CN108837677A - A kind for the treatment of process and its device of sintering flue gas minimum discharge - Google Patents
A kind for the treatment of process and its device of sintering flue gas minimum discharge Download PDFInfo
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- CN108837677A CN108837677A CN201810689817.2A CN201810689817A CN108837677A CN 108837677 A CN108837677 A CN 108837677A CN 201810689817 A CN201810689817 A CN 201810689817A CN 108837677 A CN108837677 A CN 108837677A
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- flue gas
- sodium bicarbonate
- active carbon
- deduster
- gas
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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
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/508—Sulfur oxides by treating the gases with solids
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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
- B01D53/70—Organic 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
- B01D53/75—Multi-step processes
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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
- 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
- B01D53/81—Solid phase processes
- B01D53/83—Solid phase processes with moving reactants
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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
- B01D53/86—Catalytic processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/206—Organic halogen compounds
- B01D2257/2064—Chlorine
-
- 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
Abstract
The present invention provides the treatment process and processing unit of a kind of sintering flue gas minimum discharge, on the basis of existing semidry method and bag-type dust mode, increases by a grade saleratus dry desulfurization, while bag filter being transformed, increases a set of SCR denitration device；Form a set of Multistage desulfuration, denitration, removing bioxin, modified go the sintering flue gas treatment process of chalk dust removing, sintering flue gas is handled using technique of the invention and device, sintering flue gas after treatment reaches minimum discharge requirement, low using technique and installation cost of the invention, small investment.
Description
Technical field
The present invention a kind for the treatment of process and device of sintering flue gas, and in particular to it is a kind of to use semidry method and dry desulfurization,
The treatment process and device of the sintering flue gas minimum discharge of bag-type dust, SCR denitration and removal bioxin；Belong to steel sintering
Production environment protects field.
Background technique
Sintering production is that modern steel produces one of most important technique unit, while sintering production is also steel and iron industry
Heavy polluter.Sintering process NOXDischarge amount accounts for about steel and iron industry NOX50%, S0 of total release2Discharge amount accounts for about steel and iron industry
The 60% of total release, steel industry sintering and electric furnace generate bioxin and account for the 25.9% of national dioxin emission total amount.With
Environmental Protection in China require increasingly raising, not only to sintering flue gas dust and SO2Discharge is stringenter, while to NOXHe bioxin
Discharge also proposed new requirement.《Steel sintering, pelletizing industrial air pollution object discharge standard》(GB28662-2012) in
In the special emission limit clear stipulaties of atmosphere pollution：Particulate matter is 40mg/m3,S02For 180mg/m3,NOXFor 300mg/m3, two
Evil English is 0.5ngTEQ/Nm3。
Sintering plant is most of only with semidry method, wet desulphurization and bag-type dust at present, can only achieve above-mentioned standard
It is required that.With the increasingly raising that Environmental Protection in China requires, not only to sintering flue gas dust and SO2Discharge is stringenter, while to NOX
The discharge of He bioxin also proposed new requirement, and sintering flue gas will reach minimum discharge requirement：That is Ke Li Wu≤10mg/m3,
S02≦35mg/m3,NOX≦50mg/m3, Er Evil Ying≤0.25ngTEQ/Nm3。
Reach These parameters, existing semidry method, wet desulphurization and bag-type dust are obviously not achieved.It burns currently on the market
For the mode many that knot fume treatment uses for semidry method and bag-type dust mode, semi-dry desulphurization efficiency can reach 90-95%,
SO2Discharge reaches 50-130mg/m3, granular material discharged to reach 20mg/m3,NOXHe bioxin does not remove substantially.Therefore existing
The requirement of minimum discharge is not achieved in technology.
Summary of the invention
For in the prior art, sintering flue gas is handled using semidry method and dust settling pocket technique, existing cannot reach ultralow
The problem of discharge, after sintering flue gas processing, the pollutant loads such as dust, oxysulfide, nitrogen oxides, bioxin are higher to be lacked
It falls into；The present invention provides a kind of at low cost, small investment, on the basis of existing semidry method and bag-type dust mode, increases level-one
Sodium bicarbonate dry desulfurization, while bag filter being transformed, increase a set of SCR denitration device；Formed a set of Multistage desulfuration,
The sintering flue gas treatment process of chalk dust removing is gone in denitration, removing bioxin, modified, is burnt using technique of the invention and device processing
Flue gas is tied, sintering flue gas after treatment reaches minimum discharge requirement.
The first embodiment provided according to the present invention provides a kind for the treatment of process of sintering flue gas minimum discharge.
A kind for the treatment of process of sintering flue gas minimum discharge, the technique include the following steps：
1) semidry method is handled：The former flue gas of sintering is delivered in semi-dry desulphurization tower and carries out desulfurization process；
2) sodium bicarbonate dry process：Flue gas after semi-dry desulphurization tower is delivered to dry type reaction by venturi nozzle
Device；Sodium bicarbonate spray head is equipped on venturi nozzle and active carbon spray head, sodium bicarbonate enter venturi nozzle from sodium bicarbonate spray head,
Active carbon powder enters venturi nozzle from active carbon spray head；Into the sodium bicarbonate and active carbon powder and cigarette in venturi nozzle
Gas is sufficiently mixed, and flue gas is then allowed to enter in dry type reactor further to remove the oxysulfide in flue gas He Er Evil
English；
3) deduster is handled：Flue gas by dry type reactor for treatment is dusted processing by deduster；
4) SCR is handled：Will by deduster, treated that flue gas is delivered in SCR reactor, SCR reactor to flue gas into
Row denitration process is neat stress, qualified discharge by SCR treated flue gas.
