling；
Preferably, the step 2) electrically trapped tar oil is carried out in electrical tar precipitator；
Preferably, the pre-oxidation described in step 3) is carried out in pre-oxidation system；
Preferably, oxidant is appointing for hydrogen peroxide, ozone, potassium permanganate, sodium hypochlorite and sodium chlorite used by step 3)
Anticipate a kind of or at least two combinations；
Preferably, the semidry method purification described in step 4) is carried out in semidry method cleaning system；
Preferably, absorbent is flyash, lime, magnesia, red mud, carbide slag any or at least used by step 4)
Two kinds of combination, preferably flyash.
10. such as the purposes of any one of claim 1~6 described device, it is characterised in that described device is used for desulphurization denitration defluorinate
Depitching cigarette integrated purifying technique.
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108043192A (en) * | 2018-01-26 | 2018-05-18 | 福建龙净环保股份有限公司 | Pollutant removing system after a kind of stove |
| CN108310960A (en) * | 2018-03-06 | 2018-07-24 | 浙江哲丰能源发展有限公司 | A kind of method of desulphurization in circulating fluidized bed boiler |
| CN108998812A (en) * | 2018-09-29 | 2018-12-14 | 四川启明星铝业有限责任公司 | The method of the tarvia generated in processing electrolgtic aluminium prebaked anode production process |
| CN109157957A (en) * | 2018-10-26 | 2019-01-08 | 航天环境工程有限公司 | A kind of ultra-clean processing method of electrolytic aluminium carbon anode roasting flue gas and the system and application for implementing this method |
| CN109157961A (en) * | 2018-11-14 | 2019-01-08 | 中国科学院过程工程研究所 | A kind of multi-pollutant joint removing means, method and the purposes of electrolytic aluminium carbon anode roasting flue gas |
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| CN111013346A (en) * | 2019-12-27 | 2020-04-17 | 中国科学院过程工程研究所 | Electrolytic aluminum flue gas semi-dry desulfurization and defluorination system and method |
| CN111282416A (en) * | 2020-01-23 | 2020-06-16 | 国家电投集团远达环保工程有限公司重庆科技分公司 | Electrolytic aluminum carbon anode roasting flue gas purification equipment and method |
| WO2021134925A1 (en) * | 2019-12-30 | 2021-07-08 | 童裳慧 | Semi-dry flue gas desulfurization and denitrification method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20030019356A1 (en) * | 2001-07-12 | 2003-01-30 | Hansjorg Herden | Process and device for cleaning combustion flue gases |
| CN103566725A (en) * | 2013-10-15 | 2014-02-12 | 中国科学院过程工程研究所 | Device and method for jointly removing sulphur, saltpeter and mercury by semidry method through circulating fluidized bed |
| CN105195008A (en) * | 2015-10-23 | 2015-12-30 | 河北金科环保设备有限公司 | Process and equipment for flue gas roasting, adsorption desulfurization, dust removal and purification by adopting combination process |
-
2017
- 2017-09-30 CN CN201710940495.XA patent/CN107519751A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20030019356A1 (en) * | 2001-07-12 | 2003-01-30 | Hansjorg Herden | Process and device for cleaning combustion flue gases |
| CN103566725A (en) * | 2013-10-15 | 2014-02-12 | 中国科学院过程工程研究所 | Device and method for jointly removing sulphur, saltpeter and mercury by semidry method through circulating fluidized bed |
| CN105195008A (en) * | 2015-10-23 | 2015-12-30 | 河北金科环保设备有限公司 | Process and equipment for flue gas roasting, adsorption desulfurization, dust removal and purification by adopting combination process |
Non-Patent Citations (2)
| Title |
|---|
| 李建新等: "《燃烧污染物控制技术》", 31 December 2012, 中国电力出版社 * |
| 苏国全等: "《工业固体废渣在公路岩土工程中的应用研究》", 31 January 2015, 中国矿业大学出版社 * |
Cited By (14)
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| CN108043192A (en) * | 2018-01-26 | 2018-05-18 | 福建龙净环保股份有限公司 | Pollutant removing system after a kind of stove |
| CN108310960A (en) * | 2018-03-06 | 2018-07-24 | 浙江哲丰能源发展有限公司 | A kind of method of desulphurization in circulating fluidized bed boiler |
| CN108998812A (en) * | 2018-09-29 | 2018-12-14 | 四川启明星铝业有限责任公司 | The method of the tarvia generated in processing electrolgtic aluminium prebaked anode production process |
| CN109157957A (en) * | 2018-10-26 | 2019-01-08 | 航天环境工程有限公司 | A kind of ultra-clean processing method of electrolytic aluminium carbon anode roasting flue gas and the system and application for implementing this method |
| CN109224808A (en) * | 2018-11-06 | 2019-01-18 | 河北金科环保设备有限公司 | A kind of carbon baking kiln gas ultra-clean discharge cleaning equipment and purification method |
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| CN109499300A (en) * | 2018-12-11 | 2019-03-22 | 湖南涌鑫源环保有限公司 | The processing method of exhaust gas in a kind of recovery processing of cathode carbon pieces |
| CN109499300B (en) * | 2018-12-11 | 2021-08-17 | 湖南涌鑫源环保有限公司 | Method for treating waste gas in cathode carbon block recovery treatment |
| WO2021128472A1 (en) * | 2019-12-27 | 2021-07-01 | 中国科学院过程工程研究所 | Semi-dry desulfurization and defluorination system and method for aluminum electrolysis flue gas |
| CN111013346A (en) * | 2019-12-27 | 2020-04-17 | 中国科学院过程工程研究所 | Electrolytic aluminum flue gas semi-dry desulfurization and defluorination system and method |
| WO2021134925A1 (en) * | 2019-12-30 | 2021-07-08 | 童裳慧 | Semi-dry flue gas desulfurization and denitrification method |
| CN111282416A (en) * | 2020-01-23 | 2020-06-16 | 国家电投集团远达环保工程有限公司重庆科技分公司 | Electrolytic aluminum carbon anode roasting flue gas purification equipment and method |
| CN111282416B (en) * | 2020-01-23 | 2022-08-16 | 国家电投集团远达环保工程有限公司重庆科技分公司 | Electrolytic aluminum carbon anode roasting flue gas purification equipment and method |
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