Preferably, in step 1), the desulfurizing agent in semi-dry desulphurization tower uses lime slurry, allows in desulfurizing agent and flue gas
Oxysulfide reacted, remove flue gas in oxysulfide.
Preferably, in step 2), into venturi nozzle sodium bicarbonate and active carbon powder and flue gas carry out it is abundant
After mixing, sodium bicarbonate powder and hot fume contact, extruding occurs rapidly, sodium bicarbonate powder particle surface forms porous structure, small
SO in soda powder and flue gas2Gas quickly efficiently reacts.Activated carbon adsorption flue gas Zhong bioxin.Flue gas enters dry
After formula reactor, dry type reactor further removes the oxysulfide in flue gas He bioxin.
Preferably, the deduster is bag filter in step 3).Sodium bicarbonate and active carbon powder dry type reactor
Interior to be uniformly mixed, after dry type reactor for treatment, sodium bicarbonate and active carbon powder enter bag filter, sodium bicarbonate with flue gas
Filter cake is formed on the surface of bag filter with active carbon powder, the oxysulfide in filter cake conversion and absorption flue gas is He Er Evil
English.Bag filter removes the dust in flue gas.
Preferably, being equipped with blowing device in the bag filter.Filter cake forms one section on the surface of bag filter
After time, filter cake converts and has adsorbed oxysulfide He bioxin.Blowing device is opened, the filter cake on bag filter surface is blown
Fall, be then shut off blowing device, fresh sodium bicarbonate and active carbon powder continue the surface for being adsorbed on bag filter, are formed new
Filter cake, new filter cake continue convert and adsorb flue gas in oxysulfide He bioxin.
Preferably, in step 4), will by deduster, treated that flue gas initially enters GGH heat exchanger heats,
By the heat of heat accumulating element in deduster treated smoke absorption GGH heat exchanger, ammonia is sprayed into after heat exchange in flue gas, then
By the mixed gas delivery of flue gas and ammonia into SCR reactor, SCR reactor handles flue gas, removes in flue gas
Nitrogen oxides is He bioxin.It is neat stress by SCR treated flue gas, neat stress enters GGH heat exchanger, with GGH heat exchanger
Internal heat accumulating element exchanges heat, and the heat accumulating element inside GGH heat exchanger absorbs the heat of neat stress, and heat accumulating element is for adding
Heat is by deduster treated flue gas.Neat stress after heat exchange passes through smoke stack emission.
Preferably, in step 4), by deduster, treated that flue gas enters GGH heat exchanger, after heat exchange, then leads to
It crosses fume heating furnace to be heated, then carries out spray ammonia in flue gas by ammonia-spraying grid, form the mixed gas of flue gas and ammonia.
In the present invention, by deduster, treated that flue gas enters GGH heat exchanger, and the temperature of flue gas is after heat exchange
180-280 DEG C, preferably 200-270 DEG C, more preferably 220-260 DEG C.
In the present invention, the temperature of the flue gas after being heated by fume heating furnace is 210-310 DEG C, preferably 245-
300 DEG C, more preferably 250-290 DEG C.
Second of the embodiment provided according to the present invention provides a kind of processing unit of sintering flue gas minimum discharge.
A kind of processing unit of sintering flue gas minimum discharge or place for treatment process described in the first embodiment
Device is managed, which includes：Semi-dry desulphurization tower, venturi nozzle, dry type reactor, deduster, SCR reactor.It burns
Tie the smoke inlet that former flue gas is delivered to semi-dry desulphurization tower via former smoke conveying duct.It is de- that venturi nozzle connects semidry method
The exhanst gas outlet of sulphur tower and the smoke inlet of dry type reactor.The exhanst gas outlet of dry type reactor is connected by the first conveyance conduit
To the gas access of deduster.The gas vent of deduster is connected to the gas access of SCR reactor by the second conveyance conduit.
The gas vent of SCR reactor is connect with neat stress discharge tube.Wherein：Venturi nozzle is equipped with sodium bicarbonate spray head and activity
Charcoal spray head.
Preferably, the processing unit further includes：GGH heat exchanger and ammonia-spraying grid.GGH heat exchanger is defeated with second respectively
Send pipeline to connect with neat stress discharge tube, also, the heat accumulating element in GGH heat exchanger respectively with the cigarette in the second conveyance conduit
Neat stress in gas, neat stress discharge tube exchanges heat.Ammonia-spraying grid is arranged on the second conveyance conduit, and is located at GGH
The downstream of heat exchanger and the second conveyance conduit link position.
Preferably, the processing unit further includes：Fume heating furnace.Fume heating furnace is arranged in the second conveyance conduit
On, and it is located at the downstream of GGH heat exchanger and the second conveyance conduit link position, positioned at the upstream of ammonia-spraying grid.
Preferably, the processing unit further includes：Sodium bicarbonate storage tank and active carbon storage tank.Sodium bicarbonate storage tank and sodium bicarbonate
Spray head connection.Active carbon storage tank is connect with active carbon spray head.
Preferably, the processing unit further includes：Chimney.Neat stress discharge tube is connected to chimney.
Preferably, neat stress discharge tube is equipped with air-introduced machine.
Preferably, the deduster is bag filter, blowing device is equipped in bag filter.
In the present invention, semi-dry desulphurization is handled in step 1), and desulfurizing agent generally uses lime paddle liquid Ca (OH)2, reaction
After generate CaSO4, desulfuration efficiency can reach 90-95%.According to the feature of former flue gas and the temperature of former flue gas, first using half-dried
Method carries out desulfurization process, this is also scheme commonly used in the prior art.Most of sintering machines are configured with semidry method processing unit, edge
With the device, investment reduction cost.
In the present invention, in step 2), the flue gas after step 1) desulfurization enters back into venturi nozzle, in venturi
Jet pipe is equipped with sodium bicarbonate and active carbon spray head, into venturi nozzle sodium bicarbonate and active carbon and flue gas carry out it is sufficiently mixed
It closes, after sodium bicarbonate powder and hot fume contact, extruding occurs rapidly, powder particle surface forms porous structure, substantially increases
The specific surface area of sodium bicarbonate, so that sodium bicarbonate and SO2Gas can quickly and efficiently react.Using venturi nozzle position
Penetrating sodium bicarbonate is set, using the temperature of former flue gas, sodium bicarbonate is heated volume expansion, and the absorption property of sodium bicarbonate is preferable.Spray
Enter sodium bicarbonate, first, sodium bicarbonate can adsorb the oxysulfide in flue gas；The second, sodium bicarbonate can be in subsequent deduster
Filter cake is formed on cloth bag.Sodium bicarbonate is added in the position, and after dry type is reacted, sodium bicarbonate can be sufficiently mixed with flue gas, just
In the subsequent processing in deduster.Active carbon powder, the absorption property of active carbon powder are sprayed into using venturi nozzle position
Preferably.Penetrating active carbon powder, first, active carbon powder can adsorb the oxysulfide in flue gas；The second, active carbon powder exists
Filter cake can be formed in subsequent deduster on cloth bag.Active carbon powder is added in the position, after dry type is reacted, activity
Carbon powder can be sufficiently mixed with flue gas, convenient for the subsequent processing in deduster.
In flue gas after venturi nozzle, penetrating has sodium bicarbonate and active carbon powder, into dry type reactor, little Su
It beats and active carbon powder and flue gas is sufficiently mixed in dry type reactor, and convert and adsorb the oxysulfide and two in flue gas
Evil English；Mixed flue gas enters dry type reactor, and the reaction was continued, removes part SO2He bioxin.
In the present invention, sodium bicarbonate (NaHCO3) effect be：It is reacted with sulfur dioxide and generates harmless sodium sulphate, dioxy
Change carbon and water.
Reacting quintessence：SO2+H2O=H2SO3；
Then：H2SO3+NaHCO3=NaHSO3+CO2↑+H2O；
H2SO3+2NaHCO3=Na2SO3+2CO2↑+2H2。
The effect of active carbon is：Adsorb oxysulfide, bioxin and mercury.
In the present invention, in step 3), the flue gas by dry type reactor for treatment enters back into bag filter and further takes off
Except SO2He bioxin.In the step, main desulphurization reaction is the filter bag surface progress in bag filter, sodium bicarbonate, activity
Carbon powder from dry type reactor come out after, enter bag filter with flue gas because have in dry type reactor it is abundant mix
It closes, so highly uniform filter bag surface can be adsorbed on, forms certain thickness filter cake.Flue gas is entering cloth bag by filter cake
When, the SO in flue gas2It comes into full contact with and reacts with filter cake (sodium bicarbonate, active powdered carbon) with bioxin, adsorb, reach desulfurization and go
The purpose of Chu bioxin.The active carbon powder of filter cake and sodium bicarbonate group at.
In addition, compared with the prior art, due to having sprayed into sodium bicarbonate and active carbon powder in venturi nozzle, sodium bicarbonate and
Active carbon powder forms certain thickness filter cake on the cloth bag of bag filter, and filter cake is for dust in flue gas (particulate matter)
It is more excellent to capture effect, due to the formation of filter cake, increases bag filter to the dust removing effects of flue gas.
In the present invention, filter cake is made of sodium bicarbonate powder and active carbon powder, sodium bicarbonate powder and active carbon powder with
It after high-temperature flue gas mixing, is influenced by high temperature, sodium bicarbonate and active carbon expand, and volume increases, and specific surface area is significantly
Increase, also increases the effective area of sodium bicarbonate and active carbon and smoke contacts.The effect of filter cake：One, in sodium bicarbonate and flue gas
Oxysulfide chemically react, convert oxysulfide to containing sulfosalt and carbon dioxide, effective desulfurization；Two, sodium bicarbonate and
Active carbon adsorbs the oxysulfide in flue gas He bioxin, reduces the oxysulfide in flue gas He bioxin by physical absorption
Content；Three, filter cake forms filtering barrier together, is similar to " sieve ", the significantly more efficient dust (particulate matter) removed in flue gas,
Improve the dust removing effects of deduster.
Preferably, blowing device is equipped in bag filter.By the blowing of filter bag, the automatic of filter cake is realized
Timing is replaced.The low filter cake of desulfuration efficiency (filter cake after converting and having adsorbed a period of time) is blown off, and ash bucket is fallen into, fresh
Sodium bicarbonate and active carbon powder will continue to be adsorbed on filter bag, form new filter cake.That is, filter cake is in bag filter
After surface forms a period of time, filter cake converts and has adsorbed oxysulfide He bioxin.Blowing device is opened, by bag filter
The filter cake on surface is blown off, is then shut off blowing device, and fresh sodium bicarbonate and active carbon powder continue to be adsorbed on bag filter
Surface, form new filter cake, new filter cake continues to convert and adsorb the oxysulfide in flue gas He bioxin.
In the present invention, step 4) is SCR reaction, and under the effect of the catalyst, ammonia is selectively the NO in flue gasx
It is reduced to nontoxic and pollution-free nitrogen and water, while bioxin is largely decomposed reaction in SCR reactor.Flue gas exists
Reach removing NO in SCR reactorxThe purpose of bioxin is removed again.The denitration of SCR reactor and the effect for decomposing bioxin
Rate all can reach 90%, NOx Ke Da Dao≤50mg/m3, bioxin Ke Da Dao≤0.25ngTEQ/Nm3。
Preferably, adding GGH heat exchanger, the heat in the flue gas after SCR reactor for treatment is exchanged heat by GGH
Device is passed to by deduster treated flue gas (entering the flue gas before SCR reactor), when being lifted into SCR reactor
The temperature of flue gas improves SCR reactor for nitrogen oxides He the removal efficiency of bioxin.Due to the setting of fume heating furnace,
The temperature of flue gas after SCR reactor for treatment is higher than the temperature by deduster treated flue gas；Therefore, using GGH
Heat transfer and utilization are saved heat resources by heat exchanger.
In treatment process of the invention, the semidry method processing of step 1) is first time desulfurization；Sodium bicarbonate is sprayed into step 2)
It is second of desulfurization, first time Tuo bioxin with active carbon powder；Dry type reactor is third time desulfurization, second of Tuo bis- Evil
English；The deduster processing of step 3) is the 4th desulfurization, third time Tuo bioxin；The SCR reactor for treatment of step 4) be denitration,
4th Tuo bioxin.Using technique of the invention, for former flue gas is sintered, the oxysulfide in former flue gas is He bioxin is distinguished
It is handled by four removings, the pollutant that processing is sintered in former flue gas can be very good using this technique and the device of the invention,
After treatment, reach the standard of minimum discharge.
In addition, existing sintering device flue gas processing unit can be used in the device of the invention and technique, in the base of existing apparatus
It on plinth, is added or is improved, the former flue gas of sintering can be handled well.Former cigarette is sintered if only handling using existing apparatus
Gas, after treatment, pollutant load is higher in the flue gas of discharge, cannot reach minimum discharge standard.Technical side of the invention
In case, retain original sintering machine original flue gas processing device, reduce cost of investment, by adding or improving, improves and be sintered former cigarette
The processing capacity of gas promotes the removal efficiency and removal effect of pollutant；Mitigate the pollution to environment.
In the present invention, sintering flue gas, the former flue gas of sintering, former flue gas are the flue gas that sintering machine generates, general, that is,
Flue gas to be treated.Semi-dry desulphurization tower, dry type reactor, SCR reactor are to commonly use in existing sintering flue gas processing technique
Device.The oxysulfide being sintered in former flue gas is mainly sulfur dioxide (SO2)。
Compared with prior art, technical solution of the present invention has following advantageous effects：
1, the present invention adds a set of sodium bicarbonate dry desulfurization device, will be by semidry method treated flue gas using dry method
Processing, and spray into sodium bicarbonate and active carbon powder in flue gas and sulfureous in flue gas oxygen is substantially increased by the synergistic effect of the two
The removal efficiency of compound He bioxin；
2, bag filter is transformed by the present invention, blowing device is added, due to the spray of active carbon powder and sodium bicarbonate
Enter, forms filter cake on the surface of bag filter, filter cake conversion and absorption sulfur dioxide improve dedusting effect He bioxin
Fruit；Blowing device can be the filter cake on replacement cloth bag in time；
3, the present invention adds a set of SCR denitration device, and by the processing of preceding step, oxysulfide processing is more thorough,
SCR reactor focuses on the nitrogen oxides in flue gas He bioxin, is selectively handled, SCR reactor is to nitrogen oxides
The removal effect of He bioxin is obvious.
Detailed description of the invention
Fig. 1 is a kind of structural schematic diagram of the processing unit of sintering flue gas minimum discharge of the present invention；
Fig. 2 is that a kind of processing unit of sintering flue gas minimum discharge of the present invention is equipped with GGH heat exchanger, ammonia-spraying grid, flue gas
Another design structure schematic diagram of the components such as heating furnace；
Fig. 3 is a kind of flow chart of the treatment process of sintering flue gas minimum discharge of the present invention；
Fig. 4 is the flow chart of pollutant removing in a kind for the treatment of process of sintering flue gas minimum discharge of the present invention.
Appended drawing reference：
1：Semi-dry desulphurization tower；2：Venturi nozzle；201：Sodium bicarbonate spray head；202：Active carbon spray head；3：Dry type reaction
Device；4：Deduster；5：SCR reactor；6：GGH heat exchanger；7：Ammonia-spraying grid；8：Fume heating furnace；9：Sodium bicarbonate storage tank；10：
Active carbon storage tank；11：Chimney；12：Air-introduced machine；L0：Former smoke conveying duct；L1：First conveyance conduit；L2：Second delivery pipe
Road；L3：Neat stress discharge tube.
Specific embodiment
A kind of processing unit of sintering flue gas minimum discharge, the processing unit include：Semi-dry desulphurization tower 1, venturi spray
Pipe 2, dry type reactor 3, deduster 4, SCR reactor 5.It is sintered former flue gas and is delivered to semidry method via former smoke conveying duct L0
The smoke inlet of desulfurizing tower 1.The flue gas of exhanst gas outlet and dry type reactor 3 that venturi nozzle 2 connects semi-dry desulphurization tower 1 enters
Mouthful.The exhanst gas outlet of dry type reactor 3 is connected to the gas access of deduster 4 by the first conveyance conduit L1.The gas of deduster 4
Body exports the gas access that SCR reactor 5 is connected to by the second conveyance conduit L2.The gas vent of SCR reactor 5 and net cigarette
The L3 connection of gas discharge tube.Wherein：Venturi nozzle 2 is equipped with sodium bicarbonate spray head 201 and active carbon spray head 202.
Preferably, the processing unit further includes：GGH heat exchanger 6 and ammonia-spraying grid 7.GGH heat exchanger 6 is respectively with
Two conveyance conduit L2 are connected with neat stress discharge tube L3, also, the heat accumulating element in GGH heat exchanger 6 is conveyed with second respectively
The neat stress in flue gas, neat stress discharge tube L3 in pipeline L2 exchanges heat.Ammonia-spraying grid 7 is arranged in the second conveyance conduit
On L2, and it is located at the downstream of GGH heat exchanger 6 and the second conveyance conduit L2 link position.
Preferably, the processing unit further includes：Fume heating furnace 8.Fume heating furnace 8 is arranged in the second conveyance conduit
On L2, and it is located at the downstream of GGH heat exchanger 6 and the second conveyance conduit L2 link position, positioned at the upstream of ammonia-spraying grid 7.
Preferably, the processing unit further includes：Sodium bicarbonate storage tank 9 and active carbon storage tank 10.Sodium bicarbonate storage tank 9 with it is small
Soda spray head 201 connects.Active carbon storage tank 10 is connect with active carbon spray head 202.
Preferably, the processing unit further includes：Chimney 11.Neat stress discharge tube L3 is connected to chimney 11.
Preferably, neat stress discharge tube L3 is equipped with air-introduced machine 12.
Preferably, the deduster 4 is bag filter, blowing device is equipped in bag filter.
Embodiment 1
As shown in Figure 1, a kind of processing unit of sintering flue gas minimum discharge, the processing unit include：Semi-dry desulphurization tower
1, venturi nozzle 2, dry type reactor 3, deduster 4, SCR reactor 5.It is defeated via former smoke conveying duct L0 to be sintered former flue gas
It send to the smoke inlet of semi-dry desulphurization tower 1.Venturi nozzle 2 connects exhanst gas outlet and the dry type reaction of semi-dry desulphurization tower 1
The smoke inlet of device 3.The exhanst gas outlet of dry type reactor 3 is connected to the gas access of deduster 4 by the first conveyance conduit L1.
The gas vent of deduster 4 is connected to the gas access of SCR reactor 5 by the second conveyance conduit L2.The gas of SCR reactor 5
Body outlet is connect with neat stress discharge tube L3.Wherein：Venturi nozzle 2 is equipped with sodium bicarbonate spray head 201 and active carbon spray head
202.The deduster 4 is bag filter, is equipped with blowing device in bag filter.
Embodiment 2
As shown in Fig. 2, repeating embodiment 1, only the processing unit further includes：GGH heat exchanger 6 and ammonia-spraying grid 7.
GGH heat exchanger 6 is connect with the second conveyance conduit L2 and neat stress discharge tube L3 respectively, also, the accumulation of heat in GGH heat exchanger 6
Element exchanges heat with the flue gas in the second conveyance conduit L2, the neat stress in neat stress discharge tube L3 respectively.Ammonia-spraying grid 7
It is arranged on the second conveyance conduit L2, and is located at the downstream of GGH heat exchanger 6 and the second conveyance conduit L2 link position.
The processing unit further includes：Fume heating furnace 8.Fume heating furnace 8 is arranged on the second conveyance conduit L2, and
Positioned at the downstream of GGH heat exchanger 6 and the second conveyance conduit L2 link position, positioned at the upstream of ammonia-spraying grid 7.The processing unit
Further include：Chimney 11.Neat stress discharge tube L3 is connected to chimney 11.Neat stress discharge tube L3 is equipped with air-introduced machine 12.
Embodiment 3
Embodiment is repeated, only the processing unit further includes：Sodium bicarbonate storage tank 9 and active carbon storage tank 10.Sodium bicarbonate storage
Tank 9 is connect with sodium bicarbonate spray head 201.Active carbon storage tank 10 is connect with active carbon spray head 202.
Embodiment 4
Using the method for processing unit described in embodiment 1, a kind for the treatment of process of sintering flue gas minimum discharge, the technique packet
Include following steps：
1) semidry method is handled：The former flue gas of sintering is delivered in semi-dry desulphurization tower and carries out desulfurization process；
2) sodium bicarbonate dry process：Flue gas after semi-dry desulphurization tower is delivered to dry type reaction by venturi nozzle
Device；Sodium bicarbonate spray head is equipped on venturi nozzle and active carbon spray head, sodium bicarbonate enter venturi nozzle from sodium bicarbonate spray head,
Active carbon powder enters venturi nozzle from active carbon spray head；Into the sodium bicarbonate and active carbon powder and cigarette in venturi nozzle
Gas is sufficiently mixed, and flue gas is then allowed to enter in dry type reactor further to remove the oxysulfide in flue gas He Er Evil
English；
3) deduster is handled：Flue gas by dry type reactor for treatment is dusted processing by deduster；
4) SCR is handled：Will by deduster, treated that flue gas is delivered in SCR reactor, SCR reactor to flue gas into
Row denitration process is neat stress, qualified discharge by SCR treated flue gas.
Embodiment 5
Using the method for processing unit described in embodiment 2, a kind for the treatment of process of sintering flue gas minimum discharge, the technique packet
Include following steps：
1) semidry method is handled：Dust, SO will be contained2、NOXThe sintering original flue gas (130 DEG C) of He bioxin is delivered to semidry method
Desulfurization process is carried out in desulfurizing tower；Desulfurizing agent in semi-dry desulphurization tower uses lime slurry Ca (OH)2, generated after reaction
CaSO4, desulfurizing agent reacted with the oxysulfide in flue gas, removes the oxysulfide in flue gas；
Semidry method processing, desulfuration efficiency can reach 90-95%.
2) sodium bicarbonate dry process：Flue gas after semi-dry desulphurization tower is delivered to dry type reaction by venturi nozzle
Device；Sodium bicarbonate spray head is equipped on venturi nozzle and active carbon spray head, sodium bicarbonate enter venturi nozzle from sodium bicarbonate spray head,
Active carbon powder enters venturi nozzle from active carbon spray head；Into the sodium bicarbonate and active carbon powder and cigarette in venturi nozzle
Gas is sufficiently mixed, and after sodium bicarbonate powder and hot fume contact, extruding occurs rapidly, sodium bicarbonate powder particle surface forms more
Pore structure substantially increases the specific surface area of sodium bicarbonate powder, the SO in sodium bicarbonate powder and flue gas2Gas is quick and efficient
Reaction.Active carbon conversion and absorption flue gas Zhong bioxin.After flue gas enters dry type reactor, dry type reactor is further removed
Oxysulfide in flue gas is He bioxin；
3) deduster is handled：Flue gas by dry type reactor for treatment is dusted processing by deduster；The dedusting
Device is bag filter.It is uniformly mixed in sodium bicarbonate and active carbon powder dry type reactor, it is small after dry type reactor for treatment
Soda and active carbon powder enter bag filter, sodium bicarbonate and active carbon powder with flue gas and are formed on the surface of bag filter
Filter cake, SO of the flue gas when entering cloth bag by filter cake, in flue gas2It is come into full contact with simultaneously with bioxin and sodium bicarbonate, active powdered carbon
Reaction, absorption, filter cake convert and adsorb the oxysulfide in flue gas He bioxin；Bag filter removes the dust in flue gas；
By step 2) and 3) for by semidry method treated flue gas, after handling, desulfuration efficiency can reach 90%,
S02Ke Da Dao≤35mg/m3, Tuo bioxin efficiency can reach 30%, and efficiency of dust collection can reach 99.99% or more, and particulate matter is reachable
Dao≤10mg/m3。
4) SCR is handled：Will by deduster, treated that flue gas initially enters GGH heat exchanger heats, be warming up to 250
DEG C, by the heat of heat accumulating element in deduster treated smoke absorption GGH heat exchanger, after heat exchange, then pass through flue gas
Heating furnace carries out being heated to 280 DEG C, then carries out spray ammonia in flue gas by ammonia-spraying grid, forms the gaseous mixture of flue gas and ammonia
Body；Again by the mixed gas delivery of flue gas and ammonia into SCR reactor, SCR reactor carries out denitration process to flue gas, is urging
Under the action of agent, ammonia is selectively reduced to the NOx in flue gas nontoxic and pollution-free nitrogen and water, while bioxin exists
It largely decomposes in SCR reactor reaction；The nitrogen oxides in flue gas is removed He bioxin.By SCR treated cigarette
Gas is neat stress, and neat stress enters GGH heat exchanger, is exchanged heat with the heat accumulating element inside GGH heat exchanger, in GGH heat exchanger
The heat accumulating element in portion absorbs the heat of neat stress, and heat accumulating element is for heating by deduster treated flue gas.By heat exchange
Neat stress afterwards passes through smoke stack emission.
The denitration of SCR reactor and the efficiency for decomposing bioxin all can reach 90%, NOx Ke Da Dao≤50mg/m3, bioxin
Ke Da Dao≤0.25ngTEQ/Nm3。
Embodiment 6
Embodiment 5 is repeated, blowing device is only equipped in the bag filter.Surface shape of the filter cake in bag filter
After a period of time, filter cake converts and has adsorbed oxysulfide He bioxin.Blowing device is opened, by bag filter surface
Filter cake is blown off, is then shut off blowing device, and fresh sodium bicarbonate and active carbon powder continue the surface for being adsorbed on bag filter,
New filter cake is formed, new filter cake continues to convert and adsorb the oxysulfide in flue gas He bioxin.
Using one 180m of process of embodiment 62The sintering flue gas (or to be sintered former flue gas) that sintering machine generates：
Sintering device flue gas amount：65x104Nm3/h；Temperature：130℃；Particulate matter：50mg/m3；S02Amount：1500mg/m3；NOx
Measure 300mg/m3；Bioxin amount：3ngTEQ/Nm3
After step 1) of the present invention processing：
In flue gas after desulfurization process：S02Content is 150mg/m3；
After step 2) of the present invention and step 3) processing：
In flue gas after sodium bicarbonate dry process：S02Content is 15mg/m3；Particle content is 8mg/m3；Bioxin contains
Amount is 2.1ngTEQ/Nm3；
After step 4) of the present invention processing：
In flue gas after SCR reactor for treatment：Particle content is 8mg/m3；S02Content is 15mg/m3；NOx content is
30mg/m3；Content of dioxin is 0.21ngTEQ/Nm3。
It is handled using technical solution of the present invention and is sintered former flue gas, sintering flue gas can reach minimum discharge requirement.
Semi-dry desulphurization and bag filter have been had in especially existing many steel mills, on this basis, need to only be transformed, increase by the
Two-grade desulfurizing, Tuo bioxin, bag filter transformation and SCR reactor, sintering flue gas can reach the requirement of minimum discharge.
It is the good method that one kind can reach minimum discharge requirement and reduce investment outlay.
In addition, compared with prior art, by spraying into sodium bicarbonate and active carbon powder in flue gas, passing through the collaboration of the two
Effect, significantly improves sulfureous in flue gas oxide He the removal efficiency of bioxin.
Claims (10)
1. a kind for the treatment of process of sintering flue gas minimum discharge, the technique include the following steps：
1) semidry method is handled：The former flue gas of sintering is delivered in semi-dry desulphurization tower and carries out desulfurization process；
2) sodium bicarbonate dry process：Flue gas after semi-dry desulphurization tower is delivered to dry type reactor by venturi nozzle；
Sodium bicarbonate spray head and active carbon spray head are equipped on venturi nozzle, sodium bicarbonate enters venturi nozzle from sodium bicarbonate spray head, living
Property carbon powder enters venturi nozzle from active carbon spray head；Into the sodium bicarbonate and active carbon powder and flue gas in venturi nozzle
It is sufficiently mixed, flue gas is then allowed to enter in dry type reactor further to remove the oxysulfide in flue gas He Er Evil
English；
3) deduster is handled：Flue gas by dry type reactor for treatment is dusted processing by deduster；
4) SCR is handled：Will by deduster, treated that flue gas is delivered in SCR reactor, SCR reactor takes off flue gas
Nitre processing is neat stress, qualified discharge by SCR treated flue gas.
2. treatment process according to claim 1, it is characterised in that：Desulfurizing agent in step 1), in semi-dry desulphurization tower
Using lime slurry, desulfurizing agent is allowed to be reacted with the oxysulfide in flue gas, removes the oxysulfide in flue gas；And/or
In step 2), into venturi nozzle sodium bicarbonate and active carbon powder be sufficiently mixed with flue gas, saleratus power
Behind end and hot fume contact, extruding occurs rapidly, sodium bicarbonate powder particle surface forms porous structure, sodium bicarbonate powder and flue gas
In SO2Gas quickly efficiently reacts, activated carbon adsorption flue gas Zhong bioxin；After flue gas enters dry type reactor, do
Formula reactor further removes the oxysulfide in flue gas He bioxin.
3. treatment process according to claim 1 or 2, it is characterised in that：In step 3), the deduster is bag-type dust
Device；It is uniformly mixed in sodium bicarbonate and active carbon powder dry type reactor, after dry type reactor for treatment, sodium bicarbonate and active carbon
Powder enters bag filter, sodium bicarbonate and active carbon powder with flue gas and forms filter cake on the surface of bag filter, and filter cake turns
Change and adsorbs the oxysulfide in flue gas He bioxin, bag filter remove the dust in flue gas；
It is preferred that being equipped with blowing device in the bag filter；After filter cake forms a period of time on the surface of bag filter, filter
Cake converts and has adsorbed oxysulfide He bioxin；Blowing device is opened, the filter cake on bag filter surface is blown off, is then closed
Blowing device is closed, fresh sodium bicarbonate and active carbon powder continue the surface for being adsorbed on bag filter, form new filter cake, newly
Filter cake continue convert and adsorb flue gas in oxysulfide He bioxin.
4. treatment process according to any one of claim 1-3, it is characterised in that：In step 4), deduster will be passed through
Treated, and flue gas initially enters GGH heat exchanger is heated, by storing in deduster treated smoke absorption GGH heat exchanger
The heat of thermal element, sprays into ammonia in flue gas after heat exchange, then by the mixed gas delivery of flue gas and ammonia to SCR reactor
In, SCR reactor handles flue gas, removes the nitrogen oxides in flue gas He bioxin；By SCR, treated that flue gas is
Neat stress, neat stress enter GGH heat exchanger, exchange heat with the heat accumulating element inside GGH heat exchanger, inside GGH heat exchanger
Heat accumulating element absorbs the heat of neat stress, and heat accumulating element is for heating by deduster treated flue gas；After heat exchange
Neat stress passes through smoke stack emission；
It is preferred that in step 4), by deduster, treated that flue gas enters GGH heat exchanger, adds after heat exchange, then through flue gas
Hot stove is heated, and then carries out spray ammonia in flue gas by ammonia-spraying grid, forms the mixed gas of flue gas and ammonia.
5. treatment process according to claim 4, it is characterised in that：By deduster, treated that flue gas enters GGH changes
Hot device, the temperature of flue gas is 180-280 DEG C after heat exchange, preferably 200-270 DEG C, more preferably 220-260 DEG C；And/or
The temperature of flue gas after being heated by fume heating furnace be 210-310 DEG C, preferably 245-300 DEG C, more preferably
250-290℃。
6. a kind of processing unit of sintering flue gas minimum discharge or the place for treatment process described in any one of claim 1-5
Device is managed, which includes：Semi-dry desulphurization tower (1), venturi nozzle (2), dry type reactor (3), deduster (4),
SCR reactor (5)；It is sintered the smoke inlet that former flue gas is delivered to semi-dry desulphurization tower (1) via former smoke conveying duct (L0),
Venturi nozzle (2) connects the exhanst gas outlet of semi-dry desulphurization tower (1) and the smoke inlet of dry type reactor (3), dry type reaction
The exhanst gas outlet of device (3) is connected to the gas access of deduster (4), the gas of deduster (4) by the first conveyance conduit (L1)
Outlet is connected to the gas accesses of SCR reactor (5) by the second conveyance conduit (L2), the gas vent of SCR reactor (5) with
Neat stress discharge tube (L3) connection；Wherein：Venturi nozzle (2) is equipped with sodium bicarbonate spray head (201) and active carbon spray head
(202)。
7. processing unit according to claim 6, it is characterised in that：The processing unit further includes：GGH heat exchanger (6)
With ammonia-spraying grid (7)；GGH heat exchanger (6) is connect with the second conveyance conduit (L2) and neat stress discharge tube (L3) respectively, and
And the heat accumulating element in GGH heat exchanger (6) respectively with flue gas, the neat stress discharge tube (L3) in the second conveyance conduit (L2)
Interior neat stress exchanges heat；Ammonia-spraying grid (7) be arranged on the second conveyance conduit (L2), and be located at GGH heat exchanger (6) with
The downstream of the second conveyance conduit (L2) link position.
8. processing unit according to claim 7, it is characterised in that：The processing unit further includes：Fume heating furnace
(8)；Fume heating furnace (8) is arranged on the second conveyance conduit (L2), and is located at GGH heat exchanger (6) and the second conveyance conduit
(L2) downstream of link position is located at the upstream of ammonia-spraying grid (7).
9. processing unit a method according to any one of claims 6-8, it is characterised in that：The processing unit further includes：It is small
Soda storage tank (9) and active carbon storage tank (10)；Sodium bicarbonate storage tank (9) is connect with sodium bicarbonate spray head (201), active carbon storage tank (10)
It is connect with active carbon spray head (202).
10. the processing unit according to any one of claim 6-9, it is characterised in that：The processing unit further includes：Cigarette
Chimney (11), neat stress discharge tube (L3) are connected to chimney (11)；Preferably, neat stress discharge tube (L3) is equipped with air inducing
Machine (12)；And/or
The deduster (4) is bag filter, is equipped with blowing device in bag filter.
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| CN109663500A (en) * | 2019-03-04 | 2019-04-23 | 浙江深度能源技术有限公司 | A kind of mostly de- bag filter of smoke catalytic |
| CN110433633A (en) * | 2019-09-04 | 2019-11-12 | 无锡市东方工业节能环保有限公司 | A kind of sintering machine desulfuration denitration disappears white integral control system |
| CN110538557A (en) * | 2019-09-04 | 2019-12-06 | 无锡市东方工业节能环保有限公司 | Desulfurization, denitrification and whitening integrated system for sintering machine |
| CN111151108A (en) * | 2020-02-21 | 2020-05-15 | 中冶大地工程咨询有限公司 | Sintering machine head flue gas desulfurization and denitrification treatment device and treatment method thereof |
| CN112370946A (en) * | 2020-11-17 | 2021-02-19 | 南通联恒新材料有限公司 | Multiple treatment system for absorbing dioxin in flue gas |
| CN114504944A (en) * | 2022-01-26 | 2022-05-17 | 大冶有色金属有限责任公司 | Composite desulfurizer for low-concentration sulfur dioxide flue gas desulfurization and application thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109663500A (en) * | 2019-03-04 | 2019-04-23 | 浙江深度能源技术有限公司 | A kind of mostly de- bag filter of smoke catalytic |
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| CN110538557A (en) * | 2019-09-04 | 2019-12-06 | 无锡市东方工业节能环保有限公司 | Desulfurization, denitrification and whitening integrated system for sintering machine |
| CN111151108A (en) * | 2020-02-21 | 2020-05-15 | 中冶大地工程咨询有限公司 | Sintering machine head flue gas desulfurization and denitrification treatment device and treatment method thereof |
| CN112370946A (en) * | 2020-11-17 | 2021-02-19 | 南通联恒新材料有限公司 | Multiple treatment system for absorbing dioxin in flue gas |
| CN114504944A (en) * | 2022-01-26 | 2022-05-17 | 大冶有色金属有限责任公司 | Composite desulfurizer for low-concentration sulfur dioxide flue gas desulfurization and application thereof |
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Application publication date: 20181120 |